CN102352268A - Method for producing synthesis gas by using coal powder as raw material - Google Patents
Method for producing synthesis gas by using coal powder as raw material Download PDFInfo
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- CN102352268A CN102352268A CN2011102649376A CN201110264937A CN102352268A CN 102352268 A CN102352268 A CN 102352268A CN 2011102649376 A CN2011102649376 A CN 2011102649376A CN 201110264937 A CN201110264937 A CN 201110264937A CN 102352268 A CN102352268 A CN 102352268A
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Abstract
The invention discloses a pressurization high temperature gasification method of dry coal powder. The method comprises the following five steps: the preparation of dry coal powder, the pressurization delivery of the dry coal powder, the pressurization and high temperature gasification of the dry coal powder, the cooling of high temperature crude synthesis gas and molten ash and the washing and purifying of the crude synthesis gas, and the treatment of water containing fine ash. The method is suitable for not only the bituminous coal with low ash content and low ash fusion point, but also other types of coal, which widely exist at home and abroad, have different metamorphic degrees and qualities and contain the coal with low ash content and high ash fusion point, the coal with high ash content and low ash fusion point and the anthracite, bituminous coal and lignite with high ash content and high ash fusion point. The method has good gasification index, simple equipment, flexible process configuration, low investment and operation convenience, the large-scale product is easy to realize, and the method has the beneficial effects of wide raw material application range, environmental friendliness and the like.
Description
[technical field]
The invention belongs to the technical field of coal high-efficiency clean utilization, more specifically, the present invention relates to the method that a kind of dry coal dust pressurized high-temperature gasification prepares synthetic gas.
[background technology]
As everyone knows, in world's fossil energy reserves, oil, Sweet natural gas and coal etc. contain hydrocarbon material and account for sizable ratio, and the coal carbon source accounts for the exhausted vast scale of hydrocarbon resource.Realize that the cleaning of coal, the efficient utilization have great reality and strategic importance.Realize the utilization of resource clean and effective with the gasification mode; Development in recent years rapidly; Avoided the direct incendiary heat energy utilization of coal rate not high, and produced problems such as a large amount of greenhouse gases and solid dust, the ecotope of having contained earth crisis is already further polluted and is destroyed.The present invention is primarily aimed at the pressurized high-temperature gasification of dry coal dust, and clean and effective utilizes coal resources.
Gasification technology is through constantly development is perfect, and entrained flow bed gasification technology is good owing to its gasification index, efficient energy-saving, environmental benefit are obvious receives the favor of numerous manufacturers.Entrained flow bed gasification technology has dry method pressurized gasification technology and wet method pressurized gasification technology at present.Wet method gasifies the ash fusion point of coal, ash oontent etc. is had relatively high expectations, and owing to have a large amount of liquid waters in the feed stock for blast furnace, has influenced the efficient of gasification, has reduced gasification index, has lost part material and oxygen.The dry method gasification index is better, and cold gas efficiency is higher, but because technical difficulty is bigger, most domestic dry method gasification installation all is in the stage of fumbling.
The present invention is directed to the domestic and international energy and gasification technology present situation; Be badly in need of a kind of development trend of efficient, advanced, stable dry coal dust pressurized high-temperature gasification technology according to the derived energy chemical field, on the basis of carrying out a large amount of research work and long-term Coal Gasification Technology research and development, made the present invention.With dry coal dust is raw material, through pulverized coal preparation, positive delivery, High Temperature High Pressure gasification, generates with CO, H
2And CO
2Be synthetic gas, reducing gas or the fuel gas of main ingredient, thereby realize the effective utilization of (containing low grade coals such as high ash, high-ash-fusion coal) of various coal resources.Owing to be that dry coal dust directly sprays into vapourizing furnace, vaporized chemical adopts air, oxygen-rich air, pure oxygen, CO
2Or superheated vapour; The vapourizing furnace service temperature is higher, therefore can realize that the vaporized chemical consumption is lower, and cold gas efficiency is higher, and feed stock conversion is high, and gasification index is better.
[summary of the invention]
[technical problem that will solve]
The purpose of this invention is to provide a kind of is the method for raw material production synthetic gas with dry coal dust.
[technical scheme]
The objective of the invention is to realize like this: this method comprises dry pulverized coal preparation; Dry coal dust positive delivery; Dry coal dust high-temperature pressurizing gasification, the cooling of high temperature crude synthesis gas removes lime-ash with the cooling of bubbling cooling bath, and crude synthesis gas cooling dedusting is with washing, purifying and contain six parts of thin grey water handing.
The present invention relates to a kind of is the method for raw material production synthetic gas with the coal dust.
The method that with the coal dust is the raw material production synthetic gas comprises the steps:
The preparation of A, dry coal dust: coal raw materials is removed irony class impurity wherein through tramp iron separator 2; By belt weighing feeding machine 3 Weighings; Get into crusher 4 broken coal-forming grains; Described coal grain is promoted to feed bin 6 through bucket elevator 5; Quantitatively send into grinding machine 8 by feeding machine 7 again and grind to form coal dust; When grinding, allow the hot blast of hotblast stove 1 and described coal dust carry out abundant heat exchange, make its coal dust be dried to water content by weight≤2.0%; Described coal dust drives at hot blast and gets into powder selector 9 down, and wherein 100% coal dust of granularity＜0.10mm drives entering powder collector 10 down at hot blast, and all the other coal dusts dependence self gravitations than volume particle size return grinding machine 8 and grind; Described powder collector 10 is connected with induced draft fan 12, under the effect of induced draft fan 12, removes the steam of the water that dry hot gas and coal in the powder collector 10 discharge; Described powder collector 10 is provided with fly-ash separator 11 at the top, to reduce the dust content of discharging the gas from powder collector 10; The dry coal dust of discharging from powder collector 10 bottoms is sent into follow-up workshop section and is handled;
B, dry coal dust positive delivery: the dry coal dust by above-mentioned steps A preparation passes through pipe-line transportation in coal dust warehouse 14, is transported to fine coal positive delivery device 16 through valve 15 then; Both difference of altitude of said coal dust warehouse 14 and said fine coal positive delivery device 16 are the 10-30% of said coal dust warehouse 14 height, are 0.10MPa at least with the intake pressure that guarantees fine coal positive delivery device 16; Drive fine coal positive delivery device 16 through electric motor M then dry coal dust pressure brought up to 0.5-7.0MPa, again through pipe-line transportation to hopper 17; Described coal dust is transported to vapourizing furnace 33 through hopper outlet valve 19 after measuring through electronic scales 18; The dusty gas of discharging from coal dust warehouse 14 is discharged into atmosphere through cyclonic separator 13 gas separated from cyclonic separator 13 tops, and solid returns the recycle of coal dust warehouse.
Perhaps send into normal pressure powder storehouse 21 by the dry coal dust of above-mentioned steps A preparation, when the pressure in normal pressure powder storehouse 21 reached balance with the pressure of locking gas hopper 23, dry coal dust got into lock gas hoppers 22 through normal pressure powder storehouse 21 bottom valves 25; When the material level of lock gas hopper 22 reaches predetermined material level value; Close normal pressure powder storehouse 21 bottom valves 25; Fill high-pressure inert gas toward lock gas hopper 22 then; When the pressure of the pressure of locking gas hopper 22 and feeder 23 reaches balance; Open lock gas hopper 22 bottom valves 26; Dry coal dust gets into feeder 23 through this valve 26; Carrier gas by the input of feeder 23 bottoms makes the dry coal dust fluidisation that gets into feeder 23; The fluidized drying coal dust is discharged from feeder 23 tops, delivers to vapourizing furnace 33 through pipeline; When lock gas hopper 22 material levels are lower than predetermined material level value; Lock gas hopper 22 bottom valves 26 are closed; The discharge degree that to lock gas hopper 22 through pipeline is to cyclonic separator 20; When the pressure of lock gas hopper 22 is reduced to normal pressure; Open normal pressure powder storehouse 21 bottom valves 25; Allow normal pressure storehouse 21 interior dry coal dusts get into lock gas hopper 22, continue the recycle feed program; The dusty gas of being discharged by normal pressure powder storehouse 21, lock gas hopper 22 carries out gas through cyclonic separator 20 to be separated with solid, and gas separated is discharged into atmosphere from cyclonic separator 20 tops, and solid separated is returned the storehouse recycle of normal pressure powder through returning valve 24;
The pressurized high-temperature gasification of C, dry coal dust: the dry coal dust that above-mentioned steps B obtains is delivered to multithread road spraying burner 32 inlets that are positioned at moisture-free coal powder pressure gasifying stove 33 tops and passed through it; Spraying burner 32 outlets in the multithread road; Vaporized chemical through multithread road spraying burner 32 is sprayed onto dry coal dust in the reaction chamber 34 of moisture-free coal powder pressure gasifying stove 33; And make its vaporized chemical and dry coal dust under the condition of 1350 ℃-1600 ℃ of temperature and pressure 0.1～6.0MPa, carry out combustion reactions, generate and contain CO, H
2And CO
2Be the high temperature crude synthesis gas of main ingredient and the mixture of molten ash;
Described multithread road spraying burner 32 is the coaxial textural association equipment that is nested of a kind of multitube, and it is made up of central duct 63, cooling medium channel 64, vaporized chemical medium channel 66 and dry coal dust passage 65; This multithread road spraying burner 32 is provided with a cooling system, and this cooling system is made up of with pump 30 cooling trough 28, cooling tube 29; Be contained in water in the cooling trough 28 after cooling tube 29 cooling; Again through pump 30 pressurized stream through the multithread road spraying burner 32; Make the temperature of multithread road spraying burner 32 keep stable; Spraying burner 32 effusive water return cooling trough 28 again from the multithread road, through recycling after 29 coolings of the water-cooled tube in the cooling trough 28;
Described moisture-free coal powder pressure gasifying stove 33 is cylindrical tubes, and the top of this vapourizing furnace is reaction chamber 34, and the bottom is a quenching cooling chamber 35; Reaction chamber 34 comprises furnace roof inlet 36, burner hearth 37, around the water-cooled coil pipe 38 of burner hearth, the refractory masses 39 and vapourizing furnace shell 40 of protection water-cooled coil pipe; Furnace roof inlet 36 is connected with said multithread road spraying burner 32; Described quenching cooling chamber 35 is provided with water distributor 41, sending down abnormally ascending pipe 42 and riser 43; Sending down abnormally ascending pipe 42 upper ends are connected fixing with water distributor 41; Riser 43 is supported on quenching cooling chamber 35 housings; Sending down abnormally ascending pipe 42 and riser 43 arranged concentric; An annular space is arranged between the two, and be fixed together with preset pieces 44;
D; The high temperature crude synthesis gas; Molten ash cooling and crude synthesis gas washing, purifying: in quenching cooling chamber 35; The high temperature crude synthesis gas and the molten ash mixture that allow step C obtain mix and cooling with the water coolant that gets into bubbling cooling bath 45 through sending down abnormally ascending pipe 42 that is got into by said water distributor 41; The cinder slag is deposited in quenching cooling chamber 35 bottoms because of sudden cold-curing; The crude synthesis gas that contains a small amount of thin ash and water rises along the annular space between sending down abnormally ascending pipe 42 and the riser 43; In the annular space upper end; A part of water that said crude synthesis gas contains turns back in the bubbling cooling bath 45 along sending down abnormally ascending pipe 42 inwalls with thin ash, and remaining crude synthesis gas goes out vapourizing furnace 33 through row of conduits; Cinder slag in quenching cooling chamber 35 bottoms gets into lock bucket 47 through lock slag valve 46, discharges through vent valves 48, and the water that contains thin ash that the cinder slag is carried secretly is delivered to the vacuum evaporator 69 of water treatment portion;
The crude synthesis gas that contains thin buck of discharging from vapourizing furnace 33 perhaps gets into air water separator 51; The water that synthetic gas is carried secretly is through after separating; And further remove the thin buck of carrying secretly in the raw gas that contains through baffle plate 52; These contain thin buck sends to through pipeline after reducing pressure and carries out thin grey water handing, removes the crude synthesis gas that contains thin buck and delivers to through pipeline and soak into washer 53; Perhaps the crude synthesis gas that contains thin buck of discharging from vapourizing furnace 33 is directly delivered to through pipeline and is soaked into washer 53; In soaking into washer 53; Allow the crude synthesis gas that contains thin buck and buck thorough mixing from gas wash tower 54; Get into gas wash tower 54 through pipeline then; Arriving bubbling style water-bath storage tank 60 along downtake 58 again washs; Said crude synthesis gas rises along the annular space that between downtake 58 and upcast 59, forms again; And carry out multistage washing through traverse baffle 57, tower tray 56, eddy flow plate 55; Discharge along pipeline from gas wash tower 54 tops through scum dredger 27 backs, obtain a kind of synthetic gas; Buck in the bubbling style water-bath storage tank 60 gets into grey water-circulating pump 49 through pipeline; Separated into two parts behind grey water-circulating pump 49 pressure-raisings; A part is sent into along pipeline and is soaked into washer 53, and the water distributor 41 that another part is sent into dry coal powder pressure gasifying stove 33 cinder notch below through pipeline is used as water coolant;
E, contain thin grey water handing: gas wash tower 54 bubbling style water-bath storage tanks 60 bottoms contain thin buck and contain thin buck through Liquid level adjusting valve 50 decompressions through what Liquid level adjusting valve 61 decompressions, quenching cooling chamber discharged; Contain thin buck and get into high-temperature water heater 67 and carry out the step-down cooling with decompression back air water separator 51 is isolating, get into buck heating devices 83 from high-temperature water heater's 67 top escaping gas and reclaim heats; The thin buck that contains of discharging from high-temperature water heater 67 bottoms gets into secondary step-down transformer 68 recovery heats; The steam of overflowing from secondary step-down transformer 68 tops gets into degasification water pot 75 and reclaims heat, and the thin buck that contains of discharging from secondary step-down transformer 68 bottoms gets into vacuum evaporator 69 step-downs cooling; After the 77 cooling coolings of negative pressure condenser, get into negative pressure separator 78 from vacuum evaporator 69 top escaping gas; Gas gets into off-gas pump 80 after baffle plate 79 separates moisture; Again through 81 gas-liquid separations of off-gas pump separator; Gas emptying after baffle plate 82 separates moisture; Off-gas pump separator 81 isolating water and negative pressure separator 78 isolating water flow into aqua storage tank 73, and the thin buck that contains of discharging from vacuum evaporator 69 bottoms gets into clarification separate tank 71 behind clarification separate tank feeding pump 70 pressure-raisings; In clarification separate tank 71, add the water treatment organic polymer coargulator and make thin grey suspended substance flocculation; The top overflow water of clarification separate tank 71 flows into aqua storage tank 73; The buck of aqua storage tank 73 part behind grey water pump 74 pressure-raisings is sent into degasification water pot 75, and a part is as wash-down water, and few part effluxes; Buck in the degasification water pot 75 is through the gas that adds heat extraction and wherein carried secretly and drain, simultaneously 75 outlets of degasification water pot or degasification water pot 75 in the adding dispersion agent, to alleviate the fouling of interchanger and ash-water pipeline; The degasification buck is gone into buck heating device 83 through degasification water pump 76 pressure-raisings are laggard, heats up again with from high-temperature water heater's 67 top escaping gas heat exchange, and the bubbling style water-bath storage tank 60 of delivering to gas wash tower 54 then recycles; Clarification separate tank 71 bottom ash contents higher thin buck gets into vacuum band-type filter machine 72 and carries out separating of thin ash and water after 87 superchargings of filter feeding pump, described thin ash is collected the back and discharged, and isolating water turns back to again to be clarified in the separate tank 71.
A preferred embodiment of the invention, described coal raw materials are selected from hard coal, bituminous coal, brown coal or thermal value Q
B.adOther carbon solid raw material of＞17000kJ/kg.
According to another kind of preferred implementation of the present invention, described vaporized chemical is selected from air, oxygen-rich air, pure oxygen, CO
2Or superheated vapour.
According to another kind of preferred implementation of the present invention, described vaporized chemical and dry coal dust carry out combustion reactions under the condition of 1350 ℃-1600 ℃ of temperature and pressure 0.1～6.0MPa.
According to another kind of preferred implementation of the present invention; Described moisture-free coal powder pressure gasifying Reaktionsofen 33 is cylindrical tubes; Its reaction chamber 34 mainly is made up of water-cooled coil pipe and withstand voltage heat-resistance high-strength degree steel plate; Reaction chamber 34 height are 4-5 with the ratio of mean diameter, and top reaction compartment 34 is 1 with the ratio of the height of bottom quenching cooling chamber 35: 1-3.
According to another kind of preferred implementation of the present invention, in the said gasification reacting furnace 33, form preferably 1 to 6 by one or more steel pipe coiling around the water-cooled coil pipe 38 of burner hearth.When the hydromining in the coil pipe was got the pump circulation mode, coil pipe was one.When the hydromining in the coil pipe was taken from right Recycle design, coil pipe was many; The water coolant of water-cooled coil pipe adopts feedwater non-scaling, the process desalting treatment.
According to another kind of preferred implementation of the present invention; Said moisture-free coal powder pressure gasifying Reaktionsofen 33 comprises a heat reclamation device, and this device can be the natural convection heat reclamation device that comprises many water-cooled coil pipes 38, high-temperature water and vapour mixture upcast 89, high-temperature water downtake 88, dry pipe 31; Perhaps this device also can be to comprise single water-cooled coil pipe 38, technology cooling soft water inhalent siphon 90, high-temperature water or the outlet pipe 91 of high pressure steam or both mixtures, the pump circulation heat reclamation device of high-pressure process softened water pump 62.
According to another kind of preferred implementation of the present invention, both difference of altitude of said coal dust warehouse 14 and said fine coal positive delivery device 16 are the 15-25% of said coal dust warehouse 14 height.
According to another kind of preferred implementation of the present invention, described inertia is selected from nitrogen, argon gas or their mixture; Described carrier gas is nitrogen or air.
According to another kind of preferred implementation of the present invention; Said gas wash tower 54 dedusting washing measures comprise that washing water-bath 60 washing, traverse baffle 57 separate, tower tray 56 washings, eddy flow plate 55 separate, scum dredger 27 separates multistage washing, the stage trapping step of being formed, and the gas dustiness that has guaranteed washing tower is few.
Below the present invention will be described in more detail.
The present invention relates to a kind of is the method for raw material production synthetic gas with the coal dust.
Accompanying drawing 1,2,3,4-1,4-2,5,6-1,6-2,7,8 expression the present invention are the Figure of description of raw material production synthetic gas with the coal dust.
The method that with the coal dust is the raw material production synthetic gas comprises the steps:
Accompanying drawing 1 is the preparation flow figure of dry coal dust.
The preparation of A, dry coal dust.
Coal raw materials is removed irony class impurity wherein through tramp iron separator 2; By belt weighing feeding machine 3 Weighings; Get into crusher 4 broken coal-forming grains; Described coal grain is promoted to feed bin 6 through bucket elevator 5; Quantitatively send into grinding machine 8 by feeding machine 7 again and grind to form coal dust; When grinding, allow the hot blast of hotblast stove 1 and described coal dust carry out abundant heat exchange, make its coal dust be dried to water content by weight≤2.0%; Described coal dust drives at hot blast and gets into powder selector 9 down, and wherein 100% coal dust of granularity＜0.10mm drives entering powder collector 10 down at hot blast, and all the other coal dusts dependence self gravitations than volume particle size return grinding machine 8 and grind; Described powder collector 10 is connected with induced draft fan 12, under the effect of induced draft fan 12, removes the steam of the water that dry hot gas and coal in the powder collector 10 discharge; Described powder collector 10 is provided with fly-ash separator 11 at the top, to reduce the dust content of discharging the gas from powder collector 10; The dry coal dust of discharging from powder collector 10 bottoms is sent into follow-up workshop section and is handled.
According to the present invention, described coal raw materials is selected from hard coal, bituminous coal, brown coal or thermal value Q
B.adOther carbon solid raw material of＞17000kJ/kg.Described feed coal for example can be brown coal, long-flame coal, meager coal, the lean coal of low metamorphic grade, the hard coal of high metamorphic grade; Can be caking coal, weak bonding or dross coal; Can be middle ash, low culm, middle ash fusion point, low-ash-fusion coal be materials such as the coal of high ash content, high ash melting point, and coke powder.Described other carbon solid raw material for example is tire, rubber, the residual burnt grain of refining of petroleum, macromolecular organic compound or organic garbage of city, biomass fuel etc.Described dry coal dust is to be prone to carry, be prone to fluidizing dry powdery coal by feed coal through having of obtaining of dry, milled processed.
The crusher that the present invention uses when broken is normally used in the art crusher, for example the crusher sold with impact breaker trade(brand)name, machine Manufacturing Co., Ltd of Shanghai generation nation or mining and metallurgy company of great Santex Group of Shanghai magnificent machinofacture far away company limited; Said grinding machine is normally used in the art grinding machine, for example the grinding machine of Jiangsu Jiangyin Yate Machinery Manufacturing Co., Ltd., Shenyang Heavy Machinery Group Limited Liability Company or the sale of Shenyang Nonferrous Metallurgical Machinery Plant company.
Described feeding machine is a kind of normally used in the art feeding machine; This feeding machine has the function that the solid, powdery material is measured, and for example Qidong City perseverance in Jiangsu reaches DB, the DK type disk feeder of GF type Impeller powder feeder, disk feeder or the production of Henan Hebi City hundred million logical Meccanica Generale S. R. L of the production of electric power petrochemical equipment factory.
In the present invention; Described powder selector is a kind of normally used in the art powder selector; It has the function that the solid, powdery material is sieved, for example the Yancheng City Ji KD type powder separating machine product that JS powder separating machine that building equipment company limited produces, GXF type powder separating machine that Hebei Gaobeidian city Hua Xin cement machine factory produces or Xuzhou City Kodak cement machinery Manufacturing Co., Ltd produce of rising.
Described powder collector is a kind of normally used in the art powder collector, and this powder collector structure is top cylinder shape, lower taper, need have withstand voltage (design pressure＞7MPa), heat-resisting (design temperature＞200 ℃), wear-resisting and explosion-proof characteristic.
B, dry coal dust positive delivery.
Dry coal powder positive delivery can adopt dual mode, and promptly mechanical transport mode and gas delivery mode realize.
The mechanical transport mode is the mode of carrying dry coal dust like accompanying drawing 2 represented use fine coal positive delivery devices 16.Dry coal dust by above-mentioned steps A preparation passes through pipe-line transportation in coal dust warehouse 14, is transported to fine coal positive delivery device 16 through valve 15 then; Both difference of altitude of said coal dust warehouse 14 and said fine coal positive delivery device 16 are the 10-30% of said coal dust warehouse 14 height, are 0.10MPa at least with the intake pressure that guarantees fine coal positive delivery device 16.Preferably, both difference of altitude of said coal dust warehouse 14 and said fine coal positive delivery device 16 are the 15-25% of said coal dust warehouse 14 height.
Said fine coal positive delivery device 16 is a kind of devices with Piston Compression structure; This device is through electric motor M driven plunger; By reciprocating motion of the pistons rubber-like pump housing volume is changed; Cavity volume changes can make powder suck and extrusion cavity; Thereby form flowing of powder; Fine coal positive delivery device 16 can be brought up to 0.5-7.0MPa with dry coal dust pressure as required, arrives hopper 17 through pipe-line transportation again.After the 16 normal operations of fine coal positive delivery device, the pressure of hopper 17 is in high pressure conditions all the time, and described coal dust is transported to vapourizing furnace 33 through hopper outlet valve 19 after measuring through electronic scales 18; The dusty gas of discharging from coal dust warehouse 14 is discharged into atmosphere through cyclonic separator 13 gas separated from cyclonic separator 13 tops, and solid returns the recycle of coal dust warehouse.
The cyclonic separator that the present invention uses is a product sold in the market, for example the CLT/A type cyclonic separator produced of Hangzhou Southern Environmental Cleaning equipment Co., Ltd.
Perhaps the gas delivery mode is the dry coal dust gas delivery mode represented like accompanying drawing 3.The dry coal dust of above-mentioned steps A preparation is sent into normal pressure powder storehouse 21, and when the pressure in normal pressure powder storehouse 21 reached balance with the pressure of locking gas hopper 23, dry coal dust got into lock gas hoppers 22 through normal pressure powder storehouse 21 bottom valves 25; When the material level of lock gas hopper 22 reaches predetermined material level value; Close normal pressure powder storehouse 21 bottom valves 25; Fill high-pressure inert gas toward lock gas hopper 22 then; When the pressure of the pressure of locking gas hopper 22 and feeder 23 reaches balance; Open lock gas hopper 22 bottom valves 26; Dry coal dust gets into feeder 23 through this valve 26; Carrier gas by the input of feeder 23 bottoms makes the dry coal dust fluidisation that gets into feeder 23; The fluidized drying coal dust is discharged from feeder 23 tops, delivers to vapourizing furnace 33 through pipeline;
In the present invention, the normal pressure powder storehouse 21 of use is a kind of normal pressure, normal temperature, dustproof, explosion-proof ordinary steel container made, only bears the static pressure of coal dust in the container when normally using, and is that a kind of to have top be that round shape, bottom are the equipment of conical structure.
Described lock gas hopper 22 is a kind ofly can alternately bear normal pressure, high pressure (reaching as high as 7.0MPa) and the alternating pressure tankage of transformation (0-7.0MPa or 7.0-0MPa) in short-term; Because the container inner pressure load is high and constantly variation again; So the requirement to equipment intensity is very high, material and processing, manufacturing process also there is very harsh requirement.Its concrete structure is that top is ellipse end socket, middle circle tubular, lower cone shape; This product is a special pressure container; The unit that its design, processing, manufacturing need corresponding qualification accomplishes, for example Harbin Boiler Co., Ltd., Xi'an Nuclear Equipment Co., Ltd..
Described feeder 23 is a kind of high pressure that bear all the time, also to bear simultaneously the gas delivery coal dust to wall of container wash away, the abrasive pressure vessel and equipment.Its structure is top elipse head, middle part round shape, lower cone shape, is product sold in the market, for example the feeder produced of Xi'an Nuclear Equipment Co., Ltd..
The valve 25 in said normal pressure powder storehouse 21 is that a kind of needs bear and lock the same normal pressure of gas hopper, High Pressure Difference and the ball valve of transformation in short-term, and the ball valve that uses in its structure and the common chemical field is identical.Because cutting off medium is heterogeneous dry coal dust, thus very high to the seal form requirement of valve, require the leakage standard to be not less than IV at least in ANSI Class.This valve 25 also will stand the abrasion of washing away of dry coal dust; Because of solid particulate to wash away abrasion comparatively serious; Therefore on valve body material basis; The valve surface material that contacts with coal dust all need be carried out wear-resisting or anti-dashing and handled; Such as carbon tungsten alloy, perhaps at the Si Tailai alloy of valve surface build-up wear-resistant erosion in valve surface spraying abrasion-proof erosion.The valve 26 of described lock gas hopper 22 equally with valve 25 need bear high pressure, transformation and wear-and corrosion-resistant in short-term, and just this valve 26 is not under the normal pressure, so its strength ratio valve 25 is higher.
In the present invention, the inertia of use is selected from nitrogen, argon gas or their mixture.The carrier gas of using is nitrogen or air.
When lock gas hopper 22 material levels are lower than predetermined material level value; Lock gas hopper 22 bottom valves 26 are closed; The discharge degree that to lock gas hopper 22 through pipeline is to cyclonic separator 20; When the pressure of lock gas hopper 22 is reduced to normal pressure; Open normal pressure powder storehouse 21 bottom valves 25; Allow normal pressure storehouse 21 interior dry coal dusts get into lock gas hopper 22, continue the recycle feed program; The dusty gas of being discharged by normal pressure powder storehouse 21, lock gas hopper 22 carries out gas through cyclonic separator 20 to be separated with solid, and gas separated is discharged into atmosphere from cyclonic separator 20 tops, and solid separated is returned the storehouse recycle of normal pressure powder through returning valve 24.
The pressurized high-temperature gasification of C, dry coal dust
Accompanying drawing 4-1 and accompanying drawing 4-2 represent dry coal dust pressurized high-temperature gasification, raw gas cooling and slagging-off schema.
The dry coal dust that above-mentioned steps B obtains is delivered to multithread road spraying burner 32 inlets that are positioned at moisture-free coal powder pressure gasifying stove 33 tops and passed through it; Spraying burner 32 outlets in the multithread road; Vaporized chemical through multithread road spraying burner 32 is sprayed onto dry coal dust in the reaction chamber 34 of moisture-free coal powder pressure gasifying stove 32; And make its vaporized chemical and dry coal dust under the condition of 1350 ℃-1600 ℃ of temperature and pressure 0.1～6.0MPa, carry out combustion reactions, generate and contain CO, H
2And CO
2Be the high temperature crude synthesis gas of main ingredient and the mixture of molten ash.
Described multithread road spraying burner 32 is the coaxial textural association equipment that is nested of a kind of multitube.Accompanying drawing 5 is multithread road spraying burner structure iron.It is made up of central duct 63, cooling medium channel 64, vaporized chemical medium channel 66 and dry coal dust passage 65.Described dry coal powder sprays into simultaneously through dry coal powder passage 65 and vaporized chemical through vaporized chemical medium channel 66 and carries out gasification reaction in the dry coal powder pressure gasifying stove 33.Described central duct 63 is used for transfer the fuel, and this fuel has exported the effect of ignition source at spraying burner 32, guarantees that dry coal powder and vaporized chemical spray into dry coal dust gasification furnace 33 and can burn after interior.Described cooling medium channel 64 is used for carrying the cooling medium, avoids bearing too high temperature in normal operation to guarantee spraying burner 32.
In accompanying drawing 5, a is the import of fuel central duct, and fuel gets into multithread road spraying burner 32 thus.B and f are that import, c and the g of spraying burner cooling medium is the outlet of spraying burner cooling medium, and this medium is water coolant normally, and water coolant is used to protect whole multithread road spraying burner 32, prevents that these metal pipe materials from receiving high temperature ablation; D is the import of vaporized chemical passage 66.In the present invention; Described vaporized chemical plays the effect of its ignition dope and temperature regulato in gasification reaction, simultaneously owing to carbonaceous material in the dry coal dust of gasified raw material is more, and hydrogenous material is less relatively; Therefore, described vaporized chemical also plays the effect that protium is provided in gasification reaction.E is the import of dry coal dust transfer passage 65, and dry coal dust is dispelled by vaporized chemical at the spraying burner head through this transfer passage, and is ignited, thereby discharges a large amount of heats, for gasification reaction provides reaction power and reaction medium.
In the present invention, described fuel can be with CH
4Composition is main Sweet natural gas, also can be the natural vapour of liquefaction, diesel oil, perhaps from the flammable tail gas with certain calorific value that produces in the plant produced.
Described vaporized chemical is selected from air, oxygen-rich air, pure oxygen, CO
2Or superheated vapour, oxygen rich gas and superheated vapour or CO
2, air and water vapor or CO
2Mixture.Described oxygen rich gas is that oxygen and one or more are selected from the mixture of the gas of nitrogen, argon gas, carbonic acid gas, and wherein oxygen content accounts for more than 60% of this gaseous mixture cumulative volume meter.Described vaporized chemical is pure oxygen or oxygen rich gas and superheated vapour or CO preferably
2Mixture, more preferably be pure oxygen and superheated vapour or CO
2Mixture.Described pure oxygen is the oxygen of purity >=99.5%.For the present invention; The pressure of said water vapor is close with the pure oxygen, oxygen enrichment or the air pressure that add in the vapourizing furnace; Its temperature is higher than the saturated-steam temperature under its relevant pressure, and the mixture that this water vapor and pure oxygen, oxygen enrichment or air mixed obtain can not be separated out liquid water when its temperature reduces.The pressure of said vaporized chemical will be higher than coal dust pressure.
Preferably, described vaporized chemical and dry coal dust carry out combustion reactions under the condition of 1450 ℃-1520 ℃ of temperature and pressure 2.0-4.0MPa.
This multithread road spraying burner 32 is provided with a cooling system, and this cooling system is made up of with pump 30 cooling trough 28, cooling tube 29; Be contained in water in the cooling trough 28 after cooling tube 29 cooling; Again through pump 30 pressurized stream through the multithread road spraying burner 32; Make the temperature of multithread road spraying burner keep stable; Spraying burner 32 effusive water return cooling trough 28 again from the multithread road, through recycling after 29 coolings of the water-cooled tube in the cooling trough 28.
Described moisture-free coal powder pressure gasifying stove 33 is cylindrical tubes of a band ellipsoidal head.Fig. 6-1,6-2 are the structure diagrams of these vapourizing furnace 33 reaction chambers.These vapourizing furnace 33 cylindrical shell height are 4-5 with the ratio of mean diameter, and its top reaction compartment 34 is 1 with the ratio of the height of bottom quenching cooling chamber 35: 1-3.The top of this vapourizing furnace is reaction chamber 34, and the bottom is a quenching cooling chamber 35.Reaction chamber 34 comprises furnace roof inlet 36, burner hearth 37, around the water-cooled coil pipe 38 of burner hearth, the refractory masses 39 and vapourizing furnace shell 40 of protection water-cooled coil pipe; Furnace roof inlet 36 is connected with said multithread road spraying burner 32.
Water-cooled coil pipe 38 is formed by high temperature resistant, the corrosion-resistant steel pipe coiling around burner hearth 37 of one or more different lengths, is used for a large amount of transfer of heat that reaction chamber is produced, has an accident because of its reaction chamber temperature is too high avoiding.Water coolant in the water-cooled coil pipe 38 is the desalinating process soft water of handling through softening.The indoor heat of this technology soft water absorption reaction becomes high pressure steam, to keep the thermal equilibrium of vapourizing furnace burner hearth 37 and vapourizing furnace housing 40.Water in the water-cooled coil pipe 38 can circulate with the natural convection mode, or circulates with the pump circulation mode.
Described quenching cooling chamber 35 is provided with water distributor 41, sending down abnormally ascending pipe 42 and riser 43; Sending down abnormally ascending pipe 42 upper ends are connected fixing with water distributor 41; Riser 43 is supported on quenching cooling chamber 35 housings; Sending down abnormally ascending pipe 42 and riser 43 arranged concentric; An annular space is arranged to each other, and be fixed together with preset pieces 44.
Accompanying drawing 4-1 is for adopting natural convection mode round-robin schema.Among the figure water-cooled coil pipe of vapourizing furnace by many steel pipes with the multilayer mode around burner hearth 37, thereby reduced the resistance to heat that the back produces that is heated of water in the water-cooled coil pipe.The position of water coolant in water-cooled coil pipe 38 is different and to absorb heat also inequality; Therefore can produce a kind of gravitational difference; Hot water gets into drum 31 through upcast; Water relatively cool in the drum 31, that density is bigger gets into the water-cooled coil pipe through downtake; Absorb the part heat that gasification hearth produces, thereby form the process of a natural circulation.
Accompanying drawing 4-2 carries out the round-robin schema for adopting the pump circulation mode.Water-cooled coil pipe 38 is formed by a steel pipe coiling among the figure; The aqueous cold plate tubular construction is simple; But because water-cooled coil pipe total length is longer; Current in the water-cooled coil pipe are through the big calorimetric of the peripheral absorption of gasification hearth; Can produce very high vapour locking; So the mobile dependence high-pressure process softened water pump 62 of water-cooled coil pipe water is forced pressurization; Thereby realize the forced-flow of technology soft water in the water-cooled coil pipe; When employing is flowed with the pump circulation mode; According to vapourizing furnace 33 operating modes and technology soft water flow size, the water of discharging from the water-cooled coil pipe can be high-pressure water heating; The mixture of high-pressure water heating and water vapor; High-pressure saturated steam or high pressure, superheated steam.
Accompanying drawing 6-1 is the vapourizing furnace sketch that adopts the natural convection Recycle design.A is a vapourizing furnace upper flange interface in the accompanying drawing; This interface is connected with the flange of spraying burner 32; B is vapourizing furnace reaction chamber gas and slag exit, and this outlet links to each other with bottom quenching cooling chamber 35, and the coal gas of high temperature and the molten slag that are used for reaction chamber is produced carry out the quenching cooling.These cinder notch size decision gasification hearth 37 gas flowfields distribute, and influence gas efficiency, and the discharge of liquid towards slag simultaneously also can produce certain influence.General this cinder notch and vapourizing furnace vertical tube part chamfering are the 40-60 degree, and preferred cinder notch chamfering is 45 degree.c
1,2, c
3,4Be four entrance of cooling water of gasifier water-cooling coil pipe 38, this mouth links to each other with drum 31 through downtake, is used for the water in the drum 31 is imported water-cooled coil pipe 38.d
1,2, d
3,4Mouth is the superheated vapor mixture outlet.Cooling-water flowing is through burner hearth, absorbs part heat in the burner hearth, and self temperature improves and becomes steam water interface, through this mouth entering drum 31.E1, e2, e3, e4 are the thermopair interface of vapourizing furnace, and this interface is used for the thermopair of installation and measuring vapourizing furnace 33 service temperatures.Four thermopair interface vertical direction openings are divided into two planes, the conplane symmetrical distribution mode of taking of horizontal direction, and adjacent two thermopairs of Different Plane are mutually 90 degree uniform distribution.F is the pressure taps of vapourizing furnace 33, and this mouth is used for the setting pressure transmitter, be used to detect the working pressure in the vapourizing furnace 33, and to Controlling System output pressure signal.G1, g2 are gasifier water-cooling coil pipe 38 thermopair interfaces, and this interface is used for the thermopair of installation and measuring water-cooled coil pipe 38 temperature.H is the high pressure gas sealed interface, is used for the pressure of balance space v1 and v2, guarantees that water-cooled coil pipe 38 is in pressure balance under hot conditions, thereby prolongs its work-ing life.
Accompanying drawing 6-2 is the vapourizing furnace sketch when adopting single water-cooled coil pipe water coolant pump circulation.A is a vapourizing furnace upper flange interface in the accompanying drawing; This interface is connected with the flange of spraying burner 32; B is vapourizing furnace reaction chamber gas and slag exit, and this outlet links to each other with bottom quenching cooling chamber 35, and the coal gas of high temperature and the molten slag that are used for reaction chamber is produced carry out the quenching cooling.These cinder notch size decision gasification hearth 37 gas flowfields distribute, and influence gas efficiency, and the discharge of liquid towards slag simultaneously also can produce certain influence.General this cinder notch and vapourizing furnace vertical tube part chamfering are the 40-60 degree, and preferred cinder notch chamfering is 45 degree.C is the entrance of cooling water of gasifier water-cooling coil pipe 38, and this mouth links to each other with cooling water circulating pump 62 outlets, is used for water coolant is imported water-cooled coil pipe 38.The d mouth is the cooling water outlet that is heated, and cooling-water flowing is through burner hearth, absorbs part heat in the burner hearth, and self temperature improves.E is the pressure taps of vapourizing furnace 33, and this mouth is used for the setting pressure transmitter, be used to detect the working pressure in the vapourizing furnace 33, and to Controlling System output pressure signal.F1, f2, f3, f4 are the thermopair interface of vapourizing furnace, and this interface is used for the thermopair of installation and measuring vapourizing furnace 33 service temperatures.Four thermopair interface vertical direction openings are divided into two planes, the conplane symmetrical distribution mode of taking of horizontal direction, and adjacent two thermopairs of Different Plane are mutually 90 degree uniform distribution.G1, g2 are gasifier water-cooling coil pipe 38 thermopair interfaces, and this interface is used for the thermopair of installation and measuring water-cooled coil pipe 38 temperature.H is the high pressure gas sealed interface, is used for the pressure of balance space v1 and v2, guarantees that water-cooled coil pipe 38 is in pressure balance under hot conditions, thereby prolongs its work-ing life.
Among Fig. 6-1, the 6-2, refractory masses 39 usefulness of protection water-cooled coil pipe can stand the fusion warm sludge and wash away the erosive material and process, and such material for example is a silicon carbide, is the corrosion-proof fire-resistant material of selling in the market.In the coal gasification reaction process, on its refractory materials laminar surface, form one deck melting slag film, this film can play a kind of effect of protecting water-cooled coil pipe 38 because of thermal conductivity is low.
Said moisture-free coal powder pressure gasifying Reaktionsofen 33 also comprises a heat reclamation device, and it comprises water-cooled coil pipe 38, high-temperature water upcast, high-temperature-hot-water downtake, dry pipe 31 or high-pressure process softened water pump 62.
D, high temperature crude synthesis gas, molten ash cooling and crude synthesis gas washing, purifying.
In quenching cooling chamber 35; The high temperature crude synthesis gas and the molten ash mixture that allow step C obtain mix and cooling with the water coolant that gets into bubbling cooling bath 45 through sending down abnormally ascending pipe 42 that is got into by said water distributor 41, and the cinder slag is deposited in quenching cooling chamber 35 bottoms because of sudden cold-curing.The crude synthesis gas that contains a small amount of thin ash and water rises along the annular space between sending down abnormally ascending pipe 42 and the riser 43; In the annular space upper end; Because the space that said crude synthesis gas flows into increases suddenly; Gas velocity sharply reduces; A part of water that said crude synthesis gas contains can turn back in the bubbling cooling bath 45 along sending down abnormally ascending pipe 42 inwalls with thin ash, and remaining crude synthesis gas goes out vapourizing furnace 33 through row of conduits.
Said sending down abnormally ascending pipe 42 is the different results of both diameters with annular space between the riser 43, and this annular space has certain thickness, and promptly both diameters is poor, and this thickness is the 5-15% of sending down abnormally ascending pipe 42 diameters.If this thickness, can cause then that gas flow rate is too fast in the annular space less than 5%, and cause the gas entrainment amount of liquid to increase, increase the unstable of system; If the gas that this thickness greater than 15%, then can cause getting off from downtake directly flows out from annular space, do not carry out abundant heat exchange with water-bath 45, cause gas temperature too high.Therefore, this thickness 8-12% of sending down abnormally ascending pipe 42 diameters preferably.
According to the present invention; Described water distributor is a kind of equipment with open circles annular structure of uniform distribution ostium excurrens; Its main effect is in aperture, to spray water coolant; High-temperature gas, liquid slag to going out the gasifier slag mouth cool off; The effusive water of aperture forms water membrane in downtake 42 simultaneously, and protection downtake 42 is avoided the high temperature invasion and attack.
Described bubbling cooling bath 45 is a kind of equipment with water storage function, high temperature resistant, high pressure resistant tube structure; Its main effect is that the synthetic gas that downtake 42 is further cooled off; Slag is lowered the temperature; Simultaneously the synthetic gas that goes out downtake 42 is tentatively washed, remove part soot particle wherein.
In addition, said cinder slag disposal facilities is set below moisture-free coal powder pressure gasifying stove 33.Cinder slag in quenching cooling chamber 35 bottoms gets into lock bucket 47 through lock slag valve 46, discharges through vent valves 48, and the water that contains thin ash that the cinder slag is carried secretly is delivered to the vacuum evaporator 69 of accompanying drawing 8 water treatment portion.Said cinder slag discharging is that the waste residue (being referred to as the cinder slag) of unconverted hydrocarbon substance and generation in the gasification reaction is discharged from moisture-free coal powder pressure gasifying stove 33 bottoms through lock bucket 47.The high-temperature synthesis gas that generates at the reaction chamber of this vapourizing furnace 33 and fusion warm sludge leave the quenching cooling chamber 35 of this reaction chamber entering vapourizing furnace 33; In this quenching cooling chamber 35; Water coolant gets in the bubbling cooling bath 45 of quenching cooling chamber 35 bottoms through sending down abnormally ascending pipe 42 with high-temperature synthesis gas, fusion warm sludge and stream behind the uniform distribution under said water distributor 41 effects; Said cinder slag is cooled after the water cooling, gets into bottom cinder slag disposal facilities and drains.This cinder slag disposal facilities comprises lock slag valve 46, lock bucket 47 and vent valves 48.
When the cinder slag is collected; At first lock bucket 47 is carried out punching press; Make the pressure of pressure and vapourizing furnace 33 of lock bucket 47 basic identical; Open lock slag valve 46 then; Said cinder slag relies on the effect of self gravitation and circulating water flow to get into lock bucket 47 from bubbling cooling bath 45, closes locking slag valve 46 after the cinder slag is collected and accomplished; When the cinder slag discharges; Earlier lock bucket 47 is carried out release; Unload to normal pressure and open cinder slag vent valves 48; The cinder slag relies on wash-down water pressure to discharge lock bucket 47; In order to impel cinder slag smooth discharge and to prevent cinder slag vent valves 48 inner slag inclusions; Lock bucket 47 is washed with wash-down water in tapping process, and wash-down water is from accompanying drawing 8 grey water pump 74 outlets, and flushing is closed cinder slag vent valves 48 after finishing.
Described lock slag valve 46 is that a kind of to have topworks, magnetic valve, bound switch, spool and valve seat be the equipment of globosity, is product sold in the market, and for example U.S. tall and erect automatization Shanghai company limited is with trade(brand)name lock bucket valve product sold.Its main effect is to cut off or connection quenching cooling chamber 35 and the grain slag stream of locking bucket 47, when locking bucket 47 receipts slags, and this valve open, when lock bucket deslagging, this valve closes.
Described lock bucket is that a kind of top with band elipse head is the equipment of cylindrical lower part circle of position pyramidal structure; It is product sold in the market; For example Harbin Boiler Co., Ltd. is with trade(brand)name lock bucket product sold; Its main effect is to collect the pulp water that quenching cooling chamber 35 discharges, and constantly bears high pressure, normal pressure, high pressure to normal pressure conversion, the normal pressure reactive force to high pressure conversion.
The crude synthesis gas that comes out from quenching cooling chamber 35 gets into high temperature crude synthesis gas washing, purifying part.The crude synthesis gas that contains thin buck of discharging from vapourizing furnace 33 or get into air water separator 51 is removed the thin buck of wherein carrying secretly that contains, and these contain thin buck and after reducing pressure, send to through pipeline and carry out thin grey water handing.Remove the crude synthesis gas that contains thin buck and deliver to infiltration washer 53 through pipeline.Perhaps the crude synthesis gas that contains thin buck of discharging from vapourizing furnace 33 is directly delivered to through pipeline and is soaked into washer 53.
In the present invention; Described air water separator is a kind of columnar structured equipment with band end socket and cone; It is product sold in the market; For example first ground, Shanghai valve company limited is with trade(brand)name AS gas-liquid separator product sold., its main effect is that the gas that gets into this equipment is effectively separated with liquid.
Said infiltration washer 53 is made up of not isometrical outer tube and intervalve, and wherein intervalve is that the diameter of its two end portions is 1.2-2.0 a times of middle portion diameter, and the length of middle portion is the 70-85% of whole intervalve length; Outer tube diameter is 1.1-1.4 a times of intervalve diameter.Crude synthesis gas gets into from outer tube; The middle standpipe tube passage is walked buck; It is even to arrive the buck and the crude synthesis gas thorough mixing that soak into washer 53 by gas wash tower 54 bottom bubbling style water-bath storage tanks 60 through grey water-circulating pump 49 pressure-raisings in the trunnion exit, and the thin ash in the crude synthesis gas is soaked into fully.
In soaking into washer 53; Allow the crude synthesis gas that contains thin buck and buck thorough mixing from gas wash tower 54; Get into gas wash tower 54 through pipeline then; Arriving bubbling style water-bath storage tank 60 along downtake 58 again washs; Said crude synthesis gas rises along the annular space that forms between downtake 58 and the upcast 59 again; And carry out multistage washing through traverse baffle 57, tower tray 56 and eddy flow plate 55; Discharge along pipeline from gas wash tower 54 tops through scum dredger 27 backs, obtain a kind of synthetic gas.After gas wash tower 63 multistage washings, ash oontent can be reduced to 0.8mg/Nm in this synthetic gas
3Below, can be used as follow-up unstripped gas.
In the present invention, accompanying drawing 7 is the structure diagram of washing tower.Described gas wash tower 54 is a cylindrical pressure vessel; In gas wash tower 54, be provided with downtake 58; Upcast 59; Bubbling style water-bath storage tank 60; Traverse baffle 57; Tower tray 56; Eddy flow plate 55 multistage washing devices; Top is provided with scum dredger 27 simultaneously; They constitute in the following manner: downtake 58 tops link to each other with inlet pipe g; Upcast 59 is fixed on the tower body; Downtake 58 inserts in the bubbling style water-bath storage tank 60 with the bottom of upcast 59; On bubbling style water-bath storage tank 60 tops from setting gradually down traverse baffle 57; Tower tray 56 and eddy flow plate 55 are provided with scum dredger 27 above eddy flow plate 55.A is the syngas outlet after cleaning among the figure, and b is tower tray 56 phlegma inlet pipes, and the phlegma of cleaning washs synthetic gas to be used for carrying comparatively to tower tray, and c is tower tray 56 grey water inlets, is used for carrying the washing buck to tower tray, and synthetic gas is washed.D is a pressure taps, is used to measure washing tower pressure.E is the clean relatively grey water outs in washing tower water-bath 60 tops, and being connected through grey water-circulating pump 49 is used for to soaking into washer 53, water distributor 41 water supply.F is washing tower water-bath 60 water supplement ports, and the buck of the back system that is used for recycling imports the washing tower water-bath.H is the more relatively Heisui River outlet of washing tower bottom ash content, is used for Heisui River is imported follow-up thin grey water treatment system.
Described tower tray can be sieve-board type, bubble-cap formula or float-valve type tower tray; Be normally used equipment in chemical technology field; Company of Yantai Guobang Chemical Machine Technology Co., Ltd. product sold for example; Their main effect is respectively gas and liquid to be carried out the adverse current uniform distribution contact, and removes the dust in the crude synthesis gas.
Described eddy flow plate, traverse baffle are normally used equipment in chemical technology field, Yixing City original dust-removal and desulfurizing environmental protection equipment company limited product sold for example, and their main effect is respectively that the liquid of carrying secretly in the gas is separated.
Described scum dredger is a kind of cancellated equipment that has, and is product sold in the market, the Nanjing mound safe metal products company limited product sold of fighting for example, and its main effect is to remove the liquid entrainment of carrying secretly in the gas.
What the washing crude synthesis gas obtained contains in the bubbling style water-bath storage tank 60 that thin buck collects in gas wash tower 54 bottoms.The buck on these bubbling style water-bath storage tank 60 tops part after pipeline is by grey water-circulating pump 49 pressure-raisings is delivered to moisture-free coal powder pressure gasifying stove 33 entrance of cooling water along pipeline; Another part is sent into along pipeline and is soaked into washer 53 and soak into thin ash wherein with the crude synthesis gas thorough mixing, and these bubbling style water-bath storage tank 60 bottom ash contents are more contains thin buck and after reducing pressure, sent to by pipeline and contain thin grey water treatment system.Gas wash tower 54 a bath wateies part is come the circulation buck after the self-contained thin grey water handing; Get into bubbling style water-bath storage tank 60 from gas wash tower 54 middle and lower part imports; Another part is from downstream section phlegma or the outer make up water that supplies, and they get in the gas wash tower 54 between tower tray 56 and eddy flow plate 55.
The buck of discharging from bubbling style water-bath storage tank 60 is through separated into two parts behind grey water-circulating pump 49 pressure-raisings; A part is sent into along pipeline and is soaked into washer 53, and the water distributor 41 that another part is sent into moisture-free coal powder pressure gasifying stove 33 cinder notch below through pipeline is used as water coolant.
Accompanying drawing 8 is to contain thin grey water treatment system schema.Bubbling style water-bath storage tank 60 bottoms of gas wash tower 54 contain that thin buck, air water separator 51 are isolating to be contained thin buck and get into high-temperature water heater 67 and carry out the step-down cooling with the thin buck back of reducing pressure respectively that contains of discharging from quenching cooling chamber.In this high-temperature water heater 67, can reclaim the heat of high temperature phlegma on the one hand, the loss that can replenish gasification system water on the other hand.From high-temperature water heater's 67 top escaping gas mainly is that steam gets into buck heating device 83 recovery heats.In buck heating device 83, evolving gas and the circulation buck heat exchange of being sent here by degasification water pump 76 are delivered to the bubbling style water-bath storage tank 60 of gas wash tower 54 then; Evolving gas major part after heat exchange is condensed into liquid, gets into gas-liquid mixed separating tank 84 again, and from its top emptying or be sent to follow-up workshop section and reclaim, isolating water turns back to degasification water pot 75 to gas separated through liquid barrier 85.Described buck heating device 83 is floating head type tubular structures known to those skilled in the art, and the size of its heat interchanging area and material can be confirmed according to characteristic, temperature, the quantity of heat transferring medium.Described gas-liquid mixed separating tank 84 is the cylindrical overpressure resistant barrels that have end socket up and down, can be the sky cylindrical shell perhaps is provided with liquid barrier on top cylindrical shell.
The thin buck that contains of discharging from high-temperature water heater 67 bottoms gets into secondary step-down transformer 68 recovery heats; The steam of overflowing from secondary step-down transformer 68 tops carries out temperature adjustment back or directly gets into degasification water pot 75 without gas condenser 86 through gas condenser 86 reclaiming heat, and the thin buck that contains of discharging from secondary step-down transformer 68 bottoms gets into vacuum evaporator 69 step-downs cooling; After the 77 cooling coolings of negative pressure condenser, get into negative pressure separator 78 from vacuum evaporator 69 top escaping gas; Gas gets into off-gas pump 80 through liquid barrier 79 after separating moisture; Emptying after off-gas pump separator 81 separates moisture again; Off-gas pump separator 81 isolating water and negative pressure separator 78 isolating water flow into aqua storage tank 73, and the thin buck that contains of discharging from vacuum evaporator 69 bottoms gets into clarification separate tank 71 behind clarification separate tank feeding pump 70 pressure-raisings; In clarification separate tank 71, add the water treatment organic polymer coargulator and make thin grey suspended substance flocculation.Described organic polymer coargulator is a kind ofly can impel the thin grey particles agglomerate that suspends to be coupled to thick cotton-shaped or agglomerate and reach the organic high molecular polymer of rapid subsidence; It is the polyacrylamide of polymerization ferrous sulfate, polymerize aluminum chloride and molecular weight 1200-1500 ten thousand, and for example Tianjin Chemical Research & Desing Inst is with trade(brand)name polymer flocculating agent product sold.The technician in present technique field can be according to containing the thin grey water yield is easy to confirm to add flocculation agent through test amount.The top overflow of clarification separate tank 71 flows into aqua storage tank 73; The buck of aqua storage tank 73 part behind grey water pump 74 pressure-raisings is sent into degasification water pot 75; A part is as wash-down water; Few part effluxes; The main purpose that effluxes is in order to keep the balance of solubility salt in the buck, to alleviate equipment and Corrosion of Pipeline.
Buck in the degasification water pot 75 adds the gas that heat extraction wherein carried secretly through interchanger and drains, simultaneously 75 outlets of degasification water pot or degasification water pot 75 in the adding dispersion agent, to alleviate the fouling of interchanger and ash-water pipeline.Described dispersion agent should be appreciated that it is a kind of agent that promotes that dissolved gases overflows fast in the water, delays fouling; Described dispersion agent for example is the maleic anhydride of 4-10% hydrolysis by weight.For example Tianjin Chemical Research & Desing Inst with trade(brand)name high temperature dirt dispersion agent product sold, the calm and peaceful water treatment in Shandong company with trade(brand)name TH-504 product sold.Said dispersant dosage is that preferably 60～75PPm is more preferably 65～70PPm in pending thin grey water yield gross weight 50～80PPm.
The degasification buck is gone into buck heating device 83 through degasification water pump 76 pressure-raisings are laggard, heats up again with from high-temperature water heater's 67 top escaping gas heat exchange, and the bubbling style water-bath storage tank 60 of delivering to gas wash tower 54 then recycles; Higher dense of clarification separate tank 71 bottom ash contents contains thin buck and after 87 superchargings of filter feeding pump, gets into vacuum band-type filter machine 72 and carry out separating of thin ash and water, and described thin ash is collected the back and discharged, and isolating water turns back to again to be clarified in the separate tank 71.Described vacuum band-type filter machine 72 be for example Nuclear Industry Yantai Tongxing Industry Co., Ltd with trade(brand)name vacuum band-type filter machine product sold, Huzhou examine the mechanical company limited of rich filtration with trade(brand)name vacuum band-type filter machine product sold, Tianhe Machinery Equipment Co., Ltd., Shijiazhuang with trade(brand)name vacuum band-type filter machine product sold.
In the present invention; Described high-temperature water heater is a kind of columnar structured equipment with last elipse head, following cone; It is product sold in the market; For example chemical of Nanjing chemical industry company limited is with trade(brand)name flasher product sold; Its main effect is that the higher gas-vapor mix of unexpected post-decompression ash content is carried out gas-liquid separation; Produce the vapor recovery heat, carry out concentrating of ash content to containing buck simultaneously, be convenient to follow-up convenient the processing.
The structure of described secondary step-down transformer is go up elipse head, following cone columnar structured; It is product sold in the market; For example chemical of Nanjing chemical industry company limited is with trade(brand)name flasher product sold; Its main effect is that the higher gas-vapor mix of unexpected post-decompression ash content is carried out gas-liquid separation; Produce the vapor recovery heat; Simultaneously spissated buck is carried out further concentrating of ash content, be convenient to follow-up convenient the processing.
Described vacuum evaporator is a kind of the columnar structured of last elipse head, following cone that has; It is product sold in the market; For example chemical of Nanjing chemical industry company limited is with trade(brand)name flasher product sold; Its main effect is that the higher gas-vapor mix of unexpected post-decompression ash content is carried out gas-liquid separation; Make that sour gas parses in the water in water; Simultaneously spissated buck is carried out further concentrating of ash content, be convenient to follow-up convenient the processing.
The structure of described off-gas pump separator is with the cylindrical device that goes up lower cover; It is inner to be empty; Also can establish liquid barrier; It is product sold in the market; For example chemical of Nanjing chemical industry company limited is with trade(brand)name separator product sold, and its main effect is that liquid-vapor mixture is separated.
Described buck heating device is a floating head type tubular structure known to those skilled in the art, and the size of its heat interchanging area and material need to confirm according to characteristic, temperature, the amount of medium.
The invention still further relates to the product that adopts the inventive method to produce, this product is to contain CO, H
2And CO
2Be the synthetic gas of main ingredient, wherein the content of CO can reach in anhydrous synthetic gas cumulative volume more than 63%, H
2Content can reach more than 27%, CO
2Content can reach below 10%.
CO, H in the product of the present invention
2And CO
2Content be to adopt GB/T17132-1997 to analyze.
The product that adopts the inventive method to produce promptly contains CO, H
2And CO
2For the synthetic gas of main ingredient can be used for synthesizing methanol, ammonia, dme, alkene, producing acetic acid by carbonylation method, aceticanhydride etc.; Also can be used to generate electricity, the unstripped gas of heat, chemical etc., also can be used for IGCC combined cycle generation project supply raw materials gas and fuel gas simultaneously.Adopt other method that its product is carried out the resulting H of purifying
2Can be used as the unstripped gas of the required unstripped gas of gelatin liquefaction, Hydrogen Energy battery, the reducing gas of metallurgical project etc.
[beneficial effect]
The present invention has following positively effect.
1, adopted and the diverse moisture-free coal powder pressure gasifying of prior art stove 33 owing to the inventive method; So method of the present invention has been expanded raw material subject range greatly; Method for example of the present invention can be used the coal of various metamorphic grade, various ash content, different grey melting characteristics, and prior art is just made raw material with fine bituminous coal.
2, the vaporized chemical choice is bigger, and different to the requirement of unstripped gas composition according to follow-up workshop section, vaporized chemical of the present invention can be selected pure oxygen and water vapor or CO
2, oxygen-rich air and water vapor or CO
2, air and water vapor or CO
2Mixture, produce chemical industry synthetic gas, fuel gas etc. according to different use approach.
3, the present invention's employing high-temperature gasification that gasifies, gasification temperature can reach 1600 ℃, and fuel is decomposed into gas fully under this high temperature, can not produce any organism such as phenol, anthracene, and the synthetic gas effective constituent of generation can be up to more than 90%, and the fuel carbon transformation efficiency surpasses 98%.And its synthetic gas effective constituent of wet method gasification process commonly used at present only can reach about 80%, and carbon transforms and is up to 97%.Therefore efficiency of energy utilization of the present invention is very high.After synthetic gas adopted the water Quench, buck can be realized most of recycle after adopting conventional heat recuperation, liquid-solid separation, and few part effluxes and is used for equilibrium system soluble salt ion, and it is also comparatively simple to efflux the water treatment mode.
4, because the present invention has adopted and the diverse crude synthesis gas of prior art washs and purification techniques; I.e. washing, vapor-liquid separation, washing, cleaned condensate washing, vapour-liquid cyclonic separation, foam removal again are so the thin ash content that adopts the inventive method to produce synthetic gas is lower than 0.8mg/Nm
3, and prior art generally reaches 1.5mg/Nm
3, therefore, the thin ash content that the present invention produces synthetic gas is starkly lower than prior art.
5, owing to can adopt the dry coal dust mode of movement of mechanical type, improve transport efficiency greatly, reduced the nitrogen use level of sending into gasified boiler system.Compare with existing dry coal powder gasification technology, gasification efficiency of the present invention can reach more than 80%, and prior art generally reaches about 75%.Adopt dry coal dust e Foerderanlage can reduce investment, working cost simultaneously, reduce the frequent parking that causes owing to fine coal delivery system fault, improved the cycle of operation of device greatly.
6, vapourizing furnace of the present invention can adopt the aqueous cold plate protection of pipe metal shell of pump circulation mode; Thereby the layout of vapourizing furnace heating surface coil pipe is more flexible, and the even water cycle of heated coil is good, and it is fast that vapourizing furnace plays blowing out; Coil pipe can use the tubule diameter pipes, also saves the part steel simultaneously.
7, the present invention has adopted and has contained thin buck recycle utilization after treatment, makes whole dry coal dust pressurized high-temperature gasification system waste water, discharge amount of exhaust gas very little, and compared with prior art, waste water, discharge amount of exhaust gas reduce more than 30%.Therefore, method of the present invention is environmentally friendly.
In a word, method of the present invention is utilized raw mineral materials, adopts the novelty procedure of processing, at lower cost and environmental friendliness ground produce the energy and Industrial products desired raw material gas, the high added value conversion of realization resource with high value.Simultaneously, take operating method such as high-temperature gasification, flash distillation heat recuperation, solid-liquid be settlement separate, realized the recycle of waste water,waste gas and industrial residue, for China's emission reduction tasks is made significant contribution.
[description of drawings]
Fig. 1 is dry coal dust preparation flow figure;
Fig. 2 is that dry coal dust fine coal positive delivery device is carried schema;
Fig. 3 is dry coal dust gas delivery schema;
Fig. 4-the 1st, the dry coal dust pressurized high-temperature gasification of natural recirculating type, raw gas cooling washing and slagging-off schema;
Fig. 4-the 2nd, the dry coal dust pressurized high-temperature gasification of forced cyclic type, raw gas cooling washing and slagging-off schema;
Fig. 5 is a multithread road spraying burner sketch;
Fig. 6-1 natural recirculating type moisture-free coal powder pressure gasifying stove;
Fig. 6-2 forced cyclic type moisture-free coal powder pressure gasifying stove;
Fig. 7 is the washing tower sketch;
Fig. 8 contains thin grey water treatment system schema;
Wherein, 1, hotblast stove; 2, tramp iron separator; 3, belt weighing feeding machine; 4, crusher; 5, bucket elevator; 6, feed bin; 7, feeding machine; 8, grinding machine; 9, powder selector; 10, powder collector; 11, fly-ash separator; 12, induced draft fan; 13, cyclonic separator; 14, coal dust warehouse; 15, valve; 16, fine coal positive delivery device; 17, hopper; 18, electronic scales; 19, outlet valve; 20, cyclonic separator; 21, normal pressure powder storehouse; 22, lock gas hopper; 23, feeder; 24, return valve; 25, valve; 26, valve; 27, foam removal; 28, cooling trough; 29, cooling tube; 30, pump; 31, dry pipe; 32, multithread road spraying burner; 33, vapourizing furnace; 34, reaction chamber; 35, quenching cooling chamber; 36, furnace roof inlet; 37, burner hearth; 38, water-cooled coil pipe; 39, refractory masses; 40, vapourizing furnace shell; 41, water distributor; 42, sending down abnormally ascending pipe; 43, riser; 44, preset pieces; 45, bubbling cooling bath; 46, lock slag valve; 47, lock bucket; 48, vent valves; 49, grey water-circulating pump; 50, Liquid level adjusting valve; 51, air water separator; 52, baffle plate; 53, soak into washer; 54, gas wash tower; 55, eddy flow plate; 56, tower tray; 57, traverse baffle; 58, downtake; 59, upcast; 60, water-bath storage tank; 61, Liquid level adjusting valve; 62, high-pressure process softened water pump; 63, central duct; 64, cooling medium channel; 65, dry coal dust passage; 66, vaporized chemical medium channel; 67, high-temperature water heater; 68, secondary step-down transformer; 69, vacuum evaporator; 70, feeding pump; 71, clarification separate tank; 72, vacuum band-type filter machine; 73, aqua storage tank; 74, grey water pump; 75, degasification water pot; 76, degasification water pump; 77, negative pressure condenser; 78, negative pressure separator; 79, gas is through baffle plate; 80, off-gas pump; 81, off-gas pump separator; 82, gas is through baffle plate; 83, buck heating device; 84, gas-liquid mixed separating tank; 85, liquid barrier; 86, gas condenser; 87, filter feeding pump; 88, high-temperature water downtake; 89, vapour mixture upcast; 90, technology cooling soft water inhalent siphon; 91, outlet pipe.
[embodiment]
Embodiment 1: according to the inventive method is the raw material production synthetic gas with the coal dust
Use the method for Shaanxi shenfu coal as the raw material embodiment of the present invention.Said raw material thermal value: 27070J/g, principal element analytical results are listed in the table below in 1:
Table 1: the principal element analytical results of Shaanxi shenfu coal
Implementation step is following:
The preparation of A, dry coal dust: after the Shaanxi shenfu coal removed the iron that wherein possibly exist with magnet; Re-use Shanghai magnificent machinofacture far away company limited and produce impact breaker and be crushed to the coal grain of granularity, allow this coal grain be promoted to feed bin 6 then through bucket elevator 5 less than 30mm.Coal grain in the feed bin is quantitatively sent into grinding machine 8 by feeding machine 7, and grinding machine grinds to form coal dust to the coal grain, and the abundant heat exchange of hot blast that allows described coal dust and hotblast stove 1 send here is simultaneously carried out drying to coal, makes wherein water content by weight≤2.0%.Described coal dust is carried secretly at hot blast and is got into down powder selector 9, and wherein 100% coal dust of granularity＜0.10mm drives at hot blast and gets into powder collector 10 down, and all the other coal dusts dependence self gravitations than volume particle size return grinding machine 8 and grind.Powder collector 10 is connected with induced draft fan 12, under the effect of induced draft fan 12, removes the steam of the water that dry hot gas and coal discharge in the powder collector 10.Fly-ash separator 11 is arranged at powder collector 10 tops, to reduce the dust content of discharging the gas from powder collector 10.The dry coal dust of discharging from powder collector 10 bottoms is sent into follow-up workshop section and is used.
B, dry coal dust positive delivery: the dry coal dust by above-mentioned steps A preparation is delivered in the coal dust warehouse 14; Dry coal dust in the coal dust warehouse 14 is delivered to 16 imports of fine coal positive delivery device through valve 15 and pipeline; Dry coal dust is brought up to 5.0MPa through fine coal positive delivery device with coal dust pressure, arrives hopper 17 through pipe-line transportation again; Described coal dust is transported to vapourizing furnace 33 through hopper outlet valve 19 after measuring through electronic scales 18; The dusty gas of discharging from coal dust warehouse 14 is discharged into atmosphere through cyclonic separator 13 gas separated from cyclonic separator 13 tops, and solid returns the recycle of coal dust warehouse.
The pressurized high-temperature of C, dry coal dust gasification: the superheated vapour that feeds 380 ℃ of purity by volume 99.6% oxygen and temperature through multithread road spraying burner 32; These dry coal dusts are sent in spraying burner 32 exits forth in the multithread road; And make they and dry coal dust under the condition of 1350 ℃～1600 ℃ of temperature, pressure 4.0MPa, carry out violent incomplete combustion reaction, generate and contain CO, H
2And CO
2The high temperature crude synthesis gas of main component obtains the melting slag mixture.In the present embodiment, the dry pulverized coal flow of sending into vapourizing furnace 33 is 500t/d, and oxygen flow is 12347.67Nm
3/ h, steam flow are 4983.72kg/h.
D; The high temperature crude synthesis gas; Molten ash cooling and crude synthesis gas washing, purifying: the high temperature crude synthesis gas of generation; The melting slag mixture; The water coolant of unconverted carbon and the flow 78417kg/h through water distributor 41 is together through sending down abnormally ascending pipe 42 and flow into bottom bubbling cooling bath 45; After ash is washed in 45 coolings of bubbling cooling bath; Said crude synthesis gas leaves moisture-free coal powder pressure gasifying stove 33 along the upper end of the annular space between sending down abnormally ascending pipe 42 and the riser 43; 223 ℃ of the temperature of this crude synthesis gas; Pressure 3.74MPa; The gaseous constituent of this crude synthesis gas and flow thereof are according to the GB/T17132-1997 assay determination; The thin ash content of this crude synthesis gas is according to the GB/T1574-1995 assay determination, and these analytical resultss are listed in the table below in 2.The thick slag temperature of discharging from lock bucket 47 is 76 ℃, and flow is in butt 1333kg/h.
Table 2: the gaseous constituent of crude synthesis gas and flow thereof and thick slag flow
Is that the buck of 41504kg/h gets into and soaks into washer 53 from the crude synthesis gas of moisture-free coal powder pressure gasifying stove 33 with the flow behind grey water-circulating pump 49 pressure-raisings of passing through from gas wash tower 54; Mix through soaking into washer 53; Through sending into follow-up system as unstripped gas after gas wash tower 54 ash disposal; Ash content in this washing synthetic gas is analyzed according to GB/T1574-1995, and its ash content is reduced to less than 0.8mg/Nm
3, 216.88 ℃ of temperature, pressure 3.74MPa, the gaseous constituent and the flow of this washing synthetic gas are analyzed according to GB/T17132-1997, and its analytical results is listed in the table 3:
Table 3: the gaseous constituent and the flow thereof of this washing synthetic gas
E, contain thin grey water handing: contain thin buck from what moisture-free coal powder pressure gasifying stove 33 quenching cooling chamber discharged; After step-down, send in the high-temperature water heater 67 who contains thin grey water handing part from the thin buck that contains that gas wash tower 54 is discharged; Meanwhile the phlegma of lower procedure is also delivered among the high-temperature water heater 67; Wherein the temperature that contains thin buck of discharging from moisture-free coal powder pressure gasifying stove 33 quenching cooling chamber is 223 ℃; Flow 46532kg/h, thin ash content by weight 1.83%; The temperature that contains thin buck of discharging from gas wash tower 54 is 218 ℃, and flow 22090kg/h, thin ash content by weight 1.79%; The temperature of this phlegma is 95 ℃, flow 14500kg/h.Said thin buck and the said phlegma of containing carries out the step-down cooling through high-temperature water heater 67, is 0.9MPa with pressure-controlling, is dissolved in gas in the water and overflows and get into buck heating device 83, evolving gas total flux 10669.04Nm
3/ h, wherein the steam content by volume 99.2%, 179 ℃ of temperature, gaseous constituent and flow are to analyze according to GB/T17132-1997, its analytical results is listed in the table 4.
Table 4: the gaseous fraction of synthetic gas and flow thereof
The circulation buck heat temperature raising that the mixed gas that comes out from high-temperature water heater 67 is sent here water pump 75 at the bottom of the degasification water pot in buck heating device 83; Its circulating ash discharge is 68929.51kg/h; 109 ℃ of temperature; 148.6 ℃ of circulating ash discharge 68929.51kg/h after the intensification, temperature arrive bottom bubbling style water-bath storage tank 60 through gas wash tower 54 middle and lower part imports; The air-water mixture of discharging from buck heating device 83 is 1072Nm with the gas flow
3/ h, liquid water flow 7838kg/h delivers to gas-liquid mixed separating tank 84, discharge from the top through gas-liquid mixed separating tank 84 back gases, and isolating buck returns degasification water pot 75 for 105 ℃ with flow 7838kg/h, temperature; 67 of high-temperature water heaters are spissated to be contained thin buck and delivers to secondary step-down transformer 68 with flow 75489.23kg/h, thin ash content 1.58% (weight); Under 0.15MPa (G), 128 ℃ of conditions, carry out rapid evaporation, vaporized gas is directly sent into degasification water pot 75 through interchanger 86 coolings or through bypass.The concentrated thin buck that secondary step-down transformer 68 comes out gets in the vacuum evaporator 69; Meanwhile the pulp water of cinder slag discharge unit is delivered to vacuum evaporator 69 with flow 41061kg/h, thin ash content 1.2% weight; Vacuum evaporator is controlled at 68.7 ℃ of pressure-0.07MPa, temperature, by vacuum evaporator 69 top escaping gas with flow 8662.53Nm
3/ h; Behind negative pressure condenser 77, deliver to negative pressure separator 78; Gas is delivered to off-gas pump 80 after separating moisture; Negative pressure separator 78 parting liquids get into aqua storage tank 73 with flow 7547kg/h, and vacuum evaporator 69 bottom concentrated solutions are delivered to clarification separate tank 71 with flow 144458.50kg/h, thin ash content 1.6% (weight) through clarification separate tank feeding pump 70.Thin ash in the said concentrated solution is carrying out natural subsidence in said concentrated solution weight 0.001%, molecular weight under the effect of 1200～1,500 ten thousand polyacrylamide flocculants; Then through sending into vacuum band-type filter machine 72 after 87 pressurizations of filter feeding pump; Filtration obtains the thin ash of concentration 50% (weight), flow 1406.68kg/h, and its filtrating turns back to clarification separate tank 71 with flow 6523.93kg/h.Clarification separate tank 71 overflow waters are delivered to aqua storage tank 73 with flow 143052kg/h, and off-gas pump separator 81 isolating bucks flow to this aqua storage tank 73 with buck total flux 4977kg/h simultaneously.All water fractions behind grey water pump 74 pressure-raisings that flow into aqua storage tank 73 efflux processing with flow 17795kg/h; A part is delivered to degasification water pot 75 with flow 42569kg/h; A part is returned as flushing water and cold pulp water with flow 95212kg/h; Degasification water pot 75 also needs to replenish a part of water with total flow 26360.51kg/h simultaneously; Condensate liquid and Yuan Shui comprising follow-up system; In degasification water pot 75, add Tianjin Chemical Research & Desing Inst with trade name high temperature dirt dispersion agent product sold dispersant; Addition is in buck weight 65ppm in the degasification water pot 75; Allow after the on-condensible gas emptying of dissolving in the water; Buck is delivered to buck heating device 83 for 109 ℃ with flow 68929.51kg/h, temperature behind degasification water pump 76 pressure-raisings; Be elevated to 148.6 ℃ from high-temperature water heater's 67 top step-down effusion vapour temperature after heating, delivered to bubble type water-bath storage tank 60 by gas scrubbing tower 54 middle and lower part imports again.
Embodiment 1 use Shaanxi shenfu coal is as the method for raw material embodiment of the present invention, and this coal is the more shallow low ash of metamorphic grade, the long-flame coal of low ash smelting point.Present embodiment uses ash-rich, high ash melting point, the dark Huainan meager coal of metamorphic grade to be raw material.Said raw material thermal value: 22590J/g, the principal element analytical results is following:
Implementation step is following:
The preparation of A, dry coal dust: after Huainan coal removed the iron that wherein possibly exist with magnet, use impact breaker to be crushed to granularity, allow this coal grain be promoted to feed bin 6 then through bucket elevator 5 less than 30mm.Coal grain in the feed bin is quantitatively sent into grinding machine 8 by feeding machine 7, and grinding machine grinds the coal grain, and the abundant heat exchange of sending here with hotblast stove 1 of hot blast is carried out drying to coal simultaneously, makes wherein water content≤2.0% (weight).Coal dust is carried secretly at hot blast and is got into powder selector 9 down, and relatively large particulate coal wherein relies on self gravitation to return grinding machine 8 and further grinds, and the coal dust of remaining granularity 100%＜0.10mm gets into powder collector 10 under the strength effect.Powder collector 10 is connected with induced draft fan 12, the water vapor of under the effect of induced draft fan, removing dry hot gas in the powder collector and from coal, separating out.Fly-ash separator 11 is arranged at powder collector 10 tops, is used to guarantee out the cleaning of powder collector 10 gases.Send into the use of follow-up workshop section from the dry coal dust that powder collector 10 gets off.
B, dry coal dust positive delivery: the coal dust that is prepared by above-mentioned steps A is sent in the coal dust warehouse 14; Dry coal dust in the coal dust warehouse 14 enters into 16 imports of fine coal positive delivery device through the valve 15 of bottom with pipeline; Dry coal dust is brought up to 5.0MPa (G) through fine coal positive delivery device with coal dust pressure, arrives hopper 17 through pipe-line transportation again; Described coal dust is transported to vapourizing furnace 33 through hopper outlet valve 19 after measuring through electronic scales 18; The dusty gas of discharging from coal dust warehouse 14 is discharged into atmosphere through cyclonic separator 13 gas separated from cyclonic separator 13 tops, and solid returns the recycle of coal dust warehouse.
The pressurized high-temperature of C, dry coal dust gasification: the superheated vapour that feeds 380 ℃ of purity by volume 99.6% oxygen and temperature through multithread road spraying burner 32; These dry coal dusts are sent in spraying burner 32 exits forth in the multithread road; And make they and dry coal dust under the condition of 1350 ℃～1600 ℃ of temperature, pressure～4.0MPa, carry out violent incomplete combustion reaction, generate and contain CO, H
2And CO
2The high temperature crude synthesis gas of main ingredient and the mixture of fusion warm sludge.The dry coal dust amount that gets into vapourizing furnace 33 is 500t/d, and amount of oxygen is 10842.46Nm
3/ h, quantity of steam are 3477.41kg/h.
D; The high temperature crude synthesis gas; Molten ash cooling and crude synthesis gas washing, purifying: the high temperature crude synthesis gas of generation; The fusion warm sludge; The water coolant of unconverted carbon and the flow 78417kg/h that gets into water distributor 41 is through sending down abnormally ascending pipe 42 and flow into bottom bubbling cooling bath 45;, 45 coolings of bubbling cooling bath leave moisture-free coal powder pressure gasifying stove 33 after washing ash along the annular space between sending down abnormally ascending pipe 42 and the riser 43; 226 ℃ of its temperature; Pressure 3.74MPa; Gaseous constituent and flow thereof are analyzed according to GB/T17132-1997; Thin ash content is analyzed according to GB/T1574-1995; These analytical resultss are listed in the table below 1; Ash content in unconverted carbon and the raw material is discharged through lock bucket 47 with thick slag form; This thick slag temperature is 76 ℃, and flow is in butt 4275.90kg/h.
Table 1
Is that the buck of 41000kg/h gets into and soaks into washer 53 from the crude synthesis gas of moisture-free coal powder pressure gasifying stove 33 with the flow behind grey water-circulating pump 49 pressure-raisings of passing through from gas wash tower 54; Mix through soaking into washer 53; Through sending into follow-up system as unstripped gas after gas wash tower 54 ash disposal; Ash content in the unstripped gas of washing back is analyzed according to GB/T1574-1995, and its ash content is reduced to less than 1mg/Nm
3, 216.88 ℃ of temperature, pressure 3.74MPa, gaseous constituent and flow are analyzed according to GB/T17132-1997, and its analytical results is listed in table 2:
Table 2
E, contain thin grey water handing: contain thin buck from what moisture-free coal powder pressure gasifying stove 33 quenching cooling chamber discharged; After step-down, send in the high-temperature water heater 67 who contains thin grey water handing part from the thin buck that contains that gas wash tower 54 is discharged; Meanwhile the phlegma of lower procedure is also delivered among the high-temperature water heater 67; Wherein the temperature that contains thin buck of discharging from dry coal dust gas pressurized-gasification furnace 33 quenching cooling chamber is 221 ℃; Flow 45500kg/h, thin ash content 2.1% (weight); The temperature that contains thin buck that gas wash tower 17 is discharged is 217 ℃, flow 23000kg/h, thin ash content 1.85% (weight); The temperature of this phlegma is 95 ℃, flow 14500kg/h.Said thin buck and the said phlegma of containing carries out the step-down cooling through high-temperature water heater 67, is 0.5MPa with pressure-controlling, is dissolved in gas in the water and overflows and get into buck heating device 83, evolving gas total flux 10338.78Nm
3/ h, steam content 99.4% (volume) wherein, 179 ℃ of temperature, gaseous constituent and flow are to analyze according to GB/T17132-1997, its analytical results is listed in table 3.
Table 3
The circulation buck heat temperature raising that the mixed gas that comes out from high-temperature water heater 67 is sent here degasification water pump 76 in buck heating device 83; Its circulating ash discharge is 69000kg/h; 109 ℃ of temperature, the circulation buck after the intensification are passed through gas wash tower 54 middle and lower part imports with 162.5 ℃ of grey discharge 69000kg/h temperature and are arrived bottom bubbling style water-bath storage tanks 60; The air-water mixture that goes out buck heating device 83 is 1025Nm with the gas flow
3/ h, liquid water flow 7484.29kg/h delivers to gas-liquid mixed separating tank 84, discharge from the top through gas-liquid mixed separating tank 84 back gases, and isolating buck returns degasification water pot 75 for 105 ℃ with flow 7484.29kg/h, temperature; 67 of high-temperature water heaters are spissated to be contained thin buck and delivers to secondary step-down transformer 68 with flow 74965.64kg/h, thin ash content 2.21% (weight); Under 0.15MPaG, 128 ℃ of conditions, carry out rapid evaporation, vaporized gas is directly sent into degasification water pot 75 through interchanger 86 coolings or through bypass.The concentrated thin buck that secondary step-down transformer 68 comes out gets in the vacuum evaporator 69; Meanwhile; The pulp water of cinder slag discharge unit is delivered to vacuum evaporator 69 with flow 47173kg/h, thin ash content 1.8% (weight); Vacuum evaporator is controlled at 68.7 ℃ of pressure-0.07MPa, temperature, by vacuum evaporator 69 top escaping gas with flow 8554.53Nm
3/ h; Behind negative pressure condenser 77, deliver to negative pressure separator 78; Gas is delivered to off-gas pump 80 after separating moisture; Negative pressure separator 78 parting liquids get into aqua storage tank 73 with flow 7465kg/h, and vacuum evaporator 69 bottom concentrated solutions are delivered to clarification separate tank 71 with flow 120566.50kg/h, thin ash content 2.3% weight through clarification separate tank feeding pump 70.Thin ash in the said concentrated solution is carrying out natural subsidence in said concentrated solution weight 0.001%, molecular weight under the effect of 1200～1,500 ten thousand polyacrylamide flocculants; Then through sending into vacuum band-type filter machine 72 after 87 pressurizations of filter feeding pump; Filtration obtains the thin ash of concentration 50% (weight), flow 4642.55kg/h, and its filtrating turns back to clarification separate tank 71 with flow 1989.67kg/h.Clarification separate tank 71 overflow waters are delivered to aqua storage tank 73 with flow 115923.95kg/h, and off-gas pump separator 81 isolating bucks flow to this aqua storage tank 73 with buck total flux 4977kg/h simultaneously.All water fractions behind grey water pump 74 pressure-raisings that flow into aqua storage tank 73 efflux processing with flow 22000kg/h; A part is delivered to degasification water pot 75 with flow 11065.95kg/h; A part is returned as flushing water and cold pulp water with flow 95300kg/h; Degasification water pot 75 also needs to replenish a part of water with total flow 57934.05kg/h simultaneously; Condensate liquid and Yuan Shui comprising follow-up system; In degasification water pot 75, add Tianjin Chemical Research & Desing Inst with trade name high temperature dirt dispersion agent product sold dispersant; Addition is in buck weight 65ppm in the degasification water pot 75; Allow after the on-condensible gas emptying of dissolving in the water; Buck is delivered to buck heating device 83 for 109 ℃ with flow 69000kg/h, temperature behind degasification water pump 76 pressure-raisings; Be elevated to 162.5 ℃ from high-temperature water heater's 67 top step-down effusion vapour temperature after heating, delivered to bubble type water-bath storage tank 60 by gas scrubbing tower 54 middle and lower part imports again.
Claims (10)
1. one kind is the method for raw material production synthetic gas with the coal dust, it is characterized in that this method comprises the steps:
The preparation of A, dry coal dust: coal raw materials is removed irony class impurity wherein through tramp iron separator (2); By belt weighing feeding machine (3) Weighing; Get into the broken coal-forming grain of crusher (4); Described coal grain is promoted to feed bin (6) through bucket elevator (5); Quantitatively send into grinding machine (8) by feeding machine (7) again and grind to form coal dust; When grinding, allow the hot blast of hotblast stove (1) and described coal dust carry out abundant heat exchange, make its coal dust be dried to water content by weight≤2.0%; Described coal dust drives at hot blast and gets into powder selector (9) down, and wherein 100% coal dust of granularity＜0.10mm drives entering powder collector (10) down at hot blast, and all the other coal dusts dependence self gravitations than volume particle size return grinding machine (8) and grind; Described powder collector (10) is connected with induced draft fan (12), under the effect of induced draft fan (12), removes the steam of the water that dry hot gas and coal in the powder collector (10) discharge; Described powder collector (10) is provided with fly-ash separator (11) at the top, discharge the dust content the gas to reduce from powder collector (10); The dry coal dust of discharging from powder collector (10) bottom is sent into follow-up workshop section and is handled;
B, dry coal dust positive delivery: the dry coal dust by above-mentioned steps A preparation passes through pipe-line transportation in coal dust warehouse (14), is transported to fine coal positive delivery device (16) through valve (15) then; Said coal dust warehouse (14) and both difference of altitude of said fine coal positive delivery device (16) are the 10-30% of said coal dust warehouse (14) height, are 0.10MPa at least with the intake pressure that guarantees fine coal positive delivery device (16); Drive fine coal positive delivery device (16) through electric motor (M) then, dry coal dust pressure is brought up to 0.5～7.0MPa, arrive hopper (17) through pipe-line transportation again; Described coal dust is transported to vapourizing furnace (33) through hopper outlet valve (19) after measuring through electronic scales (18); The dusty gas of discharging from coal dust warehouse (14) is discharged into atmosphere through cyclonic separator (13) gas separated from cyclonic separator (13) top, and solid returns the recycle of coal dust warehouse.
Perhaps by above-mentioned steps A) the dry coal dust of preparation sends into normal pressure powder storehouse (21), and when the pressure of the pressure in normal pressure powder storehouse (21) and lock gas hopper (22) reached balance, dry coal dust got into lock gas hopper (22) through normal pressure powder storehouse (21) bottom valve (25); When the material level of lock gas hopper (22) reaches predetermined material level value; Close normal pressure powder storehouse (21) bottom valve (25); Fill high-pressure inert gas toward lock gas hopper (22) then; When the pressure of the pressure of locking gas hopper (22) and feeder (23) reaches balance; Open lock gas hopper (22) bottom valve (26); Dry coal dust gets into feeder (23) through this valve (26); Carrier gas by the input of feeder (23) bottom makes the dry coal dust fluidisation that gets into feeder (23); The fluidized drying coal dust is discharged from feeder (23) top, delivers to vapourizing furnace (33) through pipeline; When lock gas hopper (22) material level is lower than predetermined material level value; Lock gas hopper (22) bottom valve (26) is closed; The discharge degree that to lock gas hopper (22) through pipeline is to cyclonic separator (20); When the pressure of lock gas hopper (22) is reduced to normal pressure; Open normal pressure powder storehouse (21) bottom valve (25); Allow the interior dry coal dust in normal pressure storehouse (21) get into lock gas hopper (22), continue the recycle feed program; The dusty gas of being discharged by normal pressure powder storehouse (21), lock gas hopper (22) carries out gas through cyclonic separator (20) to be separated with solid; Gas separated is discharged into atmosphere from cyclonic separator (20) top, and solid separated is returned the storehouse recycle of normal pressure powder through returning valve (24);
The pressurized high-temperature gasification of C, dry coal dust: the dry coal dust that above-mentioned steps B obtains is delivered to multithread road spraying burner (32) inlet that is positioned at moisture-free coal powder pressure gasifying stove (33) top and passed through it; Spraying burner (32) outlet in the multithread road; Vaporized chemical through multithread road spraying burner (32) is sprayed onto dry coal dust in the reaction chamber (34) of moisture-free coal powder pressure gasifying stove (33); And make its vaporized chemical and dry coal dust under the condition of 1350 ℃-1600 ℃ of temperature and pressure 0.1～6.0MPa, carry out combustion reactions, generate and contain CO, H
2And CO
2Be the high temperature crude synthesis gas of main ingredient and the mixture of molten ash;
Described multithread road spraying burner (32) is the coaxial textural association equipment that is nested of a kind of multitube, and it is made up of central duct (63), cooling medium channel (64), vaporized chemical medium channel (66) and dry coal dust passage (65); This multithread road spraying burner (32) is provided with a cooling system, and this cooling system is made up of with pump (30) cooling trough (28), cooling tube (29); Be contained in water in the cooling trough (28) after cooling tube (29) cooling; Again through pump (30) pressurized stream through the multithread road spraying burner (32); Make the temperature of multithread road spraying burner (32) keep stable; The effusive water of spraying burner (32) returns cooling trough (28) again from the multithread road, through recycling after the cooling of the water-cooled tube (29) in the cooling trough (28);
Described moisture-free coal powder pressure gasifying stove (33) is a cylindrical tube, and the top of this vapourizing furnace is reaction chamber (34), and the bottom is quenching cooling chamber (35); Reaction chamber (34) comprises furnace roof inlet (36), burner hearth (37), the water-cooled coil pipe (38) around burner hearth, the refractory masses (39) of protecting the water-cooled coil pipe and vapourizing furnace shell (40); Furnace roof inlet (36) is connected with said multithread road spraying burner (32); Described quenching cooling chamber (35) is provided with water distributor (41), sending down abnormally ascending pipe (42) and riser (43); Sending down abnormally ascending pipe (42) upper end is connected fixing with water distributor (41); Riser (43) is supported on quenching cooling chamber (35) housing; Sending down abnormally ascending pipe (42) and riser (43) arranged concentric; An annular space is arranged between the two, and be fixed together with preset pieces (44);
D; The high temperature crude synthesis gas; Molten ash cooling and crude synthesis gas washing, purifying: in quenching cooling chamber (35); The high temperature crude synthesis gas and the molten ash mixture that allow step C obtain mix and cooling with the water coolant through sending down abnormally ascending pipe (42) entering bubbling cooling bath (45) that is got into by said water distributor (41); The cinder slag is deposited in quenching cooling chamber (35) bottom because of sudden cold-curing; The crude synthesis gas that contains a small amount of thin ash and water rises along the annular space between sending down abnormally ascending pipe (42) and the riser (43); In the annular space upper end; A part of water that said crude synthesis gas contains turns back in the bubbling cooling bath (45) along sending down abnormally ascending pipe (42) inwall with thin ash, and remaining crude synthesis gas goes out vapourizing furnace (33) through row of conduits; Cinder slag in quenching cooling chamber (35) bottom gets into lock bucket (47) through lock slag valve (46), discharges through vent valves (48), and the water that contains thin ash that the cinder slag is carried secretly is delivered to the vacuum evaporator (69) of water treatment portion;
The crude synthesis gas that contains thin buck of discharging from vapourizing furnace (33) perhaps gets into air water separator (51); The water that synthetic gas is carried secretly is through after separating; And further remove the thin buck of carrying secretly in the raw gas that contains through baffle plate (52); These contain thin buck sends to through pipeline after reducing pressure and carries out thin grey water handing, removes the crude synthesis gas that contains thin buck and delivers to through pipeline and soak into washer (53); Perhaps the crude synthesis gas that contains thin buck of discharging from vapourizing furnace (33) is directly delivered to through pipeline and is soaked into washer (53); In soaking into washer (53); Allow the crude synthesis gas that contains thin buck and buck thorough mixing from gas wash tower (54); Get into gas wash tower (54) through pipeline then; Arriving bubbling style water-bath storage tank (60) along downtake (58) again washs; Said crude synthesis gas rises along the annular space that between downtake (58) and upcast (59), forms again; And carry out multistage washing through traverse baffle (57), tower tray (56), eddy flow plate (55); Discharge along pipeline from gas wash tower (54) top through scum dredger (27) back, obtain a kind of synthetic gas; Buck in the bubbling style water-bath storage tank (60) gets into grey water-circulating pump (49) through pipeline; Separated into two parts behind grey water-circulating pump (49) pressure-raising; A part is sent into along pipeline and is soaked into washer (53), and the water distributor (41) that another part is sent into dry coal powder pressure gasifying stove (33) cinder notch below through pipeline is used as water coolant;
E, contain thin grey water handing: gas wash tower (54) bubbling style water-bath storage tank (60) bottom contains thin buck and reduces pressure through Liquid level adjusting valve (50) through the thin buck that contains that Liquid level adjusting valve (61) decompression, quenching cooling chamber discharge; Contain thin buck and get into high-temperature water heater (67) and carry out the step-down cooling with decompression back air water separator (51) is isolating, escaping gas gets into buck heating device (83) and reclaims heat from high-temperature water heater (67) top; The thin buck that contains of discharging from high-temperature water heater (67) bottom gets into secondary step-down transformer (68) recovery heat; The steam of overflowing from secondary step-down transformer (68) top gets into degasification water pot (75) and reclaims heat, and the thin buck that contains of discharging from secondary step-down transformer (68) bottom gets into vacuum evaporator (69) step-down cooling; After negative pressure condenser (77) cooling cooling, get into negative pressure separator (78) from vacuum evaporator (69) top escaping gas; Gas gets into off-gas pump (80) after baffle plate (79) separates moisture; Again through off-gas pump separator (81) gas-liquid separation; Gas emptying after baffle plate (82) separates moisture; The isolating water of isolating water of off-gas pump separator (81) and negative pressure separator (78) flows into aqua storage tank (73), and the thin buck that contains of discharging from vacuum evaporator (69) bottom gets into clarification separate tank (71) behind clarification separate tank feeding pump (70) pressure-raising; In clarification separate tank (71), add the water treatment organic polymer coargulator and make thin grey suspended substance flocculation; The top overflow water of clarification separate tank (71) flows into aqua storage tank (73); The buck of aqua storage tank (73) part behind grey water pump (74) pressure-raising is sent into degasification water pot (75); A part is as wash-down water, and few part effluxes; Buck in the degasification water pot (75) is through the gas that adds heat extraction and wherein carried secretly and drain, simultaneously degasification water pot (75) outlet or degasification water pot (75) in the adding dispersion agent, to alleviate the fouling of interchanger and ash-water pipeline; The degasification buck is gone into buck heating device (83) through degasification water pump (76) pressure-raising is laggard, and with the escaping gas heat exchange heats up from high-temperature water heater (67) top, the bubbling style water-bath storage tank (60) of delivering to gas wash tower (54) then recycles again; Clarification separate tank (71) bottom ash content higher thin buck gets into vacuum band-type filter machine (72) and carries out separating of thin ash and water after filter feeding pump (87) supercharging, described thin ash is collected the back and discharged, and isolating water turns back in the clarification separate tank (71) again.
2. method according to claim 1 is characterized in that described coal raw materials is selected from hard coal, bituminous coal, brown coal or thermal value Q
B.adOther carbon solid raw material of＞17000kJ/kg.
3. method according to claim 1 is characterized in that described vaporized chemical is selected from air, oxygen-rich air, pure oxygen, CO
2Or superheated vapour.
4. method according to claim 1 is characterized in that described vaporized chemical and dry coal dust carry out combustion reactions under the condition of 1350 ℃-1600 ℃ of temperature, pressure 0.1～6.0MPa.
5. method according to claim 1; It is characterized in that described moisture-free coal powder pressure gasifying Reaktionsofen (33) is a cylindrical tube; Its reaction chamber (34) mainly is made up of water-cooled coil pipe and withstand voltage heat-resistance high-strength degree steel plate; Reaction chamber (34) height is 4-5 with the ratio of mean diameter, and reaction chamber (34) is 1 with the ratio of the height of bottom quenching cooling chamber (35): 1-3.
6. method according to claim 1 is characterized in that in gasification reacting furnace (33), is formed by 1 to 6 steel pipe coiling around the water-cooled coil pipe (38) of burner hearth.The water coolant of water-cooled coil pipe is the feedwater through desalting treatment.
7. method according to claim 1; It is characterized in that said moisture-free coal powder pressure gasifying Reaktionsofen (33) comprises a heat reclamation device, this device can be the natural convection heat reclamation device that comprises many water-cooled coil pipes (38), high-temperature water and vapour mixture upcast (89), high-temperature water downtake (88), dry pipe (31); Perhaps this device also can be to comprise single water-cooled coil pipe (38), the outlet pipe (91) of technology cooling soft water inhalent siphon (90), high-temperature water or high pressure steam or both mixtures, the pump circulation heat reclamation device of high-pressure process softened water pump (62).
8. method according to claim 1 is characterized in that said coal dust warehouse (14) and both difference of altitude of said fine coal positive delivery device (16) are the 15-25% of said coal dust warehouse (14) height.
9. method according to claim 2 is characterized in that described indifferent gas is selected from nitrogen, argon gas or their mixture; Described carrier gas is nitrogen or air.
10. method according to claim 1 is characterized in that institute's gas wash tower (54) dedusting washing measure comprises washing water-bath (60), traverse baffle (57), tower tray (56), eddy flow plate (55), scum dredger (27).
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1721511A (en) * | 2005-07-01 | 2006-01-18 | 煤炭科学研究总院北京煤化工研究分院 | Process for pressurized gasification of dry coal fines |
| CN1746270A (en) * | 2005-10-18 | 2006-03-15 | 西北化工研究院 | Gasification of dry-powder solid fuel |
| WO2009020442A1 (en) * | 2007-08-03 | 2009-02-12 | Detes Maden Enerji Ve Cevre Teknoloji Sistemleri Limited Sirketi | Solid fuel gasification and gas cleaning system |
| CN101982528A (en) * | 2010-11-23 | 2011-03-02 | 神华集团有限责任公司 | Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof |
| US20110173885A1 (en) * | 2010-01-19 | 2011-07-21 | Hatch Ltd. | Atmospheric pressure gasification process and system |
-
2011
- 2011-09-08 CN CN 201110264937 patent/CN102352268B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1721511A (en) * | 2005-07-01 | 2006-01-18 | 煤炭科学研究总院北京煤化工研究分院 | Process for pressurized gasification of dry coal fines |
| CN1746270A (en) * | 2005-10-18 | 2006-03-15 | 西北化工研究院 | Gasification of dry-powder solid fuel |
| WO2009020442A1 (en) * | 2007-08-03 | 2009-02-12 | Detes Maden Enerji Ve Cevre Teknoloji Sistemleri Limited Sirketi | Solid fuel gasification and gas cleaning system |
| US20110173885A1 (en) * | 2010-01-19 | 2011-07-21 | Hatch Ltd. | Atmospheric pressure gasification process and system |
| CN101982528A (en) * | 2010-11-23 | 2011-03-02 | 神华集团有限责任公司 | Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof |
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