NL8202327A - METHOD FOR PARTIAL OXYDATION - Google Patents

Description

82301 VA / mm ^,

Short designation: Process for partial oxidation.

This invention relates to the preparation of gaseous mixtures comprising H 2 and CO, for example, synthesis gas, fuel gas, and reducing gas by the partial oxidation of pumpable suspensions of solid carbonaceous fuels in a liquid carrier and / or liquid or gaseous shaped hydrocarbon fuels. In one of its more specific aspects, the present invention relates to switching from one type of fuel to another without interrupting the process.

In the operation of a synthesis gas generator by partial oxidation, it is when the primary fuel is no longer available or is under-supplied and it is desired to operate the gas generator with a replacement or reserve fuel than previously necessary. release the pressure from the system and shut down the gas generator while the burner is being changed and other adjustments are made to the system to make it suitable for the new fuel. Such a costly downtime is avoided by the present method.

The annular type burners have been used for introducing liquid hydrocarbon fuels into a gas generator for partial oxidation. For example

U.S. Patent 3,528,930 shows a single annular burner, and U.S. Pat. patents 3,758,037 and 3,847,564 See 25 double annular burners. To achieve suitable mixing, atomization, and operating stability, * a burner is selected for a specific pass-through. As 8202327

I X

Substantially changing the type of fuel feed stream or required product gas yield, system shutdown is usually required to replace one burner with another. Such costly shutdowns are avoided by the present method and the present operating system.

The more complex process of preheating a gas generator by means of a preheating burner, removing the preheating burner from the gasifier, and inserting a separate production burner has been described in U.S. Pat. patent 4,113,445.

A method of partial oxidation and control system for continuous production of synthesis gas, fuel gas or reducing gas while changing from one type of fuel to another without shutting down the gas generator or releasing its pressure is described. This multi-fuel process is not bound to a special fuel and produces reaction suspensions of solid carbonaceous fuel and / or liquid or gaseous hydrocarbon fuel. Fuel availability problems are reduced due to the wide selection of fuels suitable for the present process. By the present process, the total yield of the gas generator by partial oxidation can be kept almost constant while the feed is changed from one fuel to another.

The present invention relates to a process for the preparation of gaseous mixtures containing H 2, CO, CO 2, entrained carbon particles, and at least one material from the group consisting of H 2, N, H 2 Sf COS, CH., A, and ash, in a free-flow catalytic partial oxidation gas generator, comprising the use of a δέη or two-section burner having at least one liquid or gas conduit or group of conduits to provide first passage or passages for liquid or gas, and at least one bonded radially spaced second conduit for liquid or gas surrounding said first conduit or group of conduits for liquid or gas about at least one annular second passage for providing a liquid or gas therebetween and comprising a central or central and annular exit port 8202327; - 3 - has one end of the burner, and a change from one reactant feedstream to another without stopping the system or releasing the pressure, which method comprises the combination of the steps of: 5 (1) letting go a first reactant stream of first slurry of solid carbonaceous fuel or hydrocarbon fuel with or without mixing with a teraperature moderator through at least 6dn of said first or second passages for liquid or gas 10 (2) simultaneously passing a separate reactant stream of free oxygen-containing gas with or without mixing with a temperature moderating gas through the unused passageway or passageways in said burner associated with a passageway through which said first reactant stream flows into (1)? (3) mixing said reactant streams of (1) and (2) together to produce a well-distributed mixture, and reacting said mixture by partial oxidation in the reaction zone of said gas generator at an autogenous temperature in the range of about 1182-1926 ° C, a pressure in the range of about 1 to 300 atmospheres, an atomic ratio of oxygen / carbon in the range of about 0.5-1.7, and a weight ratio of H 2 O / fuel in the range of About 0-5.0; (4) the out-of-phase passage of the passage or passages for liquid or gas in which in said burner said stream of first slurry of solid carbonaceous fuel or hydrocarbon fuel with or without mixture with a temperature moderator, which out-of-phase application is effected with a uniform decreasing flow rate ranging from maximum to 0 over a period of time in the range of about 1-3600 seconds; and simultaneously phasing said stream of second slurry of solid carbonaceous fuel or hydrocarbon fuel with "or without mixture with temperature moderator in the same gas or liquid / **% passage in said burner at a uniformly increasing flow rate ranging from 0 to maximum speed over the same time period, and mixing the phase-in flow with the remaining part of said first slurry stream 8202327 4 {-4- 'or hydrocarbon fuel with or without mixture with a temperature moderator flowing therein; and (5) setting the flow rate of the reaction-5 component stream of free oxygen-containing gas with or without mixture with a temperature moderator passing through the burner and initiating if necessary additional H 2 O in the reaction zone, for setting the free oxygen / carbon atom ratio and the I / O / bran weight ratio substance in the reaction zone to design conditions for the reaction for partial oxidation.

Manual or automatic control means are included for switching and controlling the (fuel, oxidant and steam flows. By these means the main and reserve fuels can be switched and the straw-free oxygen-containing gas and / or temperature moderator can be used. controlled up or down to maintain the yield of the gasifier while maintaining efficiency and stability.

To illustrate the invention in more detail, reference is made to various embodiments shown in the figures of the drawing, in which: figure 1 is a schematic representation of an embodiment of the invention showing control means for replacement of a fuel by another while maintaining continuous operation? Figs. 2 and 3 are vertical longitudinal schematic representations of two preferred burners for use in the present process; Fig. 4 is a schematic representation of another embodiment of the invention. and FIG. 5 is a vertical, longitudinal schematic representation of a two-section burner suitable for the present process.

The present invention relates to a continuous process for the preparation of gas mixtures comprising -: H2, CO, CO2, carbon particles and at least. a material selected from the group consisting of H 2 O, N 2, Ar, CH 4, H 2 S, COS, and ash, such as synthesis gas, fuel gas, and reducing gas, through 8202327 -T * - 5 - the partial oxidation of a reactant stream of fuel which is then replaced by a different one. fuel reactant stream without shutdown of the gas generator or release of the pressure from the gas generator.

5 Furthermore, there can be virtually no change in the amount of gas produced. This multi-fuel process is not limited to a special fuel. Problems of fuel availability are reduced. The two reactant fuel streams can be selected from the group consisting of a pumpable slurry of solid carbonaceous fuel in a liquid carrier, liquid or gaseous hydrocarbon fuel, and mixtures thereof with or without mixing with a temperature moderator. The fuels are reacted by partial oxidation with a reactant stream of free oxygen containing gas with or without mixing with a temperature moderator. The product gas mixture is prepared in the reaction zone of a non-catalytic refractory lined gas generator for partial free-flow oxidation, as described in co-assigned 20 Ti. Patent 2,809,104 issued to Dale M. Strasser et al. at a temperature in the range of about 1182-1926 ° C and a pressure in the range of about 1-300 atmospheres, such as about 5-250 atmospheres / e.g. about 10 -100 atmosphere.

During the operation of the partial oxidation gas generator, it may be necessary to switch from one fuel to another without changing the burner and without sacrificing stable operation and efficiency. Changing the burner requires a costly shutdown period with delay as a result. Furthermore, the burner must be able to operate with a variety of the liquid / solid and gaseous fuels, and mixtures thereof. Unstable combustion and poor efficiency may be the main concern when using certain known burners 3E for gasifying liquid iase suspensions of solid carbonaceous fuels. Furthermore, feed streams may be poorly mixed and solid fuel particles may pass through the gasifier without coming into contact with large amounts of oxygen. Unreacted oxygen in the reaction zone may be 8202327.

then react with the product gas.

A new burner that can be used in the present method is shown in Figure 2 of the drawing and includes: a retracted central conduit coaxial with the central longitudinal axis of the burner and with an upstream inlet allowing a first feed stream to be separately - can be led, and a downstream discharge outlet; an outer coaxial conduit concentric to said central conduit and having an upstream inlet through which a second feed stream can be separately introduced, and a converging at least partially frusto-conical outlet nozzle connecting said outer conduit at the downstream end of the burner ends? wherein (said central conduit with the downstream exhaust outlet is withdrawn upstream from the downstream face of the burner by a distance of two or more times, eg 3-10 times, the minimum diameter of said downstream outlet nozzle of the outer conduit to provide a premix zone, and means for radially spacing said central and outer conduits to provide a coaxial annular passage allowing said second feed stream to separate simultaneously with said first feed stream in said premixing zone where a multiphase-25 mixture is formed before it is discharged through said outer conduit outlet nozzle.

I

Another new burner that can be used in the present method is indicated in Figure 3 of the drawing and includes: a central conduit coaxial with the central longitudinal axis of the burner and with an upstream inlet through which a first feed stream can be introduced and a circular downstream discharge outlet, and said central conduit discharge outlet is withdrawn upstream from the downstream face of the burner by a distance of 3-10 times the minimum diameter of a downstream outlet nozzle of an outer conduit further will be described to provide a pre-mixing zone comprising 2-5 cylindrically formed pre-mixing chambers serie in series and coaxial with the central longitudinal axis of the burner genoemde 8202327 / 4-7. intermediate coaxial conduit concentric with said central conduit and with an upstream inlet through which a second feed stream is introduced. and a converging, at least partially cone-shaped, downstream outlet nozzle terminating said intermediate conduit, and the end of said intermediate conduit exit nozzle is withdrawn upstream from the downstream face of the burner at a distance of 1-5 times the minimum diameter 10 of said downstream outlet pipe of the outer pipe? an outer coaxial conduit concentric to said central and intermediate conduits and with an upstream inlet. whereby a third feed stream (can be introduced) and a converging at least partially frusto-conical shaped downstream outlet nozzle terminating said intermediate conduit, and the end of said intermediate conduit outlet nozzle is withdrawn upstream from the downstream face of the burner a distance of 1-5 times the minimum diameter of said downstream outflow nozzle of the outer pipe; an outer coaxial pipe concentric to said central and intermediate pipes and with an upstream inlet through which a third feed stream can be introduced, and a converging downstream outlet nozzle terminating said outer conduit and comprising a frusto-conical shaped rear portion and a straight cylindrical shaped advantage at the downstream end of the burner, and means for radially spacing the means the central, intermediate, and outer conduits to form intermediate and outer coaxial annular passages, and said intermediate annular passage is between> the outer diameter of the central conduit and the inner diameter of the intermediate conduit and the passage making said 35 second feed stream can pass separately at the same time as said first feed stream in a premix zone where a multiphase mixture of said first and second feed streams is formed, and said outer annular passageway is located between the outer diameter of the 8202327 - ι - 8 - said intermediate conduit and the inner diameter of said outer conduit and is the passage through which said third feed stream can pass separately simultaneously with said first and second feed streams and then mix with said multiphase mixture of said first and second feed streams doctor relative to the downstream face of the burner. Optionally, the walls of said intermediate conduit may include a plurality of cavities or passages in a plurality of circumferential rings along its length to enable at least a portion of said third feed stream flowing into said outer annular conduit suggest by passing and mixing with 6έη or more of the other materials flowing simultaneously - with a lower pressure through the other passages or premixing zone of the burner. Optionally, blocking agents may be applied at the downstream outlet of the said outer annular passage for complete or partial closure of the downstream outlet of said outer annular passage The blocking means may comprise an annular plate disposed perpendicular to the central longitudinal axis of the burner with or without a plurality of cavities of small diameter The said third feed current may be a temperature moderator n selected from the group consisting of K ^ O, CO ^ f and mixtures thereof. Also, a portion of cooled and purified product recycled in the process or a stream of free oxygen-containing gas may comprise the third feed stream.

Thus, in this embodiment of the burner, as shown in FIG. 3, a large number of high pressure, high speed turbulent streams of said third feed stream may pass through the walls of the intermediate conduit and into the annular passage and premixing chambers. in different places along their length. By these means, atomization of the fuel feed stream and, optionally, mixing with the oxidant stream can be facilitated. For example, the third feed stream may pass through a plurality of small diameter passages or cavities, i.e., 0.32 - 0.50 diameter, leading into said annular passage and premixing chambers.

8202327 i χ · - 9 -

In other embodiments, an annular type burner as shown and described in U.S. Pat. patent 3,874,592 used. Furthermore, the central and / or annular conduits can comprise a large number of parallel or curved linear tubes.

Straightening pins, fins, centering blades, spacers and other conventional means are used to keep the burner lines spaced symmetrically from one another and to keep them in stable centering without impeding the free flow of the feed streams in the power plant conduit and annular passages.

The outlet nozzle of the outer and / or intermediate conduit may include a frusto-conical rear portion (with a converging angle in the range of about 15 ° - 90 ° from the burner central longitudinal axis. The rear portion may develop into a normal cylindrical advantage that ends at the downstream surface of the burner. The cylindrical advantage may have a height in the range of about 0-1.5 times its own diameter. In one embodiment, the exit nozzle of the outer conduit is in the form of or was developed by an American Society of Mechanical Engineer's standard long-radius nozzle. A further description of this nozzle can be found in "Thermodynamics Fluid Flow and Heat Transmission" by Huber 25 0. Croft, page 155, first edition, 1938 McGraw-Hill Book Company.

The burner can be cooled externally by means of cooling hoses that surround the burner outer vessel along its length. The downstream end of the burner 30 may include a pierced outer sheet through which a coolant is circulated. For example, an annular cooling chamber can surround the downstream outlet nozzle of the outer conduit. The cooling chamber and the outer nozzle of the outer conduit may form a single piece of heat resistant and wear resistant material such as tungsten carbide or silicon carbide. Any suitable coolant can be used, for example water. Preferably, the downstream end of the central conduit can be retracted

S

$ are upstream of the entrance to the first premix chamber

a

·· · ----- 8202327 i r - 10 - in the line. Preferably, the replacement of the end of the central conduit with respect to the entrance of the first premix chamber can be in the range of about 0.1-2.0 times the diameter of the first premix chamber.

In one embodiment, each of the premixing chambers in the central conduit except the first are cylindrical shaped and comprise a coaxial cylindrical body portion formed by a coaxial at least partially converging outlet portion. The first cylindrically shaped premix chamber in the central conduit comprises a normal coaxial cylindrical body portion that directly discharges into the next in-line coaxial cylindrical premix chamber. The converging outlet parts of said premixing chambers may be made of tungsten carbide or silicon carbide for increased wear resistance.

The size ratio between successive premixing chambers in the present burners can be expressed in the following way: for burners in which the premixing chambers in the central pipe are consecutively numbered 1 to 5, the diameter ratio of each one of the aforementioned central chambers to the diameter of the next central chamber in the line i.e. 0 ^ 02? D2: D3? D ^ iD ^; or D4: Dg in the range of about 0.2-1.2. The ratio of the length of a central pre-mixing chamber in said central conduit to the length of the next central pre-mixing chamber in the conduit, ie. 1 ^ :? L3: L4; or can be in the range of about 0.1-1.0.

In operation of the embodiment of the burner using premixing chambers, flow control means 30 may be used to control the flow of the feed streams to the passageways in the burner in the same manner as described above. The feed streams entering the burner and colliding simultaneously and simultaneously at different speeds collide and mix with each other in the first premix chambers. The collision of a reactant stream, such as the liquid slurry of solid carbonaceous fuel in a liquid medium, optionally mixed with a temperature moderator, with another reactant stream, such as a gaseous free-oxygen stream. 8202327 * fr-11 gas, optionally mixed with a temperature moderator of a higher rate, disintegrates the liquid suspension into a fine sprayed liquid. The multiphase mixture then formed then passes through remaining pre-mixing chambers where additional mixing takes place. When the mixture passes freely through the burner according to the invention without obstructions, its speed changes many times. For example, at different points in the burner, the speed of the mixture can vary from about 20-600 ft. per sec. As the mixture flows from one premix chamber to the next, the speed changes are mainly due to changes in flow path diameter and mixture temperature.

This promotes a thorough mixing of the components. By operating (v in the area of turbulent flow, the mixing can be maximized. Furthermore, direct heat transfer between the materials takes place within the burner. From 0-100 vol.%, For example about 5-25 vol.% Of the liquids in the feed streams can be evaporated before the feed streams leave the burner By means of converging outlet nozzles, the feed streams can be directly accelerated in the reaction zone of the gasifier by partial oxidation.

Burning of the combustible materials as they pass through the pre-mixing zone of the burner can be prevented by discharging the multiphase mixtures at the outlet nozzle of the outer pipe at the end of the burner at a discharge rate greater than the rate of propagation of the flame. Flame rates are a function of factors such as mixture composition, temperature and pressure and can be calculated by conventional methods or determined experimentally. Advantageously, with the aid of the present burner, the exothermic partial oxidation reactions take place at a sufficient distance downstream of the burner bulge face to protect the burner from thermal damage.

Depending on factors such as the temperature, speed, residence time and composition of the feed flows; γ the desired degree of evaporation of liquid carrier; the temperature and amount of return gases in the generator; · * .....- -—.....

82 02 3 2 7 ΐ i - 12 - βη the desired life of the burner; cooling hoses may or may not surround the outer surface of the burner along its length. For such reasons, the burner may or may not have an annular cooling chamber at the downstream end.

Liquid hydrocarbon fuels and / or pumpable suspensions of solid carbonaceous fuels with a dry solids content in the range of about 30-75 wt%, for example about 40-70 wt%, may pass through the inlet passage of the burner of the invention be fed. For example, fuel streams, whether or not mixed with the temperature rotaryator, i.e., H 2 O, may be passed through the center conduit or through the annular f 'passages. The inlet temperature of the liquid hydrocarbon or the slurry is in the range of approximately about 260 ° C, but preferably below the evaporation temperature of the liquid hydrocarbon at the given inlet pressure in the range of about 1-300 atmospheres, such as 5 -250 atmospheres, preferably about 10-100 atmospheres. At the same time, free oxygen-containing gas, whether or not mixed with the temperature moderator, is fed into the burner through the corresponding unoccupied passage.

Thus, if the main or first fuel flowing through a central pipe of the burner or through the coaxial annular passage of the burner becomes unavailable and it is desired to switch to a reserve or second fuel, or for some reason it is desirable to switch from a first slurry of solid carbonaceous fuel or hydrocarbon fuel to a second solid slurry of carbonaceous fuel or hydrocarbon fuel without shutting down the system or releasing the pressure, as follows: proceed: (1) separately determining the flow rates of four feed streams 1-4 consisting of steam, reserve fuel, main fuel, and free oxygen-containing gas, respectively, and providing signals s, m, a, and b corresponding respectively to the actual flow rates of the supply currents 1-4 to a control unit; (2) comparing said actual current - 8202327 _ * κ% - 13 - with velocity signals s, m, a, and b respectively manually or automatically calculated and input inputs that are the desired flow rate or determined point for that moment before each of the four supply currents, and providing a corresponding control signal to a flow rate controller for controlling the flow rate of each of the supply currents 1-4 in accordance with the respective determined point of each; (3) supplying a feed stream of said main fuel into the reaction zone of a gas generator for free-flowing non-catalytic partial oxidation, by means of a burner comprising a central conduit radially spaced from a concentric coaxial outer conduit having a downstream outlet nozzle and providing a coaxial annular passage therebetween and wherein said main fuel feed stream is passed through the central conduit of the burner or through the coaxial annular passage; (4) simultaneously conducting a separate feed -20 flow of a free oxygen-containing gas, whether or not mixed with a separate steam feed stream through the unoccupied fluid passage in said burner; (5) mixing the said reactant streams from (3) and (4) to prepare a well-distributed mixture, and react these mixtures by partial oxidation in the reaction zone of said gas generator at an autogenous temperature in the range of about 1182-1926 ° C, a pressure in the range of about 1-300 atmospheres, an atomic ratio of oxygen / carbon in the range of about 30 spring 0.5-1.7, and a weight ratio of O 2 / fuel in the range of about 0-5.0, such as about 0.1-3.0; (6) replacing in said central conduit or annular passage of said main fuel feed stream with a replacement feed fuel of reserve fuel by dephasing the fluid passage in which said main fuel stream comprising the first suspension of solid carbonaceous fuel or hydrocarbon fuel, which flows out of phase formation with a uniformly decreasing flow rate which is 8202327.

r14 - varies from maximum to 0 over a period of time in the range of about 1-3600 seconds; and at the same time. phase said backup fuel stream comprising second slurry of solid carbonaceous fuel or hydrocarbon fuel in the same fluid passage. a uniformly increasing flow rate ranging from 0 to maximum speed over the same period of time and mixing with the remainder of and replacing the phase-out portion of said stream of first slurry 10 of solid carbonaceous fuel or hydrocarbon fuel; and simultaneously with or after the termination of said substitution of feedstreams; and simultaneously with or following (6); v- (7) controlling the flow rate of the feed stream of free oxygen-containing gas passing through the burner, and if necessary introducing additional H 2 O into the reaction zone to control the atomic ratio of free oxygen. oxygen / carbon and the weight ratio of I / O / fuel in the reaction zone under the designed conditions in the partial oxidation reaction.

By the present process, the temperature in the reaction zone can be kept almost constant, ie a variation of less than + 37 ° C, and the weight ratio H 2 O / fuel can be maintained in the range of about 0.1- 3.0.

In the present flow control means, a manually or automatically controlled flow recorder with transmitter or transmitter is used to provide signals to a flow rate controller 30 located in each power line. For slurry fuel power lines, a signal from the flow recording control device is provided to a speed control for a positive displacement pump. For liquid and gaseous hydrocarbon fuel feed lines and for oxidant feed lines, the signal from the flow recording controller is supplied to a flow control valve. Responding to this signal or those signals, the speed of this pump or those pumps is changed, or alternatively the orifice in said flow control valve or valves is changed. By these means, 8202327, die - 15 - the flow rate for each fuel flow passing through the burner can be adjusted up or down depending on whether it is in or out of phase.

The rate of the reactant flow through the central conduit or annular passage is in the range of about 0.5-100, such as 10-50 feet per second, for example, 2-20 feet per second at the outer face of the burner when this reactant is> stream is a liquid hydrocarbon fuel or liquid suspension of solid carbonaceous fuel, or mixtures thereof, and in the range of about 85 feet per second to sonic speed, for example, 100-600 feet per second when this reactant stream is a gaseous hydrocarbon fuel or a free oxygen-containing gas, whether or not mixed with a temperature moderator or a temperature moderating gas. The rate of a reactant fuel flow or a reactant fuel mixture flow is greater than the flame propagation intensity for that fuel or fuel mixture.

The term solid carbonaceous fuels used herein to describe suitable solid carbonaceous feedstocks is intended to include various materials and mixtures thereof from the group consisting of coal, coke from coal, charcoal from coal, residues of the liquid making coal, petroleum coke, particulate carbon black, and solids derived from oil slate, tar sands, and pitch. All types of coal can be used including anthracite, bituminous coal, sub-bituminous coal, and lignite. The particulate carbon can be any. is as a by-product of the present partial oxidation process, or that obtained by burning fossil fuels. The tern solid carbonaceous fuel, by definition, also includes debris, dewatered sanitary sewage sludge, and semi-solid organics such as asphalt, rubber, and rubber-like materials, including rubber car tires that have been comminuted or pulverized to the appropriate particle size. Any suitable grinding system can be used to comminute the solid carbonaceous fuels or mixtures thereof to the desired size.

\ The solid carbonaceous fuels are preferably 8202327 - 16 - 1 1

finely crushed to a particle size so that 100% of the material is passed through an ASTM E 11-70 sieve standard designation 1.4. mm (alternative No. 14) and at least 80% passes through an ASTM

E 11-70 sieve stand designation 425 ^ m (alternative no. 40).

The moisture content of the solid carbonaceous fuel particles is in the range of about 0-40 wt%, such as 2-20 wt%.

The term liquid carrier, as used herein as the dispersant medium to prepare pumpable suspensions of solid carbonaceous fuels, is intended to include various materials from the group consisting of water, liquid hydrocarbon material, and mixtures thereof. However, water is the preferred carrier for the solid carbonaceous fuel particles. In one embodiment, the liquid carrier is liquid carbon dioxide. In such a case, the liquid suspension may contain 40-76 wt% solid carbonaceous fuel and the remainder is liquid CO2 The CC> 2 solid fuel suspension can be introduced into the burner at a temperature in the range of -55 ° C to 37 ° C depending on the pressure.

The term liquid hydrocarbon material as used herein to describe suitable liquid carriers and fuels is intended to include various liquid hydrocarbon materials, such as those selected from the group consisting of liquefied petroleum gas, petroleum distillates and residues, gasoline, naphtha, kerosene, crude petroleum, asphalt, gas oil, residual oil, tar sand oil and slate oil, coal derived oil, aromatic hydrocarbons (such as benzene, toluene, xylene fractions), coal tar, cyclic gas oil liquid catalytic cracking, furfural extract of coconut palm gas oil and mixtures thereof.

The term liquid hydrocarbon material as used herein to describe suitable liquid fuels is also intended to include various oxygen-containing liquid hydrocarbon organic materials, such as those selected from the group consisting of carbohydrates, cellulosic materials, aldehydes, organic acids, "alcohols, ketones, oxidized fuel oil, waste liquids and by-products of chemical processes for the preparation of oxygenated 8202327 * * - 17 - hydrocarbon organic materials, and mixtures thereof.

For example, in one embodiment, the feed streams comprise slurry of liquid hydrocarbon material and solid carbonaceous fuel. H20 in liquid phase · 5 can be mixed with the liquid hydrocarbon carrier, for example as an emulsion. A portion of the H 2 O, i.e. about 0-25 wt.% Of the total amount of H 2 O, can be introduced as steam mixed with the free oxygen-containing gas. The H 2 O / fuel weight ratio may range from about 0-5, for example about 0.1-3.

The designation gaseous hydrocarbon material as used herein to ora write suitable gaseous hydrocarbon fuels is intended to include a gaseous feedstock from the group consisting of ethane, propane, butane; pentane, methane, natural gas, coke overu gas, refinery. gas, acetylene waste gas, ether waste gas, and mixtures thereof.

Simultaneously with the fuel stream, a free oxygen-containing gas stream is supplied by means of a free passage or free passages in the burner. The free oxygen-containing gas may pass through the central and / or annular pipes at a temperature in the range of approximately about 815 ° C, and preferably ≤ Q * in the range of approximately in the range of 113 C, for oxygen enriched air, and about 260 ° C to 650 ° C for air, and a pressure in the range of above about 1 - 300 atmospheres, such as 5-250 atmospheres, for example, 10-100 atmospheres atmosphere. The atoms of free oxygen plus atoms of organically bound oxygen in the solid carbonaceous fuel per 30 atomic carbon in the solid carbonaceous fuel (O / C atomic ratio) may range from 0.5-1.95. With free oxygen-containing gas in the reaction zone, the wide range of said O / C atomic ratio can be about 0.5-1.7 *, such as about 0.7-1.4. More specifically, with air to the reaction zone, said O / C atomic ratio may be about 0.7-1.6, such as about 0.9-1.4.

The designation free oxygen-containing gas, as used herein, is intended to include air, oxygen-enriched air, that is, more than 21 mole percent oxygen, and substantially * 8202327 l-ia - pure oxygen, that is, more than 95 mole % oxygen, (the rest includes N2 and noble gases).

. The free oxygen-containing gas can be supplied, whether or not mixed with a temperature-moderating gas. The 5 designation temperature-moderator or temperature moderating gas. as used herein, is intended by definition to include a representative of the group consisting of H 2 O, CO 2, N 2, a process-recycled portion of the cooled and purified exhaust gas stream from the gas generator, and mixtures thereof. When additional steam is used as a temperature moderator, the entire amount of steam can be supplied through a passageway. Alternatively, about 0-25% by volume of the steam may be mixed with the free-oxygen-containing gas stream and passed through a passageway, and the remainder of the steam may be passed through the remaining passageway.

The present single and multi-ring premix burners can be operated with the feed streams passing through alternative passages in the burner. Typical modes of operation are summarized in Tables I-III below.

Table I lists the materials fed into the gasifier through the burner and their corresponding symbol. The solid carbonaceous fuel 25 (B), water (C), and liquid hydrocarbon material (E) can be mixed together in different combinations upstream of the burner inlet to form a pumpable slurry that can be passed into the burner and then passed through one of the different free-flow passages of the burner as indicated in Table II for the single-annular premix burner (see Figures 1 and 2); and as shown in Table III for the double annular premix burner (see Fig. 3). For example, the first entry in Table II shows that a pumpable slurry stream comprising solid carbonaceous fuel (B) mixed with water (C) through the retracted center conduit 15 of a single annular premix burner, i.e., Figures 1 and 2, may while simultaneously passing a stream of free oxygen-containing gas through annular passage 17.

8202327 y 1 - 19-

Other embodiments of the present invention are possible in addition to those in Tables II and III. indicated.

With respect to the operation of an embodiment of the double ring burner shown in Fig. 3, the second entry of Table III 2ien allows free oxygen-containing gas (A) to pass through both annular passages.

In such a case, any member of the following group may be simultaneously passed through one or both annular passages 17, 10 and 51: air, oxygen enriched air, and substantially pure oxygen. Also, as shown in the seventh entry of Table III, five-oxygen-containing gas (A) can be mixed with steam (D) (for example, up to 25% by volume of the total amount of EQ) through the central conduit 15. and the remainder of the H 2 O as water (C) can be passed through the intermediate ring 17 as part of the liquid carrier for the suspension.

When the solid carbonaceous fuel suspension liquid carrier is a liquid hydrocarbon-20 material, premature combustion in the burner may be avoided by δδη or more of the following measures: (1) keeping the fuel below its own ignition temperature, k (2) incorporating water into the solid fuel slurry, (3) using air or oxygen enriched air, ie, up to about 40% by volume, (4) mixing steam with the air (5) the use of a double annular premix burner (Fig. 3) in which the end of the intermediate exhaust nozzle has a retraction of about 0 with respect to the surface of the burner. In such a case, the free oxygen-containing gas, such as substantially pure oxygen, can be passed separately through the outer annular passage of the burner and into the reaction zone of the gas generator where it reacts by partial oxidation with the multiphase mixture. discharged from the pre-mixing zone of the burner and (6) discharging the multiphase mixture at the exit nozzle at the end of the burner at a discharge rate greater than the flame propagation rate.

^ 8202327 I t - 20 -

TABLE I

Material Symbol

* Free oxygen-containing gas A.

Solid carbonaceous fuel B

5 Water C

Steam D

Liquid hydrocarbon material E

Temperature ^ -inoding gas F '

TABLE II

10 V66r Single Ring Mixer Burner (See Figures 1 & 2)

Central pipe 15 Annular passage 17

B + C A

(, B + C + E A

B + C A + D

15 A B + C

A * B + C + E

A + D B + E

TABLE III

Pre-burner burner with double ring (see figure 3) 20 Central pipe 15 Intermediate Outer ring _ ring 17_ 51_

A B + C A

B + C A A

B + C A F

25 A + B + C + E A

; A B + C + E A + D

D B + C + E A

A + D B + C + E A

B + C + E A A

30 B + C + E D A

B + C + E A D

A B + E A + D

A + D B + E A

A + D B + E A + D

35 D B + E A

A B + E D

B + E A + D A + D

B + E A A + D

B + E D A

40 B + E A D

A B + E F

F B + C A

A B + C F

E B + C A

45 B + C Ξ A

8202327.> ^ - 21 -

The burner casing of the invention is introduced downwardly through an inlet port at the top of a compact, unfilled, non-catalytic, free-flow synthesis gas generator lined with refractory material, for example, as shown in FIG. 1. The burner extends along the central longitudinal axis of the gas generator and the downstream end of the burner carries a multiphase mixture of fuel, free oxygen-containing gas, and a temperature moderator directly into the reaction zone. The relative proportions of solid or solid and liquid fuel, water and oxygen in the feed stream to the gas generator are carefully controlled to a large proportion of the carbon in the fuel, for example, up to about 90% by weight or more , convert to carbon oxides; and to maintain an autogenous reaction zone temperature in the range of about 1182-1926 ° C, preferably in the range of 1095-1540 ° C.

The residence time in the reaction zone is in the range of about 1-10 seconds, and preferably in the range of about 2-8 seconds. With near pure oxygen feed for the gas generator, the gas generator exhaust gas composition in mol% on a dry basis may be as follows: H2 10-60, CO 20-60, CO2 5-40, CH4 0.01-5, H2S + C0S 0-5, N2 0-5, and A 0-1.5. With air supply to the gas generator, the composition of the exhaust gas of the generator in mol% on a dry basis can be approximately as follows: H2 2-20, CO 5-35, CO2 5-25,: CH1 0 -2, H2S + COS 0-3, N2 45-80, and Ar 0.5-1.5. Unconverted carbon and ash are present in the exhaust gas stream.

The hot gaseous exhaust stream from the reaction zone of the synthesis gas generator is rapidly cooled below the reaction temperature to a temperature in the range of about 120-370 ° C by direct quenching in water, or by indirect heat exchange for example with water to produce steam in a gas cooler. The gas stream can be cleaned and purified by conventional methods.

A more complete understanding of the invention can be obtained by reference to the accompanying schematic drawing showing the present invention in detail. Although the drawing illustrates preferred embodiments of the invention, it is not intended to limit the invention to the disclosed special device or materials.

Referring to Figs. In the drawing, Fig. 1 is a schematic representation of an embodiment of the invention showing control means for the continuous operation of a synthesis gas generator while one fuel is out of phase and another in phase at the same time without the pressure of the gas generator. Furthermore, the control means can be used for rapid change of throughput levels above or below the flow path for which the burner shown is designed. By these means, adjustments can be made to control the amount of raw exhaust gas produced, and to provide for a change in demand for the product gas. Furthermore, another use of the control system is to maintain the desired composition of the product gas when it is possible to do so by adjusting the flow rates of € dn or more of the reactant flows. Thus, by the present flow control system, the flow rates for all of the reactant flows are controlled separately and independently so that the temperature and weight ratio of H 2 O to fuel in the reaction zone are maintained at designed conditions and within desired operating ranges for the fuel being reacted. If necessary, the atomic ratio of free oxygen to carbon in the fuel 25 in the reaction zone can also be adjusted within design conditions.

While the control system shown in Fig. 1 is particularly designed for the combination of feed supplies comprising a slurry of a solid carbon-containing fuel in a liquid hydrocarbon fuel, the system can be changed by simple changes in the means for changing of the flow rate of the fuel flow as described below. are used to control other combinations of solid carbonaceous fuel, liquid and gaseous hydrocarbon fuel suspensions. In Figure 1, burner 1 is mounted in a central flanged inlet 30 located in the top portion of a conventional refractory lined free-flow synthesis gas generator 41 along the central longitudinal axis. Reaction 8202327 - * Λ - 23 - component currents enter through the upstream end of brarlder 1, pass downward through it, and are discharged through downstream end 42. Burner 1 is designed to have the required system production for operation 5 steady state can be achieved or even surpassed by a certain amount when the flow rate through all passage & aximal. The control system can independently change the flow rate of or more of the supply currents in lines 18l, 161, 43 and 63. By these means, the temperature in the reaction zone 31 is maintained at the desired operating temperature. Furthermore, the weight ratio of H 2 O to fuel, and if necessary the atomic ratio of free oxygen to carbon in the fuel in the reaction zone, can be maintained at design conditions.

The operation of the method and the control system shown in Fig. I follows. For illustrative purposes, the main fuel may be, for example, a slurry of a solid carbonaceous fuel, ie coal-water or coal-oil suspension in line 43. The reserve fuel is a liquid hydrocarbon fuel, ie residual oil in line 161. Naturally, any liquid or gaseous hydrocarbon fuel can be chosen as the primary fuel.

In the present process, the remaining portions of the main liquid streams flowing from line 50 in line 14 are mixed with the reserve liquid stream introduced into line 167. H2 O may be mixed with the fuels in lines 161 and 43 or the free oxygen-containing gas in line 63. Also, as shown in Figure 1, at least a portion, i.e. 10-100 vol.% Of the H2 O as the temperature moderator are provided, eg steam. Thus, as shown in Fig. 1, steam in line 187 in line 18 can be mixed with the free oxygen-containing gas flowing in line 70. This scheme allows controlled amounts of steam to be introduced and mixed with the straw-free oxygen-containing gas and / or fuel upstream of the burner. Valves 183, 163, 77, and 65 can be operated manually or automatically to achieve a fully open position up to V a fully closed position. The sizes in which each valve can be opened or closed is also adjustable. The suspension feed stream in line 43 is pumped into the reaction zone 31 of synthesis gas generator 41 by means of positive displacement pump 45 provided with speed control 46, line 47, flow meter and converter 48, line 49, valve 77, 5 lines 50 and 14, and inlet 8 of burner 1. The flow rate of the slurry through line 43 is controlled by the speed of the positive displacement pump 45. To phase out the slurry flowing through line 43 speed continuously reduced from maximum to zero over a period in the range of about 1-3600 seconds, such as about 60-1800 seconds, for example about 300-1000 seconds. Flow recorder controller with transmitter 51 includes a microcomputer programmed with the desired time versus decreasing flow rate curve. The magnitude of the slurry flow in line 47 is measured and a signal a is supplied by flow transmitter 48 corresponding to the flow rate of the slurry in line 43. Flow recorder controller 51 receives. signal a, compares it with a signal representing the desired flow rate at that time, and provides a corresponding control signal to speed controller 46 to down-speed pump 45 so that the slurry charge flowing in line 49 has a given reduced flow rate records for that moment in the phase-out period. The new suspension rate is measured and the cycle is repeated. By these means, repeated flow rate adjustments are made and the slurry flowing in line 50 is dephased.

Simultaneously with the de-phaseing of the major slurry fuel flowing in line 43, the reserve liquid hydrocarbon fuel flowing in line 161 is phase-out during this same period. Flow recorder controller with transmitter 171 includes a microcomputer programmed with the desired time against increasing flow rate curve. The oil flow rate in line 161 is measured and a signal m is provided by flow transmitter 165 in accordance with the flow rate vj? oil in conduit 161. Flow recorder control member 171 receives signal m, compares it with a signal representing the desired flow rate at that moment, and provides a corresponding control signal to valve 163. wider to open so that the oil charge in line 166 assumes a given increased flow rate instantaneously in phase 5 period. The new oil speed is measured and the cycle is repeated. By these means, repeat controls for the flow rates of the main and reserve fuels can be made so that the oil flowing into line 167 can be fed into line 14 in an amount that compensates for the reduced amount of slurry of solid carbonaceous fuel which flows into line 50.

^ .v, during or after the period when the solid carbonaceous fuel slurry from line 43 is brought into phase 15 and the portion of the reserve liquid hydrocarbon fuel from line 161 is brought into phase, the weight ratio of H 2 O to fuel in the reaction zone are controlled at design conditions or kept constant, ie less than + 10% variation, by increasing or decreasing the flow rate of the temperature moderator. Accordingly, in the present example, an additional amount of H 2 O from an external source can be phase-out during this same period of time simultaneously with the phase out of the hydrocarbon slurry. Thus, in Figure 1, a portion of the steam in line 181 is passed through line 187 and introduced into line 18 where it mixes with the free oxygen-containing gas from line 70. Flow recorder controller with transducer 191 includes a microcomputer programmed with the desired time versus 30 incremental flow rate curve.

The velocity of the steam flow in line 181 is measured and a signal s is provided by flow transmitter 185 in accordance with the flow rate of the steam in line 181. Flow recorder controller 191 receives a signal s, compares it with a signal that the desired flow rate at that time and provides a matching control signal to valve 183 to open wider so that the steam charge in line 186 assumes a given increased flow% rate for that time in the period before in t *.

I 8202327

L

- 26 - bring phase. The new steam speed is measured and the cycle is repeated. By these means, repeated controls of the velocity of the steam flow are made and the steam flowing into line 187 is transferred into line 18 in an amount that will maintain the weight ratio of 1: 0 to fuel in the reaction zone at designed conditions, for example almost constantly. In another embodiment, the H 2 O / fuel weight ratio in the reaction zone is controlled up or down by controlling the steam rate as described above to obtain a desired temperature in the reaction zone and a desired product composition.

At the same time with or after de-phasing the main fuel, de-phasing the reserve fuel, and optionally with or without de-phasing the steam depending on the nature of the fuels, free oxygen-containing gas can be set up or down. By these means, the temperature in the reaction zone can be controlled to design conditions, or kept almost constant, ie less than + 95 ° C variation.

Thus, in the present example in Figure 1, a portion of the free oxygen-containing gas in line 63 is passed through line 70 and introduced into line 18 where it mixes with the steam, if present, from line 187 as above described. Flow controller 74 is programmed with the desired time versus flow rate curve. The control period is the same as for the fuel and steam flows.

The control at the oxygen flow rate can be up or down depending on the nature of the fuel flows and the addition of steam, if at all. In the present example, the oxygen rate will be increased to meet the additional requirements for the partial oxidation of a liquid hydrocarbon compared to a solid carbonaceous fuel.

The velocity of free oxygen-containing gas in line -63 is measured and a signal b is provided by flow fA transducer 67 corresponding to the flow rate of free flow. '

TV oxygen containing gas in line 63. Flow recorder controller with transmitter 74 includes a microcomputer which receives a signal, compares it with a signal representing a desired flow rate for that time, and provides a corresponding control signal to valve 65 to open wider so that the charge of free oxygen-containing gas in line 68 assumes a given increased flow rate at that moment in the phase-in phase. The new rate of the free oxygen-containing gas is measured and the cycle is repeated. By these means, repeated adjustments of the rate of oxygen flow are made, and the free-oxygen-containing gas flowing into line 70 is introduced into line 18 in an amount that will maintain the temperature in the reaction zone at design conditions or substantially constant. In an embodiment in which the burner shown in Fig. 3 is used, part of the temperature moderator, for example steam in conduit 187, is introduced through the inlet 13 of the burner.

In another embodiment, the rate of the free oxygen-containing gas is controlled up and down to obtain a desired temperature in the reaction zone and a desired composition of the product gas. Alternatively, by the means described above, the oxygen to carbon atomic ratio in the reaction zone can be controlled at design conditions, i.e., in the range of about 0.5-1.7.

The aforementioned time versus flow rate curves for programming conventional flow recorder controllers 191, 171, 51, and 74 can be determined by conventional calculations based on system-wide heat and weight balances.

In another embodiment, the parameters for said calculations and others can be measured by conventional detectors and the responsive signals can be added to a general control system 40.

The input to control system 40 may be manually controlled or may be a signal from a computer, analyzer, or sensor. Controller 40 includes conventional circuits and components for providing or converting signals, i.e. pneumatically or electronically, to operate said speed controls and valves.

8 8202327 i t • - 28 -

In controller 40, the computer-computed values or the manually input determined points for the desired flow rates at specific times for the different flows are compared with the signals 5 a, m, s and b, respectively. For example, responding to signal a, controller 40 can automatically control pump speed controller 46 by transmitting signal power recorder controller 51. Also, signal c can be directly applied to speed controller 46. In another embodiment, for example, 1 · '> Image stream recorder regulator 51 receives a signal from current transducer 48 and signal c from controller 40 and the speed control signal for operation. calculate speed controller 46. In yet another embodiment, the flow of the feed stream can be stopped by a signal i from controller 40 to valve 77.

In such a manner, responding to signal controller 40, can automatically control liquid hydrocarbon fuel valve 163 by sending signal b to flow recorder controller 191.

Likewise, in such a manner, in response to signal b, controller 40 can automatically control free oxygen-containing gas valve 65 by sending signal j to flow recorder controller 74.

«

Two suitable burners to be used in the present method and control system are shown in. Figs. 1-3. Corresponding parts of the burner shown in Figures 1 and 2 have the same reference number.

Burner 1 is shown in great detail in Figure 2 and comprises substantially an unobstructed inner coaxial retracted central conduit 15 and an outer concentric coaxial conduit 16 longitudinally disposed about inner central conduit 15. Disc-shaped flange 10 is attached to the outer surface of the outer coaxial conduit 16 and supports burner 1 in a vertical longitudinal direction. The central longitudinal axes of burner 1 and gasifier 41 are coaxial. Spacers 18 provide an annular passage 17 with free flow between the outer diameter of central cylindrical conduit 15 and the inner diameter of outer cylindrical conduit 16. The exit opening at the downstream end of the 8202327-29 *. central conduit 15 is preferably straight, circular in cross section, and perpendicular to the X-axis of the burner. Outlet opening 20 can also be convergent or divergent. Outer conduit 16 terminates at 5 at the downstream end of the burner with a converging nozzle 21. A vertical cross-section of outlet nozzle 21 may be frusto-conical in shape or not. a straight cylinder can go up. Preferably, as indicated in Fig. 2, wear resistance nozzle 21 comprises a frusto-conical rear portion 22 which develops into a straight cylindrical advantage 23 terminating at the downstream outer surface 6 of the burner. The cylindrical blank will allow: (1) additional burner life due to a larger surface area available for wear, and (2) the manufacture of a ceramic or refractory insert or an entire cooling chamber of a thermal and abrasion resistant material i.e. tungsten or silicon carbide to prevent damage and to extend the life of the burner.

The height of the front cylindrical portion 23 of the exhaust nozzle 21 is in the range of about 0-1.5, for example 0.1-1.0 times, its own diameter ie the minimum diameter of converging nozzle 21. The diameter of exit port 20 of central conduit 15 is in the range of about 0.2-1.5, for example, 0.5-0.8 times the minimum diameter. of converging nozzle 21.

The downstream end of the burner may or may not be cooled. Preferably, as shown in Fig. 2, coaxial annular cooling chamber 2 exit opening at the burner end. By passing water through the pierced part 24 of cooling chamber 2, the end of burner 1 can be prevented from overheating. Optionally, for such reasons, outer conduit 16 can be kept cool by passing water through windings surrounding the outer surface 35 of outer conduit 16 along its length. Suitable converging angles for opening 21 are in the range of about 15 ° to 90 ° from the central longitudinal axis of the burner. The downstream end of outlet port 20 of central conduit 15 is withdrawn substantially upstream 8202327 if r - 30 - from outer surface 6 of burner 1 by a distance of two or more times the minimum diameter of converging outlet nozzle. 21. For example, the replacement of end 20 of central conduit 15 from burner surface 6 can be in the range of about 3-10 times the minimum diameter of converging outlet nozzle 21. The space between end 20 of central conduit 15 and burner surface 16 forms the unobstructed pre-mixing zone.

In the operation of burner 1, the reactant stream, see Table II above, can enter burner 1 through inlet 9 of Fig. 1 and pass directly from the upstream portion down through free-flow line 15, through outlet port 20 and into mixing zone 25, as shown in fig. 2. ζρ Cover plate 11 closes off the upper end of annular passage 1.7. Upstream inlet end 9 of central conduit 15 is coupled to a power line and the downstream end passes through cover plate 11 and is connected thereto. At the same time, the other reactant stream burner 1 may enter through inlet 8 and pass directly upstream portion 30 of outer conduit 16 downward through free-flow annular passage 17 and into premix zone 25 where intimate mixing of the two reactant streams occurs . Inlet 8 may or may not be tangential to outer conduit 16. Furthermore, direct heat exchange takes place between the two reactant streams in the premix zone 25. The temperature in the premix zone is controlled 1.7, so that a controlled amount of the liquid carrier can be evaporated without combustion, ie from 0-100 vol.%, for example, about 2-80 vol.%. Temperature control in the premix zone can be performed by controlling factors such as residence time and heat content of the incoming streams, and amount of external cooling such as through hoses 4, if any. Pre-mixing zone 25 is virtually free from any impediment to the free flow of the materials passing therethrough.

35 In in Figs. 1 and 2, streams of different materials flowing down through coaxially retracted central conduit 15 and simultaneously down through annular passage 17 are successively mixed together in tandem pre-mixing chambers 25 and 40 '. While the pre-8202327> Λ - 31 - mixing zone is indicated as containing in this embodiment. two separate coaxial pre-mixing chambers 25 and 40 'in series, the pre-mixing zone for other embodiments of the present invention may actually comprise one or more, such as 2-5 coaxial pre-mixing chambers. For example, three premixing chambers 25, 40 ', and 41 are provided in the embodiment of the burner shown in Figure 3. Each premix chamber in Figs. I, 2 and 3, except for the first chamber in the 11jn, includes a coaxial cylindrical body portion 45 followed by a coaxial 10 at least partially converging outlet portion 22 or 46 in Fig. 3 which may be develop into a straight cylindrical part 23 or 49, respectively. Optionally, such outlets can be made from a heat and abrasion resistant material, ie, silicon or tungsten carbide, as described above. In the multiple premixing chamber embodiments, the first premixing chamber may have in-line a straight coaxial cylindrical body portion 47 which discharges through a circular opening 39 directly into the next aligned coaxial premixing chamber 40 '. Preferably, the mixture leaving a pre-mixing chamber expands into the next successive pre-mixing chamber. When the mixture is accelerated and expanded through a final exit nozzle at the exit of the burner into the combustion chamber, this results in a more stable and efficient combustion pattern. The temperature, pressure and velocity ranges for the material flows passing through the different passages of the burner are essentially the same as those discussed above. The inlet to the first premix chamber 25 may have a converging inlet 48 as shown in Figs. 1, 2 and 3.

FIG. 3 is a vertical sectional view of an embodiment of the retracted central passage 15 premix burner similar to burner 1, as shown in FIG. 2, but modified to provide two coaxial annular passages ie intermediate annular passage 17 and outer annular passage 17. passage 51. Furthermore, the pre-mixing zone comprises three consecutive coaxial pre-mixing chambers 25, 40 'and 41 for free flow. Spacers 18 allow concentric V coaxial outer conduit 52, retracted coaxial intermediate conduit 53, and retracted coaxial central conduit 8202327 to be radially separated to provide said individual annular passages and premix chambers with virtually no hindrance to the free flow of materials. The downstream end 20 of central conduit 15 is retracted upstream from the outer surface 6 of the burner by a distance in the range of two or more, for example, 3-10 times the minimum diameter of the converging outlet port 21. The downstream end 54 of intermediate conduit 53 is withdrawn upstream from outer surface 6 of the burner by a distance in the range of 0-12, for example, 1-5 times the minimum diameter of converging outlet port 21.

Central line 15 and ring-shaped. Passages 17 and 51 of the burner in Fig. 3 are connected upstream and 15 respectively to separate inlets in a manner similar to that shown in Fig. 2. Thus, the upstream inlet end 9 of inlet tube 9 of central conduit 15 is coupled to a power line and the downstream end passes through cover plate 12 and is sealed thereto. Cover plate 12 covers the top-20 end of annular passages 51 and 17. At the same time, the other feed streams may enter burner 1 through upstream inlet 8 leading into annular passage 17, and upstream inlet 13 entering annular passage 51 leads. Optionally, an annular disc 56, with 25 or without several small diameter cavities 57, can occlude the downstream end of annular passage 51.

; 1

Inlets 8 and 13 may or may not be tangential to coaxial intermediate pipe 53 and outer pipe & pipe 52, respectively * The burner end may be cooled by passing water through the cavity portion 24 of annular cooling chamber 2 which is coaxial with the central longitudinal axis of the burner at the downstream end as shown. Alternatively, cooling chamber 2 can be omitted. Cooling hoses 4 can surround the burner along its length.

In the operation of the burner embodiment shown in FIG. 3, the feed currents which will pass down at the same time and at different rates will collide% through center conduit 15 and intermediate annular passage \ \ 8202327 + * -33-17. and mixing with each other in the first mixing chamber 25. The collision of a reactant stream, such as the liquid suspension of solid carbonaceous fuel in a liquid medium, with another reactant stream, such as a gaseous stream of a free oxygen-containing gas, steam, or temperature moderator at a higher rate causes the liquid suspension to decompose into a fine atomized liquid. The multiphase mixture then enters the second pre-mixing chamber 40 'for additional mixing. After leaving chamber 40 'through convergent outlet nozzle 46 and circular opening 54 at the downstream end of chamber 40', the multiphase mixture enters the third premix chamber 41. The third feed stream enters the burner upstream in through a separate inlet 13, and 15 goes down through annular passage 51. Optionally, at least a portion of the third feed stream in annular passage 51 can be mixed with the other feed streams in annular passage 17 and premix chamber 25, 40 ', and 41 by passing through several rings of small diameter passages or cavities 60, 61, 62 and 57 located in the wall. of intermediate pipe 53 and annular disc 56. When the reset of opening 54 at the end of intermediate pipe 53 of outer surface 6 of the burner is greater than zero, for example, in the range of about 1.0-5 ra 25, the minimum diameter of outlet opening 21, then the third feed stream can mix with the first and second feed streams in premix chamber 41 to prepare a multiphase mixture. Furthermore, in such an embodiment, there may be two or more, for example, 2-5 cylindrical coaxial premix chambers 30 in series. The multiphase mixture passes through convergent nozzle 21 at the downstream end of the burner into the reaction zone of the gas generator.

In the embodiment of the burner shown in FIG. 3 ', with a reset of about 54 zero opening 54, the third feed stream passing through the outer annular passage 51 will contact and mix with the multiphase. mixture of the other two feed streams from the premix zone downstream of the burner surface 6%, for example about 1-24 inches. Furthermore, in such an embodiment, there may be one or more, for example 2-5 cylindrical, coaxial premix chambers in series. For example, the red free oxygen-containing gas can be passed through central conduit 15 or intermediate passage 17 and the fuel feed stream can be passed through the other passage, i.e. the central conduit or intermediate passage which is free. At the same time, a flow temperature moderator can be passed through the outer annular passage 51.

10 Reference will now be made to Figs. 4 and 5 of the drawings.

During the operation of the gas generator by partial oxidation, it may be necessary to rapidly reduce the effluent production to about 1/8 to 3/4 of the factory firing.

throwing production, without replacing the burner. Changeover of the burner requires a costly shutdown period with consequent delay. In combined cycle development for energy development, a durable burner is required that has minimum pressure drop ^ and allows swap levels to be swapped quickly - up and down ^ -20 without sacrificing stable operation and efficiency.

Furthermore, the burner must be able to operate with a variety of liquid, solid, and gaseous fuels, and mixtures thereof. Combustion instability and poor efficiency can occur when using burners of the known type for gasification of liquid phase slurries of solid carbonaceous fuels. Furthermore, feed streams may be poorly mixed and solid fuel particles may pass through the gasifier without coming into contact with sufficient amounts of oxygen. Unreacted oxygen in the reaction zone can then react with the product gas.

These and other problems are avoided by a new two-section burner used in the present method> and comprising: a central conduit, which central conduit is closed at the upstream end and has a downstream circular outlet at the outlet end of the burner; an outer conduit .----, which is coaxial and concentric with said central conduit i ΐ ¥ ·. and forms an annular passage therebetween, the outer conduit and annular passage being closed at the upstream end and having a downstream annular outlet at the end of the burner; a central bundle of parallel or helical tubes with open ends 5 passing through the closed end of said central conduit and a gastight. forming a seal therewith; means for supporting said central bundle of parallel or helical tubes such that the outer surfaces of said central bundle of parallel or helical tubes form several passages within said central conduit; upstream inlet means comprising a manifold for splitting and introducing a first reaction component feed stream into the upstream ends of said central bundle of parallel or helical tubes; and wherein the downstream ends through which said first feed stream is withdrawn upward from the burner a distance of 0-12, for example 3-10 times, the minimum diameter of the central conduit outlet at the burner end; upstream inlet means for introducing a second reactant feedstock steam into said central conduit and down through said several passages within said central conduit; an annular bundle of equal or helical open-ended tubes passing through the closed end of said annular passage to form a gas-tight seal therewith so that the outer surface is covered.

planes of said annular bundle of parallel or helical tubes form several passages within said annular passage; upstream inlet means 30 comprising a manifold for splitting and introducing a third reactant feedstream into the upstream end of said annular bundle of parallel screw-down tubular tubes, and into which the upstream tube ends through which said third reactant feedstream 35 is discharged, upstream of the burner outer surfaces are retracted by a distance of 0-12, for example, 3-10 times the minimum width of the annular outlet nozzle at the end of the burner; means for supporting said annular bundle of parallel or screw 8202327 (36) linear tubes with respect to the inner wall of said annular dc channel and to each other such that the outer surfaces of said parallel or screw bundle linear tubes provide several passages within said annular passage; and upstream inlet means for introducing a fourth reactant feed stream into said annular passage and downwardly through said several passages within said annular passage, advantageously By means of the present burner, three series of flows can be obtained through the burner using either one or both groups of pipes and their surrounding lines Production levels can be changed quickly - up and down - without sacrificing stable operation.

In an embodiment of the aforementioned burner in which the downstream ends of the central and / or annular bundles of parallel or helical tubes are withdrawn upstream of the burner surface, additional mixing of the feed streams can be obtained by applying at least one coaxial cylindrical shaped pre-mixing chambers in series in said central conduit in which said first and second feed streams are mixed, and / or at least one coaxial annular shaped pre-mixing chambers in series in said annular passage in which said third and fourth feed streams be mixed.

The burner may include several longitudinal gas lines parallel to the brand axis and spaced radially between said center pipe and said annular passage. Said gas lines are at the downstream end near the end of the burner. and are connected at the upstream end to a gaseous feed stream. Several supply lines connect said gas lines to said premixing chambers in said central conduit and / or to said annular passage. A gaseous feed stream selected from the group consisting of steam, free oxygen-containing gas, CO2, Ng, fuel gas, a process-recycled portion of the product gas, and mixtures thereof, can be passed therethrough said longitudinal gas line and feed lines 8202327 And in the said premixing chambers to improve mixing, the break-through-clear passages, or around a gaseous component. to initiate that the reaction taking place in the gasifier will influence.

5 The fuel can be fed through both the power station. and / or annular bundle or bundles of tubes, or alternatively through the conduit or conduits surrounding the tubes in the central and / or annular parts of the burner. At the same time, the free oxygen-containing gas is passed through the corresponding unoccupied passage or passages in the central and / or annular parts of the burner. In one embodiment, a type of fuel is passed through a part of the burner, i.e. the central or annular part, while a second type of fuel is passed through the remaining part of the burner 15.

Preferably, in the present two-section burner, said first and third reactant feed streams and said second and fourth reactant feed streams are respectively constructed from split streams of the fuel stream or streams, and the gaseous oxidant stream. By these means, fuel is passed through the central or annular bundle of tubes, while at the same time free oxygen-containing gas is passed through the corresponding central and annular lines. In one embodiment, however, the first and fourth feed streams a.

V and the second and third feed streams, respectively, composed of split streams of the fuel stream or streams, and the gaseous oxidant stream. By these means, fuel is passed through the central bundle of tubes and the annular conduit, while at the same time free oxygen-containing gas is passed through the corresponding central conduit and annular bundle of conduits.

0

Flow control means is provided in the present method for controlling the introduction of said reactant feed streams into the burner. In addition, means are provided for exchanging fuels without shutting down or releasing the gas generator.

When the primary fuel passes through the pipes or surrounding passages in the central and / or annular parts 8202327 Λ * ..

- 38 - Flows from the burner, the following are preferred embodiments of the present method for replacing the main fuel with the reserve fuel: (1) Replacing the main fuel with the reserve fuel can be performed simultaneously in the center. radial and / or annular parts of the burner.

(2) alternatively, the replacement of the main fuel with the reserve fuel may be carried out sequentially, first in one of the burner parts. This is then followed by the replacement of the fuels in the remaining part of the burner.

When a flow of the main fuel flows through one part of the burner and the other part is unused C ~ * 4, a flow of the reserve fuel can first be introduced into the unused part of the burner. The main fuel can be shut off in the part in which it flows with the related stream of oxygen-containing gas with or without mixing with a temperature-initiating gas. The main fuel flow can be shut off simultaneously with or after the initiation of the reserve fuel flow. In such a case, after the reserve fuel replaces the main fuel, only part of the two-part burner is in use. Alternatively, the main fuel may also be replaced in the part in which it originally flowed by a flow of said second solid carbonaceous fuel slurry or hydrocarbon fuel.

In such a case, after the reserve fuel replaces the main fuel, both parts of the burner are in use.

In the above schemes, the main and / or reserve fuels may or may not be mixed with H20.

Controls are made for the free oxygen-containing gas stream with or without mixing with a temperature moderating gas flowing in the tubes or surrounding passages related to the corresponding surrounding passages or tubes in which the fuel flow flows and additional H 2 O is added if necessary. the reaction zone to maintain the weight ratio of the H 2 to fuel and the temperature in the reaction zone at design conditions. For example, the temperature 8202327 P * - 39 - in the reaction zone can be kept almost constant, i.e. less than + 95 ° C variation; and the weight ratio. H 2 O / fuel in the reaction zone can be maintained in the range of about 0.2-3.0.

5 Therefore, if the main or first fuel flowing through a first or second liquid passage in the central or first part of the burner and / or through the third or fourth liquid passage * in the annular or second part of the burner is not available and it is desired to switch to a reserve or second fuel, or for some reason it is desirable to switch from a first slurry of solid carbonaceous fuel or hydrocarbon fuel to a ('• .λ second slurry of solid carbonaceous fuel or hydrocarbon fuel, proceed as follows: (1) feeding a first reactant stream from the first slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with E 2 O through the first or second liquid passage means in the central or first portion of said burner, and / or passing a second reactant stream of the said burner at the same time passing the first slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with 10 through the third or fourth liquid, into the annular or second portion of said burner; (2) simultaneously passing a separate reactant stream of free oxygen-containing gas, whether or not mixed with a temperature-inducing gas, through the unused liquid passageway in each of the central and / or annular portions of said burner connected to said liquid passage through which said stream or streams of first slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with E 2 O, pass; (3) mixing the said reactant streams of (1) and (2) to produce a well-distributed mixture, and reacting these mixtures by partial oxidation in the reaction zone of said gas generator at an autogenous temperature in the range of about 925 ° -1926 ° c, A a pressure in the range of about 1-300 atmospheres, an atomic ratio of oxygen / carbon in the range of about 8202327 µm - 40 - 0.5-1.7, and a weight ratio of fuel to fuel in the range of about 0-5.0; (4) dephasing the liquid passage into which said central and / or annular part or parts (5) said stream or streams of first slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with streams, said out-of-phase - occurs with a uniformly decreasing flow rate ranging from maximum to 0 over a period of time in the range of about 1-3600 seconds; and simultaneously phasing said stream or streams of second slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with 10, in the same liquid passage means with a uniformly increasing flow rate that varies from 0 to maximum speed during the same period of time and mixing with the remainder of and replacing the phase-out portion of said stream of first slurry of solid carbonaceous fuel or hydrocarbon fuel with or without mixing with H 2 O 4 flowing therein, And (5) controlling the temperature and weight ratio of I 2 O / fuel in the reaction zone to design conditions by controlling the flow rate or flow rates of the reactant stream or flows of free oxygen-containing gas with or without mixing with a mode-V ... temperature gas passing through the burner, and adding additional E ^ O to the reactor if necessary control zone.

For example, by the present process, the temperature in the reaction zone can be kept almost constant, ie, a variation of less than + 95 ° C, and the weight ratio H 2 O / fuel can be maintained in the range of about 0.2-3.0 .

In the present flow control means, a manually or automatically controlled liquid control means is placed in each power line. For slurry fuel feed lines, a signal from the controller is transferred to a speed controller for a positive displacement pump.

\ For liquid and gaseous hydrocarbon fuel power lines and for oxidant power lines, the signal is 8202327

lr I

- 41 - Controller transferred to a flow control valve. In response to said signal or signals, the speed of said pump or pumps is changed, or alternatively, the opening in said flow control valve or valves S is changed. By these means, the flow rate for the fuel and / or oxidant flows passing through the burner can be controlled up or down, for example, up to about 50% of the design conditions. Alternatively, a flow control valve may be introduced into each of the feed streams to start or stop the flow of the feed streams to the central leading and / or the annular passage and to their respective tube bundles. By these means, three ζ. n flow series are obtained through the burner. Furthermore, both of these flow control schemes can be combined.

By means of the present burner, a large volume of the first reactant stream is split into several separate streams of reactant liquid or gas flowing through the central bundle of helical or similar tubes. bit allows the initiation of the second flow of reactants passing simultaneously through the center leading into the interstices and / or passages surrounding the central bundle of helical or parallel tubes. Similarly, a large volume of the third reactant stream is split into several separate reactant liquid or gas streams flowing through the annular bundle of helical or parallel tubes. The fourth stream of reactants surrounding the shaped bundle of helical or parallel tubes at the same time. The greater the number of tubes in one bundle, the better is the distribution of one reactant into the other reactant. The mixing of the reactant streams which takes place downstream of the ends of the tubes is facilitated by this improved distribution. Such efficient mixing of the feed streams facilitates a more uniform partial oxidation of the fuel; to produce H2 and CO. The combustion efficiency of the a process is thus increased.

| By means of the present invention, I 8202327 '

Reactions continue in local areas where there is less opportunity for the fuel to overheat with an insufficient supply of oxygen resulting in the formation of soot. The amount of unreacted finely divided carbon prepared at a given oxygen to carbon atom ratio in the feed can be significantly reduced. Furthermore, "over-combustion" of the fuel to prepare carbon dioxide is significantly reduced. The present burner is preferably made of heat and corrosion resistant metal alloys.

The rate of the reactant flow through the central and annular bundle of tubes, or alternatively through the centrale'λ central conduit or annular passage surrounding said tubes, is in the range of about 5-100, e.g. 15 10-50 feet per second on the outer surface of the burner when said reactant stream is a liquid hydrocarbon fuel or liquid suspension of solid carbonaceous fuel, or mixtures therefrom, and in the range of about 150 feet per second to the speed of sound, for example 200-500 feet per second when said reactant stream is a gaseous hydrocarbon fuel or a free oxygen-containing gas, whether or not mixed with a temperature moderator. The rate of a flow of reactant component fuel or a stream of a mixture of reactant component fuels is greater than the flame propagation rate for that fuel or fuel mixture.

The central bundle of tubes may have a number of tubes in the range of 1-200 or more, such as about 2-180, e.g. about 4-48. The annular bundle of tubes can have a number of tubes in the range of about 1-600, or more, such as about 2-580, for example about 8-108. There may be 1-7 or more concentric rings of tubes in the central and / or annular bundles.

The ratio of the total tube cross-sectional area (base internal diameter) for the annular bundle of tubes (T) to the total tube cross-sectional area (base ϋ * internal diameter) for the central bundle of tubes (Tc) can be in IT the range of about 2-8. In such a way, the ratio of the annular interspace cross-sectional area (1 ^) surrounding the annular bundle of tubes to the central interspace cross-sectional area (1 ^) surrounding the central bundle of tubes be in the range of about 2-8.

The inner diameter of the tubes in each bundle can range from about 1/16 to 2 inches in diameter. The length of the tubes in the central and annular bundles and their distances are such that they allow the external reactant stream to flow smoothly into the interstices between the tubes. For example, the length of the tubing or the height of the tubing in each tubing bundle can range from about 1/2 to 36 inches or longer, and preferably from approx. (./, spring 4-12 inches, requiring greater lengths when the number of tubes and the total size of the burner increases.

Preferably, the ratio of the length to inner diameter of the tubes should be at least 8. Preferably, the inner diameter and length of each tube should be the same for all tubes in the central bundle or the annular bundle.

By these means, equal flow can be obtained through all tubes.

Straightening pins, fins, centering blades, spacers and other conventional means are used for symmetrically spacing the tubes and lines from each other and to keep them in stable alignment without impeding the free flow of the feedstreams in the central and annular spacing zones.

The downstream outlet ends of the various annular and central bundles of parallel tubes terminate in the same plane perpendicular to the longitudinal central axis 30 of the burner. In an embodiment using premixing chambers, which will be described further, the ends of the central and / or annular bundle of tubes are withdrawn upstream of the burner exterior to provide substantial mixing of the reactants and evaporation of the suspension medium prior to disposal.

The central outlet opening of the conduit and / or the annular outlet opening may have converging parts.

de l For example, the outlet of the central conduit may be an I 8202327 2 *.

44 - frusto-conical rear portion having a converging angle in the range of about 15 ° -90 ° from the. central longitudinal axis of the burner. The rear part can develop into a normal cylindrical advantage 5 which ends at the downstream outer face of the burner. The cyiindrical advantage can have a height in the range of about 0-1.5 times its own diameter.

In one embodiment, the first downstream line outlet includes a converging frusto-conical rear portion that develops into a divergent frusto-conical advantage terminating at the downstream end of the burner. The converging and diverging angles are C in the range of about 15 ° -90 ° with the burner central lung longitudinal axis.

In such a manner, said annular outlet opening may comprise a developed converging frusto-conical shaped annular rear portion which has a converging angle in the range of about 15 ° -90 ° from the central axis of the frusto-conical portion / portion. said central axis is parallel to the central longitudinal axis of the burner. The rear portion can transition to a developed normal cylindrical annular advantage that ends at the downstream outer face of the burner. The cyiindrical front portion may have a height in the range of about 0-1.5 times its own width.

In one embodiment, the center conduit exit port and / or the annular exit port are in the form of or developed by an American Society of Mechanical Engineer's standard long-radius nozzle. A further description of the said nozzle can be found in "Thermodynamics Fluid Flow and Heat Transmission" by Huber 0. Croft, page 155, first edition, 1938 McGraw-Hill Book »« *

Company.

The burner can be cooled on the outside by means of cooling hoses that surround the outer barrel of the burner along its length. For example, an annular cooling chamber can accommodate the annular outlet opening and / or the outlet opening; from the central line. The cooling chamber, outlet opening - of the central pipe and / or the annular outlet opening 8202 3 2 7 - 45 - "- can form a single piece of heat and wear resistant material, such as tungsten carbide or silicon carbide. Any suitable coolant can be used, for example water.

In one embodiment of the present burner 5, several high pressure, high velocity jet streams of a gaseous material are fed into the central conduit and / or annular passageway at various locations along their length. By these means, the atomization of the fuel feed stream and, optionally mixing it with the oxidant stream, can be facilitated. For example, the gaseous material may be passed through several small diameter passages or cavities, ie, about 0.32-0.50 mm diameter, leading into said central conduit and / or annular passage.

The gaseous material can be selected from the group consisting of solids, free oxygen-containing gas, CC 2, N 2, fuel gas, a part of the product gas recycled in the process, and mixtures thereof. The gaseous material can be introduced into the burner at a temperature in the range from about ambient temperature to 825 ° C and a speed in the range from about 30.5 meters per second to the speed of sound. The pressure of the gaseous material can be in the range of about 5.3-315 kg / cm and is greater than the pressure of the other feed streams passing through the burner 25.

^. The discharge rate of the material discharged through the central exit port is in the range of about 0.5-1.5 times, and preferably the same as, the exit rate of the material discharged through the ring-shaped outlet port. The streams leaving the two outlet ports> mix together and sputtering can occur immediately downstream from the outer face of the burner.

In another embodiment of the invention. additional mixing of the reactant streams performed in at least one, eg 2-5 coaxial cylindrical shaped premix chambers in series in the central conduit and / or at least one, eg 2-5 annularly shaped premix chambers in series in the annular passage. In such a case £ ·. - the downstream / ends of the central beam are screw 8202327

i V

- 46 - linear or parallel bands withdrawn upstream from the outer pocket the burner by a distance of 0-12, such as about 2 or more, for example, 3-10 times the minimum diameter of the circular outlet and / or the 5 downstream ends of the annular bundle are helically or parallel tubes withdrawn upstream from the outer face of the burner by a distance of 0-12, such as about 2 or more, for example, about 3-10 times the minimum width of the annular outlet. Preferably, the downstream ends of the central and annular bundles of helical or parallel tubes are withdrawn upstream from the entrance of the first preform. mixing chamber in line. For example, the replacement of the ends of the tubes from the entrance to the first premix chamber can be in the range of about 0.1-2.0 times the diameter of the first premix chamber.

In one embodiment, each of the premixing chambers in the central conduit except the first are cylindrically shaped and comprise a coaxial cylindrical body portion formed by a coaxial, at least partially converging outlet portion. The first cylindrically shaped premix chamber in the central conduit includes a normal coaxial cylindrical body portion which directly discharges into the aligned coaxial cylindrical premix chamber. Each premix chamber in the annular conduit, except the first, is annular shaped and includes a coaxially developed convergent output.

cone-shaped annular outlet part. The first annularly shaped premixing chamber comprises a coaxially developed normally cylindrical annular body portion which directly discharges into the aligned coaxial annularly shaped premixing chamber. The converging exhaust parts of said precor mixing chambers may be made of tungsten carbide or silicon carbide for increased wear resistance.

The size ratio between successive pre-mixing chambers in the present burners can be expressed in the following way: for burners in which the pre-mixing chambers in the central pipe are consecutively numbered 1-5 and / or the pre-mixing chambers in the annular conduit 6-10 are numbered, the ratio of the diameter of each can be an 8202327

"· A

From said central chambers to the diameter of the next central chamber in the line, i.e. D; D2; D2: D3; D3: D4; or: D ^ are in the range of about 0.2-1.2.

The ratio of the length of each one of the central pre-mixing chambers in said central conduit to the length of the next central pre-mixing chamber in the conduit i.e. L1: L2; L2: L3; L3: L47 or can be in the range of about 0.1-1.0. The ratio of the annular width of each of said annular premixing chambers to the width of the next annular chamber in the line ie Wg: W7; W ^ iWgj Wg: W ^ 7 or W ^: W ^ q can be in the range of about 0.1-1.2. The ratio of the length of each one of the annular premixing chambers in said annular passage to the length of the next annular premixing chamber in the line, i.e., L ^ iLg; LgiL ^ r or can are in the range of about 0.1-1.0.

In most other respects, the construction of this premixing embodiment of the burner, comprising the tubes, passages, openings, water-cooled faceplate and 20 cooling hoses, is high pressure and high velocity jets of said gaseous and / or or annular premixing chambers, and flow control means substantially the same as previously described. Furthermore, the ranges of temperature, pressure and velocity for the flows of materials passing through the different passages of the burner are almost the same as those discussed above.

In the operation of the burner embodiment using premixing chambers, flow control means can be used to control the flow of the four feed streams 30 to the tubes and passages in the burner in the same manner as described above. The feed streams entering the burner and simultaneously passing through them at different speeds collide and mix together in the first premix chambers. The collision of a reactant stream, such as the liquid slurry of solid carbonaceous fuel in a liquid medium, optionally mixed with a temperature moderator, with another reactant stream, such as a gaseous stream of a free oxygen-containing gas, optionally mixed with a temperature moderator, at a higher rate, causes the liquid suspension to decompose into a fine atomized liquid. The prepared multi-phase mixture then passes successively through the remaining pre-mixing chambers where additional mixing takes place. Since the mixture 5 passes freely through the present unobstructed burner, its speed changes many times. For example, at various points in the burner, the speed of the mixture can vary from about 6-180 meters per second. As the mixture flows from one premix chamber to the next, the changes in velocity are mainly the result of changes in the diameter of the flow path and the amount and temperature of the mixture. This promotes a thorough mixing of the components. By operating in the area of turbulent flow, mixing can be maximized. Furthermore, direct heat exchange between the materials takes place within the burner. From 0-100% by volume, for example about 5-25% by volume, of the liquids in the feed streams may have evaporated before the feed streams leave the burner. The feed flows can be accelerated directly in the reaction zone of the gasifier for partial oxidation by means of converging outlet openings.

Burning of the flammable substances as they pass through the pre-mixing zone of the burner can be prevented by discharging the multiphase mixtures at the central 25 and annular exhaust openings at the end of the burner. with an exhaust velocity greater than the propagation velocity of the flame. Flame rates are a function of factors such as composition of the mixture, temperature and pressure. They can be calculated by conventional methods or determined experimentally. The ratio of the exhaust velocity for the multiphase mixture discharged through the central exhaust port to the multiphase mixture discharged through the annular exhaust port may be in the range of about 0.5-1.5, such as 1.6.

35 Depending on factors such as the temperature, speed, residence time and composition of the feed streams: the desired amount of evaporation of the liquid carrier; the temperature and quantity to be returned in the process \ gases in the generator; and the desired life of the burner hoses may or may not surround the burner outer vessel along its length. For such reasons, the burner may or may not have an annular cooling chamber at the downstream end.

The multiphase mixtures starting simultaneously from the central opening and / or the annular opening at the downstream end of the burner mix together downstream of the outer surface of the burner.

Advantageously, by means of the present burner, the exothermic partial oxidation reactions take place at a sufficient distance downstream of the burner surface to protect the burner from thermal damage.

^. Liquid hydrocarbon fuels and / or pumpable suspensions of solid carbonaceous fuels having a dry matter content in the range of about 30-75 wt%, for example about 40-70 wt%, can be passed through the inlet passages of the present burner lined. For example, the fuel flows can be passed through the central and / or annular bundle of tubes. The inlet temperature of the liquid hydrocarbon fuel or the slurry is in the range of about ambient temperature otm ^m l 13r C, preferably below the evaporation temperature of the liquid hydrocarbon at the given inlet pressure in the range of about 1 - 300 atmospheres, such as 5 -250 atmospheres, for example about 10-100 atmospheres.

The term solid carbonaceous fuels, as used herein to describe suitable solid carbonaceous feedstocks, is intended to include various materials and mixtures thereof from the group consisting of coal, carbon coke, carbonized carbon product , coal liquefaction residues, petroleum coke, particulate carbon black, and solids derived from oil-containing slate, tar sand, and pitch. All types of coal can be used, including anthracite, bituminous coal, sub-bituminous carbon, and lignite. The finely divided cabbage can be that »j.

which is obtained as a by-product of the present invention

Partial oxidation process, or that obtained by burning fossil fuels. The term solid carbonaceous fuel by definition also includes garbage pieces, dewatered sanitary sewage sludge, and semi-solid organic materials such as asphalt, rubber and rubber-like materials, including rubber car tires that can be crushed or pulverized to the appropriate particle size. Any suitable grinding system can be used to convert the solid carbonaceous fuel or mixtures thereof to the desired size.

The solid carbonaceous fuels are preferably comminuted to such a particle size that 100% of the material passes through an ASTM screen. E 11-70 Sieve 10 Designation Standard 1.4 mm (Alternative No. 14) and at least 80% passes through a sieve ASTM E 11-70 Sieve Designation Standard 425yt * m (Alternative No. 40).

The moisture content of the solid carbonaceous fuel particles ranges from about 0-40 wt%, such as 2-20 wt%.

The term liquid carrier as used herein as the suspending medium to produce the pumpable suspensions of solid carbonaceous fuels is intended to include various materials from the group consisting of water, liquid hydrocarbon material, and mixtures thereof. However, water is the preferred carrier for the solid carbonaceous fuel particles. In one embodiment, the liquid carrier is liquid carbon dioxide. In such a case, the liquid slurry may contain 40-70% by weight of solid carbonaceous fuel and the remainder is liquid. The CC ^ solid fuel suspension can be fed into the burner at a temperature in the range of about -55 ° C-38 ° C depending on the pressure.

The term liquid hydrocarbon material as used herein to describe suitable liquid carriers and fuels is intended to include various liquid hydrocarbon materials, such as those selected from the group consisting of liquefied petroleum gas, petroleum distillates residues, gasoline, naphtha, kerosene, crude petroleum, asphalt, gas oil, residual oil, tar sands oil and slate oil, carbon-derived oil, aromatic hydrocarbons (such as: A benzene, toluene, xylene fractions), coal tar, cycle gas oil from liquid catalytic cracking, furfural extract of coke oven fuel oil and mixtures thereof.

8202327 \ i. Jt - 51 -

The term liquid hydrocarbon material as used herein to describe suitable liquid fuels is also intended to include various oxygen-containing liquid hydrocarbon organic materials, such as those selected from the group consisting of carbohydrates, cellulosic materials, aldehydes, organic acids, alcohols, ketones,. oxidized fuel oil, waste liquids and by-products of chemical processes for the preparation of oxidized hydrocarbon organic materials, and mixtures thereof.

For example, the feed stream in an embodiment comprises a slurry of liquid hydrocarbon material and solid carbonaceous fuel. HjO in liquid phase ζ. can be mixed with the liquid hydrocarbon carrier, for example as an emulsion. A portion of the H 2 O, ie about 0-25 wt.% Of the total amount of Η2 <0 present, can be introduced as steam mixed with the free oxygen-containing gas. The H 2 O / fuel weight ratio may range from 0-5, for example, about 0.1-3.

The term gaseous hydrocarbon material as used herein to describe suitable gaseous hydrocarbon fuel phenols is intended to include a gaseous feedstock of the group consisting of ethane, propane, butane, pentane, methane, natural gas, coke oven gas, refinery% gas, acetylene waste gas , ethylene waste gas, and mixtures thereof.

25 Simultaneously with the fuel flow or fuel flows / r— ·.

, Έέη or more free oxygen-containing gas streams are supplied by means of a free passage or free passageways in the burner. The free oxygen-containing gas can be passed through the central and / or annular sections at a temperature in the range from about ambient temperature to 815 ° C, and preferably in the range from about ambient temperature to 150 ° C, for with oxygen enriched air, and about 260 ° C to 650 ° C, for air, and a pressure in the range of above about 1-300 atmospheres, such as about 5-250 atmospheres, for example, about 10-100 atmospheres. The atomic free oxygen plus atoms of organically bound oxygen - in the solid carbonaceous fuel per atom of carbon in the solid carbonaceous fuel (0 / C atomic ratio) may be in the range of 0.5-1.95. With free oxygen-containing λ 8202327 Γ ».

Gas in the reaction zone, the wide range of said 0 / C atomic ratio can be about 0.5-1.7, such as about 0.7-1.4. More specifically, with air fed to the reaction zone, said O / C atomic ratio can be about 0.7-1.6, such as about 0.9-1.4.

The term free oxygen-containing gas, as used herein, is intended to include air, oxygen-enriched air, that is, more than 21 mole percent oxygen, and substantially pure oxygen, i.e., more than 95 mole percent oxygen, (the rest includes N2 and noble gases).

The free oxygen-containing gas can be fed, mixed or not, with a temperature moderating gas. The recommendation. interpretation temperature moderating gas as used herein is intended by definition to include a member of the group consisting of sttom, CO2, N2, a process-recycled portion of the cooled and purified off-gas stream from the gas generator, and mixtures thereof.

The present burners as shown in Figs. 3-4 can operate with the supply currents passing through alternative 20 passages in the burner. Typical modes of operation before and after fuel replacement are summarized in Tables I and II below.

Table I lists the materials introduced into the gasifier by means of the burner and their corresponding symbol. The solid carbonaceous fuel (B), water (C), and liquid hydrocarbon material (E) can be mixed together in different combinations upstream of the burner inlet to give a pumpable slurry that can be passed into the burner and then passed through one of the several free-flow passages of the burner as indicated in Table II. For example, the first column in Table II shows that a pumpable slurry stream comprising solid carbonaceous fuel (B) mixed with water (Cj 'can be passed through the central and / or annular bundle of tubes in the burner, ie Figures 1 and 2 When a fuel stream is introduced into the burner through the center and / or bundles of tubes, a corresponding stream of oxygen-containing gas is simultaneously passed through the related center line 8202327-53 and / or Annular Passage Some additional examples follow: (1) Separate streams of free oxygen-containing gas may be passed through said central and / or annular bundles of tubes, and at the same time, separate corresponding streams of a pumpable slurry of solid carbonaceous fuel in a liquid carrier or a hydrocarbon fuel is passed through the related central conduit and / or annular passage.

(2) separate streams of free oxygen-containing gas 10 can pass through said central conduit and said central passage; while simultaneously passing a corresponding flow of liquid hydrocarbon material through the related central and / or annular bundles of tubes; and at the same time, a pumpable slurry of solid carbonaceous fuel in a liquid carrier can be passed through the unoccupied bundle of said tubes, if any.

(3) separate streams of free oxygen-containing gas may pass through said central and / or annular bundles of tubes; while simultaneously passing a corresponding flow of liquid hydrocarbon material through the related central conduit and / or annular conduit; and at the same time, a pumpable slurry of solid carbonaceous fuel in a liquid carrier can pass through the unoccupied ».

passage, if any.

25 TABLE I

!> Material Symbol

Free oxygen-containing gas A.

Solid carbonaceous fuel B

Water C

30 Steam D

Liquid hydrocarbon material E

Moderating gas temperature F

Gaseous hydrocarbon fuel G

8202327 I \

- 54 - TABLE II

Central Central Annular Annular • pipe bundle of pipes passage bundle of pipes

A B + C A B + C

5 A + D B + C A + D B + C

B + C · A. B + C A

. A B + C B + C A

B + C A A B + C

A B + C + E A B + C + E

10 B + C + E A + D B + C + EA + D

A E A E

A + D B + E A + D 'B + E

B + E A + D B + E A + D

A + D E A B + C

15 E A E A

B + C A E A

/ -, E A B + C A

A G A B + C

A G A + D E

20 A E + F A E + F

E + F A + D · E + F A + D

Other modes of carrying out the present method are possible except those indicated in Table II.

For example, jet streams of a gaseous material can be simultaneously introduced into the central conduit and / or arcuate passageway, as described above.

When έέη of the fuel flows one. liquid hydrocarbon or the liquid carrier for the suspension of solid carbonaceous fuel is a liquid hydrocarbon material f premature combustion within the burner can be prevented by one or more of the following measures: (1) holding the fuel under its auto-combustion temperature / 35 (2) introducing water into the solid fuel slurry, (3) using air or oxygen enriched air i.e. up to about 40 vol% CL,.

(4) mixing steam with the air, (5) using about 0 withdrawal of the ends of the central or annular bundles of tubes from the outside.

face of the burner. In such a case, the free oxygen-containing gas such as substantially pure oxygen can be separately vented from the burner without first contacting the fuel stream.

45 (6) discharging the multiphase mixture at the central and annular exhaust vents at the burner end with exhaust rates greater than the rate of flame propagation.

The subject burner combination is introduced downward through a top inlet port of a compact, unpacked, 8202327

* A

- 55 - Free flow permitting, non-catalytic, refractory lined synthesis gas generator, as shown, for example, in U.S. Pat. U.S. Patent 3,544,291. The burner extends along the central longitudinal axis of the gas generator with the downstream end leaving directly into the reaction zone.

The relative proportions of the reactant feed streams and any temperature moderator fed into the gas generator are carefully controlled to reduce a significant proportion of the carbon in the fuel, for example, up to about 90% or more by weight. , in carbon oxides; and to maintain an autogenous reaction temperature zone in the range of about 925 ° -1926 ° C, preferably in the range of 1095 ° -1540 ° C. ζ. The residence time in the reaction zone is in the range of about 1-10 seconds, and preferably in the range of about 2-8. With nearly pure oxygen feed to the gas generator, the composition of the gas generator outflowing gas in mol% on a dry basis may be as follows: H2 10-60,

CO 20-60, C02 5-40, CE ^ 0.01-5, H2S + COS 0-5, N2 0-5, and A

0-1.5. With air supply for the gas generator, the composition of the generator output gas in mol% on a dry basis may be approximately as follows: E2 2-30, CO 5-35, CO2 5-25, CH4 0-2, H2S + COS 0 -3, N2 45-80, and 0.5-1.5. Unreacted carbon and ash are present in the gas exhaust stream.

The hot gaseous exhaust stream from the reaction zone of the synthesis gas generator is rapidly cooled below the reaction temperature to a temperature in the range of about 120 ° -370 ° C by direct rapid cooling in water, or by direct heat exchange for example, with water to produce steam in a gas cooler.

Advantageously, in another embodiment of the present invention, the present two-section burner can be used as the preheat burner during start-up of the gasifier, as well as the production burner.

"03Γ

Start-up procedures are thereby simplified. Early time was lost when the preheat burner was replaced by the production burner, and the gasifier cooled. Now the gasifier can be brought to working temperature and held thereon by simultaneously running a gaseous or liquid hydrocarbon fuel i.e. fuel gas, whether or not 8202327 * 56 - not mixed with the central and / or annular bundle or bundles tubes and a free oxygen-containing gas, preferably air, whether or not mixed with O 2, through the related central conduit and / or annular passageway. Alternatively, the gaseous or liquid hydrocarbon fuel, ie fuel gas, whether or not mixed with E 2 O, may be passed through the central conduit and / or annular passage in the burner and air, whether or not mixed with H 2 O , can be passed through the related central and / or annular bundle or bundles of tubes. The fuel gas and air are mixed together to produce a well-distributed mixture. Combustion of the mixture by almost complete combustion then takes place in the reaction zone of the gas generator at a temperature in the range of about 1095-2480 ° C, such as about 1095-1650 ° C, and at an absolute pressure in the range of about 0.56-300 atmospheres, and preferably 1 atmosphere. The complete combustion products are removed from the reaction zone. For example, they can be vented to the atmosphere.

By these means, the reaction zone is heated to the temperature required for ignition of the autothermal partial oxidation reaction of the main fuel selected from the group consisting of a pumpable slurry of solid carbonaceous fuel, liquid or gaseous hydrocarbon fuel, and mixtures thereof with a free oxygen-containing gas and with or without a temperature moderator. For example, the auto-ignition temperature may range from about 1095-1480 ° C. At this point, the fuel gas, whether or not mixed with 1 ^ 0, is dephased from the pipes or conduits in which it flows into the central and / or annular section or sections of said two-section burner with a uniformly decreasing flow rate ranging from maximum speed to 0 over a period in the range of about 1-3600 seconds, for example about 60-1800 seconds. At the same time, the main slurry of solid carbon-containing fuel or liquid hydrocarbon fuel, whether or not mixed with H 2 O, is phase-balanced in the remaining portion of said fuel gas and replaces the phase-out portion of the fuel gas with a uniformly increasing flow rate ranging from 0 to maximum over the same time period.

8202327 4 1 - 57 -

Simultaneously with the replacement of the fuel, or alternatively when the fuel gas in the burner has been completely replaced by the main fuel, the free oxygen-containing gas, ie air, may or may not be mixed with H 2 O / off phase charged with a uniformly decreasing flow rate ranging from maximum to 0 over a period in the range of 1-3600 seconds, for example about 60-1800 seconds. At the same time, another free oxygen-containing gas, ie, oxygen-rich gas or substantially pure oxygen, is phase-aligned for the production of synthesis gas in the same line to replace the air at a uniformly increasing flow rate ranging from 0-maximum about the same £; time period. Furthermore, the flow rates of the free oxygen-containing gas, whether or not mixed with H 2 O, and if necessary the H 2 O / fuel weight ratio in the reaction zone are controlled so as to continuously maintain the temperature and H 2 O / fuel ratio in the reaction zone on the design conditions for partial oxidation of the said main fuel.

Partial oxidation of the main fuel takes place downstream in the reaction zone of the non-catalytic, free-flowing, gas generator at design conditions, which implies an autogenous temperature in the range of about 925-1925 ° C, a pressure in the range of about 1-300 atmospheres, and an atomic ratio of oxygen (... to carbon in the range of about 0.5-1.7, for example, 0.8-1.2, and an H 2 O / fuel weight ratio in the range of about 0-5.0, such as 0.1-3.

The hot gaseous exhaust stream from the reaction zone 30 of the synthesis gas generator is rapidly cooled below the reaction temperature to a temperature in the range of about 120 ° -370 ° C by direct rapid cooling in water, or by indirect heat exchange for example with water to * produce steam in a gas cooler. The gas stream can be cleaned and purified by conventional methods.

A more complete understanding of the invention can be obtained by reference to Figs. 4 and 5 of the drawings showing the present invention in detail. Although the drawing illustrates preferred embodiments of the invention, 8202327 * - 58 - it is not intended to limit the present invention to the disclosed particular device or materials described. To equal parts in the embodiments of Figs.

1-5, the same reference numerals are given.

5 Referring to Figs. 4 and 5, FIG. 4 is a schematic representation of an embodiment of the invention showing control means for the continuous operation of a synthesis gas generator while one fuel is being out of phase and another in phase at the same time without pressure relief. Furthermore, the control means can be used to quickly change flow levels above or below the flow level for which the two-piece burner shown is designed. By these means, controls can be made to control the amount of raw output gas produced, and to provide a change in demand for the product gas. Furthermore, another use of the control system is to maintain the desired composition of the product gas when it is possible to do so by controlling the flow rates of one or more of the reactant streams. Thus, the present flow control system controls the flow rates for all reactant streams separately and independently so that the temperature and weight ratio of H00 to fuel in the reaction zone are maintained at design conditions and within desired fuel operating ranges. that is brought into the response. If necessary, the atomic ratio of free oxygen to carbon in the fuel in the reaction zone can also be controlled within design conditions.

While the control system shown in FIG. 4 is especially designed for the combination of feed supplies comprising a slurry of solid carbonaceous fuel and a liquid hydrocarbon fuel, the system can, through simple changes to the means for changing the flow rate of the flows up or down in a manner similar to that described below are used to control other combinations of solid carbonaceous fuel suspensions, and liquid, or gaseous hydrocarbon fuels.

Two-section burner 1 is mounted in central flanged inlet 30 8202327% 59 - 59 located in the upper portion of a conventional refractory lined, free flow permitting, synthesis gas generator 41 along the central longitudinal axis. The reactant streams enter the upstream end of burner 1, pass through it in a downward direction, and are discharged through the downstream end. Burner 1 is designed so that the required system production for steady-state operation can be accomplished or even exceeded by a special amount when the flow rate through all passages in both sections of the two-section burner is maximum. The control system can independently increase or decrease the flow rate of one or more of the reactant streams in lines 187, 190, 167, 170, 50, 60, 70 and 73. By these means, the temperature in the reaction zone 31 is maintained at the desired operating temperature. Furthermore, the weight ratio to fuel, and if necessary the atomic ratio of free oxygen to carbon in the fuel in the reaction zone, can be maintained at design conditions when one or both sections of the burner are used to increase or decrease product gas production. to bring.

Two-section burner 1 includes a central section and a concentric annular section. The central section largely comprises: central cylindrical conduit 2 with a closed upstream end and an open downstream end, central bundle of parallel tubes 3 supported longitudinally in central passage 4 of central conduit 2 and with open upstream ends passing through and are sealed in the closed upstream end of central conduit 2 and in communication 30 with central cylindrical shaped manifold 19, inlet feed pipe 20 connected to and in communication with central manifold 19, and inlet feed pipe 25 connected to and in communication with the closed upstream end from central conduit 2. The annular section includes: outer cylindrical concentric conduit 5 which is closed at the upstream end and open at the downstream end, annular passage 6 between the outer diameter of central conduit 2 and the inner diameter of outer conduit 5 along its length, annular bundle of parallel tube and 7 longitudinally supported in said annular passage 6 and having open upstream ends which pass through and are sealed in the closed upstream end of outer conduit 5 and are connected to annular manifold 28, inlet feed pipe 5 29 connected to and in connection with annular manifold 2.8, and inlet feed pipe 35 connected to and in connection with the upstream closed end of outer conduit 5.

While the downstream ends of central beam tubes 3 and annular beam tubes 7 in Fig. 4 are indicated to be flush with the outer face of burner 1, in other embodiments of the two-section burner, the downstream ends of the central and / or annular bundle or bundles of tubes are withdrawn upstream to provide at least one pre-mixing zone as shown in Fig. 5.

Although the central bundle of tubes 3 and annular bundle of tubes 7 in FIG. 4 are indicated as parallel to each other and to the burner axis, in another embodiment of the two-coTWartiment burner shown and described in FIG. US Patent * i.e., Fig. 5 thereof, the central and / or annular bundles of tubes are formed in a helical manner. These means allow the swirling reaction component to flow downward through the center and / or annular bundles of helical tubes; and separately down through the helical passages / on the outside of the helical bundles of tubes collide both in the premix zones or downstream in the reaction zone and thereby can be intimately mixed together. The combustion efficiency of the burner is thereby improved.

In FIG. 4, for illustrative purposes, the primary fuel may be, for example, a slurry of solid carbonaceous fuel, i.e., a carbon water slurry / conduit 42. The reserve fuel is a liquid hydrocarbon hydrogen, ie residual oil in line 160. Of course, for the main fuel, any liquid or gaseous hydrocarbon fuel or a carbon oil slurry can be selected. The measured feed stream of solid carbonaceous fuel slurry in line 42 is split into two 8202327-61 fuel feed streams 43 and 44 by separate flow control means in each line. In such a manner. the measured feed stream of liquid hydrocarbon fuel in line 160 split into two fuel feed streams 161 and 162 by separate flow control means in each line. In the present process, the remaining parts of the main fuel stream or streams that have been de-phaseed from line 50 and / or line 60 in lines 15 and / or 16, respectively, are mixed with the reserve fuel stream or 10 flows flowing in line 167 and / or line 170 are brought into phase.

In such a manner, the metered feed flow of free oxygen-containing gas in line 22 is split into two feed flows 63 and 64 by separate flow controllers in each line.

H20 may be mixed with the fuels in lines 160 and 42 or the free oxygen-containing gas in line 62. Alternatively, as shown in Figure 1, at least a portion, i.e. 10-100 vol% of the H20 may be steamed provided-20. Thus, the steam in line 180 is split into two feed streams 181 and 182 by separate flow control means in each line. By these means, as shown in Figure 4, steam in conduit or conduits 187 and / or 190 may preferably be mixed in conduit or conduits 18 and / or 17, respectively, with the free oxygen-containing gas flowing in one or both ( Sections of the burner flow In such a way (not shown), steam from line or lines 187 and / or Ϊ90 can be supplied to the fuel in line or lines 15 and / or 16, respectively. quantities of steam are introduced into and mixed with the stream or streams of free oxygen-containing gas and / or fuel upstream of the burner.

The amount of flow by weight or volume for that portion of the feed that flows through each of the feed lines to the burner is a function of the burner design. For example, the dimensions of the burner passages may be such that one third of the total of the solid carbonaceous fuel slurry flowing through line 42 plus the liquid hydrocarbon fuel flowing through line 160 may be 8202327 ft. "- 62 - are discharged through central tube bundle 3 with a specified velocity range. At the same time, the remaining two thirds of the total amount of slurry of solid carbonaceous fuel plus liquid hydrocarbon-5 fuel can be discharged through annular tube bundle 7 with a specified speed range.

Valves 183, 184, 163, 164, 77, 76, 65 and 66 can be manually or automatically actuated to achieve a wide open position to a fully closed position.

10 The speeds at which each valve can be opened or closed are also adjustable. In an embodiment which will be further described, the burner can be unscrewed or segmented by closing specific valves. The burner can thereby be operated in the central part, ie central tubes 3 and annular passage 4, or in the outer annular section, ie annular tubes 7 and an annular passage 6, or with both the central annular sections of the burner in simultaneous operation.

The operation of the system using only the central part of the burner will be described first. The portion of the slurry feed stream in line 43 is pumped into the reaction zone 31 of synthesis gas generator 41 by means of positive displacement pump 45 provided with speed control 46, line 47, flow measuring device 25 and transmitter 48, line 49, valve 77, lines 50 and 15, inlet 20 of burner 1, central manifold 19, and central tube bundle 3.

The flow rate of the slurry through line 43 is controlled by the speed of the positive displacement pump 45. To phase out the slurry flowing through line 43, this speed is continuously reduced from maximum to zero over a period of time. range of about 1-3600 seconds, such as about 60-1800 seconds, for example 300-1000 seconds. Flow recorder with transducer 35 51 includes a microcomputer programmed with the desired time versus decreasing flow rate curve. The flow rate of the slurry in line 47 is measured and a signal a is provided by flow transmitter 48 corresponding to the flow rate of the slurry in line 43.

8202327 -63- V *

Flow recorder controller 51 receives a signal a, compares it with a signal representing the desired flow rate at that time, and provides a corresponding setting signal to speed control 46 to lower the speed of pump 5 45 so that the charge slurry flowing in line 49 flows a given reduced flow rate assumes for that instant in the phase-out period. The new suspension rate is measured and the cycle is repeated.

By these means, repeated adjustments of the flow rate are made and the slurry flowing in line 50 is brought out of phase.

Simultaneously with the phase-out of the portion of the main slurry of fuel flowing in line 43, the portion of reserve liquid hydrocarbon fuel flowing in line 161 is phase-out for the same period of time. Flow recorder controller with transmitter 171 includes a microcomputer programmed with the desired time against increasing flow rate curve. The rate of oil flow in line 171 is measured and a signal m is provided by flow transducer 165 corresponding to the flow rate of the oil in line 161. Flow recorder controller 71 receives signal m, compares it with a signal that the desired flow rate for that instant represents and provides a corresponding control signal to valve 163 to open wider so that the oil charge in line 166 assumes a given increased flow rate for that instant in the phase-in period. The new oil speed is measured and the cycle is repeated. By these means, repeated adjustments of the flow rates of the main and reserve fuels can be made so that the oil flowing in line 167 can be introduced into line 15 in an amount that reduces the amount of suspension of solid carbonaceous fuel which flows in line 50 compensates.

35 During or after the period when the portion of the main solid carbonaceous slurry fuel of line 43 is out of phase and the part of the reserve liquid hydrocarbon fuel of line 161 is out of phase, the weight ratio of temperature moderator to fuel may be 8202327 ι ί - 64 - in the reaction zone are controlled, for example, at design conditions, or nearly constant i.e. less than + 10% variation, by increasing or decreasing the flow rate of the temperature moderator. According to the present example, at the same time as the phase-out of the coal-water slurry, an additional amount of 10 O from an external source can be phase-ended over the same period of time.

Thus, in Fig. 4, some of the steam in line 180 passes through line 181 and is introduced into line 18 where it mixes with the free oxygen-containing gas from line 70. Flow recorder controller with transducer 191 includes a microcomputer is programmed with the desired time against increasing flow rate curve.

^ ...... The. flow rate of steam in line 181 is measured and a signal s is provided by flow transmitter 185 corresponding to the flow rate of steam in line 181.

Flow recorder controller 191 receives signal s, compares it with a signal representing the desired flow rate for the time, and provides a corresponding control signal to valve 183 to open wider so that the steam charge in line 186 assumes an increased flow rate for that time in the phase-in phase. The new steam speed is measured and the cycle is repeated. By these means, repeated controls of the flow rate of the steam are made and the steam flowing in line 187 is phase-fed in line 18 in an amount that will maintain the weight ratio of E2 O to fuel in the reaction zone at design conditions .

In another embodiment, the weight ratio of fuel / fuel in the reaction zone is controlled up or down by controlling the steam rate as described above to obtain a desired temperature in the reaction zone and a desired product gas composition. .

Simultaneously with or after de-phasing the primary fuel, de-phasing the reserve fuel, and optionally with or without de-phasing or de-phasing

Depending on the nature of the fuels, the free oxygen-containing gas may be regulated up or down to control the temperature in the reaction zone, for example at design conditions, or almost constant i.e. less than + 95 ° C variation. Thus, in the present example in Fig. 1, a portion of the free oxygen-containing gas in line 62 is passed through line 63 and phase 5 in line 18 where it mixes with steam, if any, from line 187 as described above. Flow controller 74 is programmed with the desired time versus flow rate curve. The regulation period is the same as for the fuel and steam flows. The oxygen flow rate control 10 can be up or down depending on the nature of the fuel flows and the addition of steam, if any. In the present example, the flow rate of the oxygen will be increased to meet the additional requirements for the partial oxidation of a liquid hydrocarbon as compared to a solid carbonaceous fuel.

The velocity of the free oxygen-containing gas in line 63 is measured and a signal b is provided by flow transmitter 67 corresponding to the flow rate. 20 of the free oxygen-containing gas in line 63. Flow recorder controller with transducer 74 includes a microcomputer that receives a signal b, compares it with a signal representing the desired flow rate for that time, and provides a corresponding control signal to valve 65 to open wider so that the charge of free oxygen-containing gas in line 68 assumes a given increased flow rate for that instant in the phase-in period. The new rate of the free oxygen-containing gas is measured and the cycle is repeated. By these means, repeated oxygen flow rate controls are made and the free oxygen-containing gas flowing in line 70 is phase-fed in line 18 in an amount that will keep the temperature in the reaction zone substantially constant.

In another embodiment, the rate of the free oxygen-containing gas is controlled up and down to obtain a desired temperature in the reaction zone and a desired composition of the product gas. Alternatively, by the above-described means, the atomic ratio of oxygen to carbon in the reaction zone may be at design conditions 8202327 *? , - 66 - are regulated, that is, in the range of about 0.5-1.7.

The operation of the system when using only the annular section of the burner is similar to that described above in connection with the central section of the burner. The portion of the slurry feed stream in line 44 is pumped into reaction zone 31 of synthesis gas generator 41 by positive displacement pump 55 provided with speed control 56, line 57, flow meter and transducer 58, line 59, valve 76, lines 60 and 16, inlet 29 of burner 1, annular manifold 28, and annular tube bundle 7.

The flow rate of the slurry through line 44 is controlled by the speed of positive displacement pump 55. To phase out the slurry flowing through line 44, this speed is continuously decreased from maximum to zero over a period in the range from about 1-3600 seconds, such as about 60-1800 seconds, for example about 300-1000 seconds. Flow recorder controller with transducer 61 comprises a microcomputer programmed with the desired time versus decreasing flow rate curve. The flow rate of the slurry in line 57 is measured and a signal d is provided by flow transducer 58 corresponding to the flow rate of the slurry in line 44. Flow recorder controller 61 receives signal vd, compares it with a signal that the desired represents speed at that time, and provides a corresponding control signal to speed controller 56 about the speed of pump 55. lower so that the charge slurry flowing in line 30 59 assumes a given reduced flow rate for that instant in the phase-out period. The new suspension rate is measured and the cycle is repeated. Repeated flow rate controls are made by these means and the slurry flowing in line 60 is dephased.

Simultaneously with the phase-out of the portion of the slurry of the main fuel flowing in line 44, the portion of the reserve liquid hydrocarbon fuel flowing in line 162 is phase-shifted over 8202327 - 67 - the same time period. Flow recorder controller with transducer 172 includes a microcomputer programmed with the desired time versus increasing flow rate curve. The flow rate of oil in line 162 is measured and a signal q is provided by flow transmitter 168 corresponding to the flow rate of the oil in line 162. Flow register add-on controller 172 receives signal q, compares it with a signal that the desired represents flow rate at that time, and provides a corresponding control signal 10 to valve 164 to open wider so that the oil charge in line 169 assumes a given increased flow rate for that instant in the phase-in phase. The new oil / :: ·. speed is measured and the cycle is repeated. By these means, repeated controls of the flow rates of the main and reserve fuels are made so that the oil flowing in line 170 in line 16 can be phased in an amount that reduces the reduced amount of solid carbonaceous fuel slurry contained in line 60 flows compensates. During or during the period when the portion of the slurry of the main solid carbonaceous fuel of line 44 is phase-out and the part of reserve liquid hydrocarbon fuel of line 162 is phase-out, the weight ratio of temperature moderator to fuel in the reaction zone may be 25, for example, on design conditions, or near / constant, i.e. less than + 10% variation due to increasing or decreasing flow rate of the temperature moderator. Accordingly, in the present example, an additional amount of H 2 O from external source can be phased over the same period of time simultaneously with de-phasing of the carbon water slurry. Thus, in FIG. 4, a portion of the steam in line 180 is passed through line 182 and phase-added in line 17 where it mixes with the free oxygen-containing gas from line 73. Flow recorder-35 controller with transmitter 192 includes a microcomputer is programmed with the desired time versus increasing flow rate curve.

The flow rate of the steam in line 182 is measured and a signal t is provided by flow transducer 188 8202327 -68 - corresponding to the flow rate of steam in line 182. Flow recorder controller 192 receives signal t, compares it with a signal that represents desired flow rate at that time, and provides a corresponding control signal to valve 184 to open wider so that the steam charge in conduit 189 assumes at that increased flow rate for that time in the phase-in phase.

The new speed of the steam is measured and the cycle is repeated. By these means, repeated adjustments of the flow rate of the steam are made, and the steam flowing in line 190 is phase-fed into line 17 in an amount that is the weight ratio of E2 O to (fuel in the reaction zone at design conditions) will maintain.

In another embodiment, the weight ratio H 2 O / fuel in the reaction zone is controlled up and down by controlling the steam velocity as described above to achieve a desired temperature in the reaction and a desired composition of the product gas. 20 obtain.

At the same time as or after the phase-out of the main fuel, the phase-in of the spare fuel, and possibly with or without the phase-in or phase-out of the steam depending on the nature of the fuel, 25 free oxygen-containing gas can be regulated up or down to control the temperature in the reaction zone, for example, on design conditions, or almost constant i.e. less than + 95 ° C variation. Thus, in the present example, in Fig. 1, a portion of the free oxygen-containing gas in line 62 is passed through line 64 and phaseed into line 17 where it mixes with steam, if any, from line 190 as described above.

• 4

The flow recorder controller with transducer 75 comprises a microcomputer programmed with the desired time versus flow velocity curve. The adjustment period is the same as that for the fuel and fuel flows. The control of the oxygen flow rate may be up and down depending on the nature of the fuel flows and the addition of steam, if any. In the present example, the flow rate of the oxygen will increase to meet the additional requirements for partial oxidation of a liquid hydrocarbon as compared to a solid carbonaceous fuel. The velocity of free oxygen-containing gas in line 64 is measured and a signal e is provided by flow transmitter 71 corresponding to the flow rate of the free oxygen-containing gas in line 64. Flow register controller 75 receives signal e, compares it with a signal representing the desired flow rate for that instant, and provides a corresponding control signal to valve 66 to open wider so that the charge of oxygen-containing gas in line 72 gives a given increased flow. speed for that instant in the phase-in period. The new rate of the free oxygen-containing gas is measured and the cycle is repeated. Through . these means are repeated adjustments of the flow rate of the oxygen and the free oxygen-containing gas flowing in line 73 is phased in line 17 in an amount which will maintain the temperature in the reaction zone 20 almost constantly.

In another embodiment, the gas velocity of the free oxygen-containing gas is controlled up or down to obtain the desired temperature in the reaction zone and a desired composition of the product gas. Alternatively, by the means described above, the atomic ratio of oxygen to carbon in the reaction zone can be controlled at design conditions, i.e., in the range of about 0.5-1.7.

The aforementioned time versus flow rate curves for programming flow controllers 191, 192, 171, 172, 51, 61, 74, and 75 can be determined by conventional calculations based on heat and weight balances for the entire system.

In another embodiment, the parameters for said calculations and others may be measured by conventional detectors and the corresponding signals may be applied to total controllers or computer 40. Input to flow control means 40 may be manual or with a signal of a computer, analyzer, or scanner, 8202327 / - 70 - tt

Controllers 4Q include conventional circuitry and components for providing signals, i.e. pneumatic or electronic, to operate said speed controllers and valves.

In controller 40, the computer-computed or manually input determined points for the desired flow rates at specific times for the different flows are compared with the signals a, d, respectively; s, t; m, q; and b, e. For example, in response to signal 10 or signals a and / or d, controllers 40 can automatically control pump speed controller or members 46 and / or 56 by transmitting signal or signals c and / or f to flow registers, strokes, respectively. control member or control members 51 and / or 61. Otherwise, signal or signals c and / or f may be directly applied to speed control member or members 46 and / or 56, respectively. Signals i and / or g from controller 40 can be used to close solid carbon fuel slurry valves 77 and / or 76, respectively. In another embodiment, flow recorder control 20 means 51 can receive signal a from transducer 48 and calculate signal c from control 40 and the speed control signal for the operation of speed control 46.

In such a manner, in response to signal or signals s and / or t, controller 40 can automatically control steam valve or valves 183 and / or 184 by transmitting. signal or signals u and / or r to current recording device controller or members 191 and / or 192, respectively.

In such a manner, in response to signal or signals m and / or q, controller 40 may automatically control valve 3O or valves 163 and / or 164 for liquid hydrocarbon fuel by transmitting signal or signals w and / or x, respectively, to flow recorder controller or organs 171 and / or 172.

Also, in such a manner, responding to signal or signals b and / or e, controller 40 may automatically control valve or valves 65 and / or 66 for free oxygen-containing gas by transmitting signal or signals j and / or h resoective. similar to flow recorder control member or means 74 and / or 75.

8202327 V τ - 71 -

Fig. 5 is a vertical longitudinal schematic representation of another embodiment of the present two-section burner. Two pre-mixing chambers in series are located in a the central conduit in the central section and also in the annular passage in the annular section. The ends of the central tube bundle in the central section and the annular tube bundle in the annular section are withdrawn upstream from the front face of the burner. In Fig. 5, burner 80 comprises central conduit 81 which partly forms wall 82 between central passage 83 and coaxial radial spacing annular passage 84, two rows of a central bundle of parallel tubes 85 longitudinal.

. ., pass through the upper portion of the central passageway 83 and have upstream ends 86 which pass through tube sheet 87 and form a gastight hermetic seal therewith, and downstream ends 88 which are retracted upstream from outer surface 89 at the downstream end of burner 80, coaxial concentric radially spaced outer conduit 90 surrounding said annular passageway 84 along its length, two rows of an annular bundle of parallel tubes 85 passing longitudinally through annular passageway 84 with upstream ends 96 passing through tube sheet 97 and which thereby form a gas-tight seal and which have downstream ends 98 which are withdrawn upstream from outer surface 89, annular manifold 100 in communication with the upstream end 96 of said annular bundle of tubes 95, manifold 101 which may be cylindrically formed in connection to the top ends 86 of said c entral beam tubes 85, inlet means 102 for introducing a first feed stream into said central manifold 101, inlet means 103 for introducing a second feed stream into said central passageway 83 and in the gaps surrounding said central beam tubes 85, inlet means 104 for introducing a third feed stream into said annular manifold 100, inlet means 105 for introducing a fourth feed stream into said annular passage 84 and into the gaps surrounding central bundle tubes 95, cooling hoses 106 encircle the outer diameter of outer conduit 80 along its length, and 8202327 X-72 hollowed cooling chamber 107 at the downstream end of the burner.

Disc-shaped central tube late 87 closes central passage 83 below its upstream end. In such a manner, annular tubular plate 87 closes annular passage 84 below its upper end. Conventional means, ie, welding, twisting, crimping / threading, rolling, can be used to provide a pressure and gas tight hermetic closure or connection wherein the central and annular tube bundles penetrate the respective tube plates. Mechanical pressure fittings and torque accessories can also be used.

(.., Plate 108 which may be disc-shaped seals the top end of central conduit 81. The space between plate 108 15 and tubular plate 87 forms said central manifold 101.

By these means, for example, a portion of a first reactant feed stream into feed line 102 can be introduced into central manifold 101 and then split into several streams passing through tube sheet 87 and individual tubes of central beam 85. Annular disc 119 closes the top end of annular passage 84. The space between annular disc 109 and annular tubular plate 87 forms annular manifold 100. Simultaneously and concomitantly with the introduction of the first reactant feed stream, the third reactant feed stream in feed line 104 can be fed into annular manifold 100 split into several streams which pass through tube plate 97 and the individual tubes in annular bundle 95.

Wall arms or tube spacers 115 hold the individual tubes in annular tubes bundle 95 in a fixed parallel non-touching relationship to each other, the inside of outer conduit 90, and the outer diameter of central conduit 81. In this manner, wall arms or tube. spacers 116 the individual tubes in central tubes 35 bundle 85 in a fixed parallel non-touching relationship to each other and the inner diameter of central conduit 81. While the pre-mixing zones shown in the embodiment in FIG. 5 provide two separate coaxial centers for -mix- * 8202327 V f - 73 - include chambers 117 and 118 in series in central conduit 83, and two separate coaxial annular premix chambers 119 and 120 in series in annular passage 84, the premix zone of other embodiments of the the present invention actually comprises 6βη or more, such as 2-5 coaxial central and / or annular premixing chambers. Each central premix chamber, except for the first chamber in the line, includes a coaxial cylindrical body portion 121 followed by a coaxial at least partially converging frusto-conical outlet portion 122 which optionally changes to a normal cylindrical portion 123. This outlet portion is shown in FIG. 5 as a converging central nozzle 124 which, ". ends at the downstream outer surface of the burner.

Optionally, nozzles 124 and 133 to be described below may be made of a heat and wear resistant material, ie silicon carbide or tungsten carbide.

The first central premix chamber in line may have a straight coaxial cylindrical body portion 125 which discharges through circular opening 126 directly into the aligned central coaxial premix chamber 118. Preferably, the inlet of the first central premix mixing chamber 117 part of a converging frusto-conical shaped section 127.

Each of the coaxially annularly shaped premixing chambers 120 except for the first annular chamber 119 comprises a co-axially developed normally cylindrical annular body portion 130 formed by a coaxially developed at least partially converging frusto-conically shaped annular outlet portion 131 which may optionally transition into a coaxially developed normally cylindrical annular portion 132. This outlet portion is shown in Figure 5 as a converging annular outlet nozzle 133 terminating at the downstream surface of the burner. The first coaxial annularly formed premix chamber 119 comprises a coaxially developed normally cylindrical annular body portion 134 which discharges through annular opening 135 into the aligned coaxially annularly shaped premix chamber 120. Preferably, the inlet comprises the first annular premix chamber. 119 part of a coaxially developed converging frusto-conical shaped section 136.

1 8202327 (i - 74 -

Pierced front face plate 107 includes a front portion 137 at the extreme end of the burner, which may be flat or curved, and which includes a coaxial central annular cooling chamber 138 surrounding the central conduit outlet nozzle 124 and / or a coaxial / radial spaced annular cooling chamber 139 surrounding said annular outlet nozzle 133 at the end of the burner. The cooling chamber may be connected to the otherwise flat burner end as shown in Fig. 4, or may be an extension of the central and outer conduits. Cold cooling water in line 140 enters the annular cooling chamber 139, distributes by baffles and flows about 180 ° and is discharged through an outlet on the opposite side connected to outer coils 106. Cooling water 15 is introduced into the central annular cooling chamber 138 by means of pipe 145 which is connected to pipe 146 which extends longitudinally downwards through wall 82 in central pipe 81. The cooling water distributes by means of baffle plates, flows about 180 ° all around central cooling channel 138, and is drained through an opposing coaxial longitudinal passage (not shown) similar to passage 146 but at a different location in wall 82.

Optionally, a gaseous feed stream selected from the group consisting of steam, free oxygen-containing gas, CO2, N2, fuel gas, recycled portion of product gas, and mixtures thereof, may be introduced into at least one of the central and / or annular premixing chambers by means of at least one inlet tube 149 which. is connected to at least one longitudinal passage 147 in wall 82 of central conduit 81, and at least one branch passage 148 connecting longitudinal passage 147 to said premixing chambers.

While the central beam tubes 85 and the annular beam tubes 95 in FIG. 5 are drawn to include several parallel tubes, in another embodiment of the burner shown in FIG. 5 of patent application Serial No. 212,054 filed in U.S. Patent and Trademark Office on December 3, 1980, which issued French Patent Application No. 8027516, and which are incorporated herein by reference, the central and annular tubular bundles are helically formed,

Although modifications and variations of the invention can be made without departing from the spirit and scope thereof, only such limitations should be imposed as set forth in the accompanying claims.

✓ (.

\ 8182327

Claims (10)

1. A method of preparing gaseous mixtures. comprising H2, CO, CO2, entrained particulate carbon, and at least one group material consisting of Η2 <3, Njr 5 H2S, COS, CH4, Ar, and ash, in a free-flow permitting gas generator for non-catalytic partial oxidation comprising using a one or two section burner having at least a first fluid conduit or group of conduits to provide a first fluid passage or passages, and at least one related radially spaced second fluid conduit surrounding the first fluid line or group of lines to provide at least one annular (second fluid passage therebetween) and having either a central or central and annular outlet opening 15 at the end of the burner, and switching a reactant feed stream to another without shutdown or pressure relief of the system, which method is characterized by the combination of the steps of: (1) letting depositing a first reactant stream of first slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with a temperature moderator through at least one of said first or second fluid passages; (2) simultaneously passing a separate reactant stream of free oxygen-containing gas, whether or not mixed with a temperature-moderating gas, through the unused passageway or passageways in said burner associated with a passageway through which said first reactant stream flows in (1): 30 (3). mixing said reactant streams from (1) and (2) together to form a well-distributed mixture, and reacting said mixture by partial oxidation in the reaction zone of said gas generator at an autogenous temperature in the range of about 925 ° -35 1925 ° C, a pressure in the range of 1 - 300 atmospheres, an atomic ratio of oxygen / carbon in the range of about 0.5-1.7, and a weight ratio H 2 O / fuel in the range - ; * from about 0-5.0; (4) phase-out the fluid passage or 8202327. -3F- "passages in which said stream of said first slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with a temperature moderator, flows in said burner, which is phase-out with a uniformly decreasing flow rate which varies from maximum to zero over a time period in the range of about 1-3600 seconds; and simultaneously phasing said flow of second slurry of solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with temperature moderator, in the same flute passage in said burner with a uniformly increasing flow rate ranging from zero to maximum speed over the same time period, and het mixing the phase-streamed stream with the remainder of said first slurry of solid carbonaceous fuel or hydrocarbon fuel stream, whether or not mixed with a temperature moderator flowing therein; and (5) controlling the flow rate of the reactant stream of free oxygen-containing gas, whether or not mixed with a temperature moderator, passing through the burner and introducing additional H 2 O into the reaction zone, if necessary, to adjust the free oxygen / carbon atomic ratio and the H 2 O / fuel weight ratio in the reaction zone at design conditions for the partial oxidation reaction. (, 2. Process according to claim 1, characterized in that in step (5) the temperature in the reaction zone is kept almost constant and the weight ratio H 2 O / fuel is maintained in the range of about 0.1-3.0. A method according to claim 1 or claim 2, characterized in that said hydrocarbon fuel is a pumpable suspension of a solid carbonaceous fuel in a liquid carrier of the group consisting of water, liquid hydrocarbon fuel, and mixtures thereof. Process according to claim 3, characterized in that said solid carbonaceous fuel is selected from the group consisting of carbon, lignite, carbon coke, carbonized carbon product, coal liquefaction residues, particulate carbon, petroleum coke, solid materials derived 8202327 -78 - * t 'from oil-containing slate, tar sand and pitch, concentrated sewage sludge, rubbish, rubber, and mixtures thereof. A method according to any one of claims 1 to 4, characterized in that said burner includes a section with the first 5 fluid conduit withdrawn upstream from the front face of the burner by a distance of about 3-10 times the minimum diameter from the central outlet at the end of the burner to provide a premix zone. A method according to claim 5, characterized in that said pre-mixing zone comprises 2-5 cylindrical shaped pre-mixing chambers in series. A method according to any one of claims 1 to 4, characterized in that said burner comprises two sections with the first fluid group of conduits in the first section comprising a bundle of parallel tubes whose downstream ends are upstream. withdrawn from the front face of the burner by a distance of about 0-12 times the minimum diameter of the central exit orifice at the tip 20 of the burner, and the first fluid group of conduits in the second section comprises an annular bundle of parallel tubes whose downstream ends are withdrawn upstream of the front face of the burner by a distance of about 0-12 times the minimum width of the annular exit nozzle at the end of the burner. . . A system for controlling the introduction of various reactant streams into the reaction zone of a gas generator for partial oxidation, characterized by: a burner comprising at least a first fluid conduit or group of conduits about a first fluid passage or passages and a second provide fluid conduit surrounding each of said first fluid conduit or group of conduits to define a second fluid passage therebetween; two af-. separate burner inlet lines connected to each of said first fluid line or lines and to each of said second fluid line, respectively; conduit members comprising four feed lines for connecting four different material feed streams to said two burner inlet lines for introducing said feed streams into the burner, a respective pair of said feed lines being connected to each burner inlet- conduits which burner drains said feed streams or mixtures thereof into said reaction zone; a separate flow rate sensor and a separate flow rate controller in each of said supply lines for independently sensing the flow rate for each material flowing through a given supply line and providing a signal corresponding to the actual flow rate for that supply flow; and a controller for receiving said signals from said flow rate sensing means and comparing each actual flow rate / signal with a manually or automatically calculated and input input signal that determines the desired flow rate or determined. represents a point at that time for each supply current and provides a corresponding control signal for separately operating the flow rate controller in that particular supply line, and independently controlling the flow rate for each supply stream entering burner 20 at that time so that a supply current in each pair of supply currents is out of phase with a uniformly decreasing flow rate ranging from maximum to zero over a period of time in the range of about 1-3600 seconds? and at the same time, a different feed current is phase-wise in the same feed line with a uniform feed. increasing flow rate ranging from zero to maximum speed over the same time period. A control system according to claim 8, characterized in that the first feed stream comprises steam, the second feed stream comprises a liquid or gaseous hydrocarbon fuel, the third feed stream comprises a pumpable suspension of solid carbonaceous fuel, and the fourth feed stream contains a free oxygen-containing gas and each flow rate control means for independently controlling the flow rate of the first, second, and fourth feed streams is a flow control valve, and the flow rate control means for independently controlling the flow rate of the third feed flow is a pump whose speed is controlled. 10. Process for the preparation of gaseous mixtures 8202327 ♦ * -80 - comprising H2, CO, CO2 entrained carbon particles, and at least one material from the group consisting of H20, H2 · H2S, COS, CH4, Ar, and ash, free-flow permitting gas generator by non-catalytic partial oxidation, characterized in that for starting and operating the gas generator using a two-section burner with a central section and an annular section with two separate fluid passages in each section, and switching from one reactant feedstream to another without shutting down the system or releasing the pressure, the method comprises the following steps: (1) passing a first reactant.. flow of gaseous or liquid hydrocarbon fuel, whether or not mixed with H 2 O, through the first or second fluid passage in the central section of said burner, and / or at the same time a second reactant stream of gaseous or liquid hydrocarbon fuel, whether or not mixed with H 2 O, through the third or fourth fluid passage in the annular section of said burner; (2) simultaneously passing a separate reactant stream of air, whether or not mixed with H 2 Q, through the unoccupied fluid passage in each of the central and / or annular sections of said burner, which is in communication with said fluid passages through which said stream or streams of first gaseous or liquid hydrocarbon fuel, whether or not mixed with H 2 O, pass; (3) mixing said reactant streams from (1) and (2) together to obtain a well-distributed mixture, and burning said mixtures by almost complete combustion in the reaction zone of said gas generator at a temperature in the range of about 1095 ° -2480 ° C and a pressure in the range of about 0.5-300 atmospheres? (4) dephasing the fluid passage in which said central and / or annular section or sections flows said stream or streams of first gaseous or liquid hydrocarbon fuel, whether or not mixed with H 2 O, which is out-of-phase with a uniformly decreasing 8202327 * m -8t - flow rate ranging from maximum to zero over a time period in the range of about 1-3600 seconds; simultaneously phasing said stream or streams of the slurry of the main solid carbonaceous fuel or hydrocarbon fuel, whether or not mixed with H 2 O, in the same flute passage with a uniformly increasing flow rate ranging from zero to maximum speed over the same time period and mixing with the remaining part of and replacing the phase-out part of said stream of slurry of first solid carbonaceous fuel or hydrocarbon fuel / whether or not mixed with H 2 O flowing therein; simultaneously phasing out (kiri) the fluid passages in which in said central and / or annular section or sections said stream or streams of air, whether or not mixed with H 2 O, flows, which phase-out takes place with a uniformly decreasing flow rate varying from maximum to zero over a period of time in the range of about 1-3600 seconds; and simultaneously phasing a replacement flow or flows of free oxygen-containing gas, whether or not mixed with H 2 O, in the same flute passage with a uniformly increasing flow rate ranging from zero to maximum speed over the same period of time and mixing with the remainder of and replacing the phase-out portion of said stream of air, whether or not mixed with HoO, flowing therein; and / z V '(5) controlling the flow rate or rates of the reactant stream or flows of free oxygen-containing gas, whether or not ni et mixed with H 2 O, passing through the burner, and introducing additional into the reaction 30 zone if necessary to adjust the free oxygen / carbon ratio and the H 2 O / fuel weight ratio in the reaction zone to design conditions for partial oxidation . 8202327