CN1032746A - The design of feeder - Google Patents
The design of feeder Download PDFInfo
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- CN1032746A CN1032746A CN 88106710 CN88106710A CN1032746A CN 1032746 A CN1032746 A CN 1032746A CN 88106710 CN88106710 CN 88106710 CN 88106710 A CN88106710 A CN 88106710A CN 1032746 A CN1032746 A CN 1032746A
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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]
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Abstract
A kind of stable equipment and method of flow rate maintenance that is discharged to the flammable particulate solids (for example coal grain) and the gaseous mixture of pressurization acceptable response device (for example gasifier) by feeder equipment that be used to make equably.
Description
The present invention relates to a kind of be used to make by feeder be discharged to the particulate solids of acceptable response device equably and the flow rate of gaseous mixture keeps stable method and apparatus.Specifically, the present invention relates to a kind of be used to make by feeder (preferably having a plurality of outlets) be discharged to the coal dust of making the pressing gas reactor (hereinafter claiming gasifier) that synthetic gas uses equably and the flow rate of gaseous mixture keeps stable method and apparatus.More particularly, the present invention relates to a kind of stable method and apparatus of mass flow rate maintenance that is used to make the dry coal grain that enters reactor.
The various equipment that are easy to mobile material (for example grain) by gravity that are used for discharging had been had already.Though at U.S. Patent application the 3rd, 289,396 and 3,367, those disclosed equipment can guarantee from main storage tank exhaust particulate matter matter effectively in No. 724, and can prevent to build bridge and this class storage tank discharge incomplete, can make like this by feeder and be discharged to the particulate solids of acceptable response device of pressurization equably and the flow rate of gaseous mixture keeps stable but these equipment can not resemble the present invention with a plurality of outlets.
The objective of the invention is to overcome technical this problem.
Therefore, the invention provides a kind of be used to the make solids of the reactor that is discharged to acceptance equably and the stable feeder equipment of flow rate maintenance of gaseous mixture.The feature of this equipment is:
The bottom has the relief outlet pressurizing vessel that is used to discharge described solids and gaseous mixture;
At least two geometrical shape containers identical, that have the downward cone-shaped wall of awl point;
Described container respectively has an inlet hole of accepting described mixture on its top, an outlet opening of discharging described mixture is respectively arranged in its bottom;
The position of described container is adjacent one another are and crossing, forms between the total face of the void between the two in intersection, and the bottom of this intersection is to have on the specific range of horizontal plane in the void perpendicular to this two containers relief outlet.
The present invention also provides a kind of and is used to make the solids that are aligned to pressurization acceptable response device equably and the flow rate of gaseous mixture to keep stable method.The method is characterized in that and have following all steps:
Mixture is introduced pressurizing vessel, and this pressurizing vessel has at least two geometrical shapies identical and be placed on container in this pressurizing vessel basically, and each container all is useful on the outlet opening of the described mixture of discharge;
The control mixture is by the flow rate of described container outlet opening separately, and its method is the flow rate of control via first gas of the wall injection of container bottom;
Through described outlet of container hole, mixture is discharged to described acceptable response device;
Keep the pressure of described pressurizing vessel, make it be higher than the pressure of described acceptable response device.
Below by enumerating embodiment and the present invention being done comparatively detailed description with reference to accompanying drawing.In the accompanying drawing:
Fig. 1 represents the sectional view of one embodiment of this invention.
Fig. 2 is the elevated bottom perspective internal view of the present invention's one advantageous embodiment.
Fig. 3 is I-I sectional view of Fig. 1.
Fig. 4 represents to be used to make the fluctuation of activity or catalytic solid particle and gas mixture quality flow rate to be reduced to the synoptic diagram of the equipment of minimum degree.
Fig. 5 is the sectional view of element 50 among Fig. 4.
Fig. 6 is the schema of the embodiment of replaceable embodiment shown in Figure 4.
In gasification, synthesis gas is in the situation that oxygen or oxygen-containing gas (for example mixture of air or air and oxygen) arranged, and carries out by making hydrocarbon fuel (for example coal) that partial combustion produces under the pressure of 800～2000 ℃ higher temperatures and 1～200 bar in gasifier. In of the present invention one favourable embodiment, the mixture of fuel and gas is discharged from a feeder equipment, this feeder preferably have a plurality of outlet shoulder the faint-hearted Cui posthumous title of Chou the Liao Dynasty warn the meaningful of guanidine Huan flatter the demon of drought be Na avoid the palm offer to sneer ā F saddle cloth border steal the disconnected snail of imperial mandate edge how extensive illiteracy offer fir and avoid the palm huge legendary turtle R words door road that stand tall and upright and avoid that palm saddle cloth is faint-hearted sheds baby teeth how extensive boundless and indistinct δ cottonrose hibiscus avoids accounts for the sincere of the strong demons and monsters curtain Zhe wife of one's mother's brother
In the process of making synthetic gas, particularly importantly, equably granular fuel is introduced burner in the gasifier, so that the fluctuation of the fuel mass flow rate of supplied burner is reduced to minimum level. If the mass flowrate of granular fuel fluctuation, then can be in gasifier overheated zone and produce the underheat district and then. Fuel can not be gasified totally in the underheat district as a result, changes into the littler product of value fully in the overheated zone, i.e. carbon dioxide and water vapour. In addition, the localized hyperthermia in the gasifier can also damage general lining at the refractory liner of gasifier wall inner surface and the burner of gasifier. Best situation is that each burner is equipped with a fuel-feed device equipment, but investment is very big. So, must reduce by the method that the feeder with at least two outlets is provided the number of feeder, so that the method for the said equipment and operation the said equipment can make the flow rate that is discharged to equably the solids of gasifier by feeder keep stable.
An advantage of the present invention is, can make the mixture of particulate solids and gas be discharged to equably gasifier, thereby can prevent from producing in reactor underheat district and overheated zone.
Another advantage of the present invention is, owing to can prevent underheat district and overheated zone, thereby can protect lining anti-alive in the gasifier and burner and the miscellaneous equipment in the gasifier.
Another advantage of the present invention is more effectively to utilize fuel in production of syngas.
Although what hereinafter will introduce mainly is that the present invention is used for the coal dust aspect, be difficult for by gravity but but method and apparatus of the present invention also is applicable to other fluidisation and flow and namely can form the particulate solids of the obstacle of flow, for example resemble and above outlet, form arch formation flour and the cement. Equally, also be applicable to can partially combusted powdered solid fuel, for example brown coal, anthracite, pitch, carbon black and petroleum coke etc. in the present invention. The granularity of solid carbonaceous fuel is to account for the granularity of fuel particle of weight of fuel 90% less than No. 6 sieve meshes (A.S.T.M). The granularity of solid carbonaceous fuel preferably accounts for the granularity of fuel particle of weight of fuel 90% less than 100 sieve meshes (A.S.T.M).
Referring to accompanying drawing 1, feeder equipment 10 is to be used to make the mixture of particulate solids and gas to be discharged to the receiving vessel of pressurization or the equipment of reactor (not drawing) equably, and this feeder equipment generally comprises: the forced feed device 12 of the passage 14 that is used to discharge solids and gaseous mixture 11 is equipped with in the bottom; At least two geometrical shapies are similar, have the downward cone-shaped wall 18 of awl point and container 16A, the 16B, container 16A, the 16B longitudinal axis 20 separately that are installed in basically in the forced feed device 12 are arranged essentially parallel to the forced feed device longitudinal axis 21; The top of container 16A, 16B respectively is useful on inlet hole 23A, 23B and its bottom of accepting mixture 11 and respectively is useful on outlet opening 24A, the 24B that discharges this mixture; The position of container 16A, 16B is adjacent one another are and crossing, forms between the total plane 26 of the void between the two in intersection, and the bottom 27 of intersection is perpendicular to container 16A, on the specific range 28 of the total horizontal plane 29 of the void of the passage 14 of 16B.
In order to withstand about 0～200 crust (definitely) pressure, it is comparatively favourable to build the pressurizing vessel 12 with cylindrical portions may.The size of pressurizing vessel 12 foot passages 14 should be enough to discharge at least the mixture of solids and gas.
Identical and the part (preferably most of) of at least two (also can be more) geometrical shapies is installed in container 16A, 16B in the pressurizing vessel 12, and it has the downward cone-shaped wall 18 of awl point, and for example angle is less than 90 °, particularly 20～40 ° cone-shaped wall.The geometrical shape of container 16A, 16B is identical, helps making the interference between container 16A, the 16B to be reduced to minimum degree, thereby makes through the solids flow rate of this discharge stable.
Container 16A, 16B are installed in the pressurizing vessel basically, can simplify the structure of container 16A, B greatly, otherwise container 16A, 16B must withstand the High Pressure Difference of wall of container 18 both sides.The inboard available polyethylene of wall 18 or technical well-known any other material lining that reduces wall friction.By reducing wall friction, can add the angle of large container 16A, 16B.
Container 16A, the 16B longitudinal axis 20 separately is all parallel with the longitudinal axis 21 of pressurizer 12 basically, owing to parallelly help to rely on gravity that solids are evenly flowed, thereby makes the flow rate through the solids of this discharge keep stable.If container is uneven basically, that just may produce eccentric channel, thereby the homogeneity of discharging flow rate is produced detrimentally affect.
Container 16A, 16B top separately is useful on ingate 23A, the 16B that accepts mixture 11, and there is outlet opening 24A, the 16B that discharges mixture 11 bottom.
The position of container 16A, 16B is adjacent one another are and crossing, forms between the total plane 26 of the void between the two in intersection.The bottom of described intersection is to have on the specific range 28 of horizontal plane 29 in the void perpendicular to container 16A, 16B outlet opening 24A, 24B.Specifically, specific range 28 is to keep passing all even equidistributed key of forced feed device 12 complete cross section solids mass flow rates.The selection of distance 28 will make the even fluid distribution of gasifier burner, and avoid the interference between container 16A, the 16B.If greater than specific range 28, then need the bigger feeder equipment of diameter, to keep selected container 16A, the angle of 16B perpendicular to horizontal plane 29 distances.If less than specific range 28, then can produce between container 16A, the 16B and disturb, thereby solids and gaseous mixture are discharged equably thus perpendicular to the distance of horizontal plane 29.
Referring to Fig. 2, dividing plate 25 is preferably made rigid plate-like, along the total plane 26(Fig. 1 of the void between container 16A, the 16B) place.The bottom of dividing plate 25 is near the bottom of intersection 27.Dividing plate 25 can guarantee that the solids bed each several part All Ranges equivalent from pressurizing vessel 12 draws solids and discharge or stop solid stream, with all even being controlled of solids mass flow rate of guaranteeing to discharge from container 16A, 16B.The height 30 of dividing plate 25 should equal apart from the distance 36 at feeder 12 tops.Maximum favourable height on the horizontal plane 29 of baffle plate 25 should be to subtract 1.0 times maximum bridge formation size apart from the distance 36 of feeder 12.Minimum constructive height is the bridge formation size.The minimum favourable height of dividing plate 25 on horizontal plane 29 should be to add 0.5 times maximum bridge formation size apart from reason 36.
Dividing plate 25 is active, and the different and height 30 different dividing plates of available geometrical shape replace, to adapt to different operational conditions, for example processing have special solids character various types of moulded coal the time operational condition.
In the present invention, the diameter of container 16A, 16B outlet opening 24A, 24B separately is less than the maximum bridge formation size of solids.In general, maximum bridge formation size is defined as, the maximum length of the particle bed that can set up when forming the stable obstruction of mobile.The bridge formation size is the function of the flowing property of solids, the geometrical shape of feeder and the material of construction feeder etc.So, if the diameter of outlet opening 24A, 24B less than the maximum size of building bridge, then can take place to stop up mobile is stable.
For example, in the present invention, if the maximum bridge formation size of solids is about 45～61cm, under the situation of not having flow promotion or initiation measure, the diameter of outlet opening should be greater than 61cm so.
But by first gas 31 is injected container 16A, the bottom of 16B makes solids inflation wherein, and the diameter of container 16A, 16B outlet opening 24A, 24B separately is reduced to approximately less than 1.3cm.
Referring to Fig. 3, the distance 32 between center 33A, the 33B of container 16A, 16B outlet opening 24A, 24B equals the radius 35 of forced feed device 12 substantially at passage 14 places of forced feed device 12.Distance 32 is the angle of predetermined container 16A, 16B and the result of distance 28 with the basis of radius 35 relations.
Between container 16A, 16B top 37 and pressurizing vessel 12 top 38 apart from 36(Fig. 1), be substantially equal to pressurizing vessel 12 diameter 40(Fig. 3 at least) 1.5 times.The basis of distance 36 and diameter 40 relation is angle, distance 28 and and height 30(Fig. 2 of dividing plate of special container 16A, 16B) the result.If distance 36 is significantly less than 1.5 times of diameter 40, the result, the volume of solids and gaseous mixture approximately is reduced to below 50% of volume of feeder in the feeder, solids circulate mutually between container 16A, the 16B thereby make.In addition, new solids are introduced feeder and can cause the flow rate instability of coming out from outlet opening 24A, 24B.
Between the bottom 27 of container 16A, 16B intersection and forced feed device 12 tops 38 apart from 42(Fig. 1), preferably equal forced feed device 12 diameter 40(Fig. 3 at least) 1.5 times.The basis of distance 42 and diameter 40 relation is the result of the selected angle of the selected diameter 40 of feeder equipment and container 16A, 16B.
The method of operation aforesaid device for example generally comprises and at forced feed device 12 top ends or near this place mixture 11 is introduced this feeder 12.
With second gas (for example nitrogen) 45, inject forced feed device 12 with the selected speed that is no more than solids terminal falling velocity in container 16A, the 16B.Terminal falling velocity is defined as, and the free-falling particle that only relies on action of gravity to quicken in stationary gas is from the static speed that reaches final stable state.
The flow rate of second gas 45 is controlled under the speed that is no more than the solids terminal falling velocity, because otherwise can make excessive the separating out like this of very thin particle influence the flowing property of solids because of removing the fine fraction that is contained in the solids in a large number; Keep stable with the flow rate of the solids that can not make discharge.
In the forced feed device 12 of special diameter, the superfacial velocity up or down of gas between specific crack (for example nitrogen) 31 is that the rate of injection by pilot-gas 31 and 45 reaches.Superfacial velocity is defined as when disregarding existing particulate solids the V-bar that cross section in accordance with regulations calculates.Keep the upwards superfacial velocity of first gas 31, can reduce bed density, thereby make by the flow rate of relief outlet stable.Keep downward superfacial velocity, can the conveying solid substance particle mixture higher with the ratio of gas.
A kind of method that obtains the specific superfacial velocity up or down of first gas 31 is, the specific gas flow rate in the control pressurizing vessel 12 in the mixtures 11, for example from pressurizing vessel 12(preferably from the top 49 of pressurizing vessel 12) emit the gas the mixture 11.Another kind method is the speed of control from the injecting gas of source of the gas 31, can obtain the specific upwards superfacial velocity of first gas 31.Equally, control can obtain the specific downward superfacial velocity of second gas 45 from the speed of the injecting gas of source of the gas 45.
The method that is reduced to minimum level according to the phase mutual interference of above-mentioned made container 16A, 16B is built container 12, can benefit from first gas 31 that injects.
General 1/4th place's injecting gas 31 in container 16A, 16B bottom can produce some effect of being discharged particulate solids about stable and uniform ground by described container.
Injecting gas 31 can produce many favourable results, and wherein three are: destroy and build bridge; Improve rate of outflow, make it surpass the situation of not inflating; With can be from then on before the minimum relief outlet size determined when not inflating also want little relief outlet smooth outflow.For example, because the structure of container 12 can make the interference between container 16A, the 16B be reduced to minimum level, thereby can control flow rate separately.
Reach required optimal gas 31 flows of maximum solids outflow rate and minimum flow rate fluctuation, may be relevant with the sliding velocity between gas 31 and the fluidized particle stream.Sliding velocity is defined as at this, injecting gas 31 and the velocity contrast between the effusive mobile gaseous state-solid stream of via hole 24A, 24B.Can measure the speed of gas and gas-solid stream at the reference section consistent with available gas 31 decanting points (one or more).
Gas 31 produce needed effect to dirty part and gas-solid stream coflow, can control rate of discharge; Can improve the situation of not inflating that surpasses to flow rate; With the fluctuation of eliminating the solids flow rate.
If the rate of injection height of gas 31 can produce gas so and upwards flow, flow downward reverse with gas-solid stream.This gas flow that makes progress can produce higher sliding velocity, reduces the density of mobile gas-solid stream, helps to improve the output of gas 49 and reduces rate of discharge effectively.In fact, can hinder the solids that flow downward by the countercurrent flow of gas 31.If the gas flow that makes progress is very high, then may produce bubble.There is air pocket in the flow, can makes the solids rate of discharge inhomogeneous.
If the injection speed of gas 31 is very low, then only can make air-flow 31 downward, with gas-solids and stream, make the speed step-down of gas-solid stream, the result reduces the rate of discharge of solids.The net result that continues the input rate of reduction gas 31 is to form immobilising condition at the outlet orifice place.
In operating process,, then must introduce gas caps to make-up gas 45 if having only a small amount of or do not have the gas of adverse current.According to the rate of discharge of solids and gas, if the rate of discharge of supplementary rate and solids adapts to fully, then in fact the flow rate of discharging current 45 may be zero.
In feeder 10, should keep the amount of solids in container 16A, the 16B and gaseous mixture to be in container 16A, 16B diameter 14A, 14B 1.5 times and locate, make the charge level effect be reduced to minimum level and can discharge fluid helping from feeder.If this amount is starkly lower than specified amount, then may make the solids mass flow rate that enters burner produce fluctuation, above-mentioned underheat and problems of excessive heat appear.Be used for monitoring the level indicator 47 of container 16A, B mixture amount, can be
-ray absorption type, or the technical well-known telltale that can not hinder any other pattern of mobile.
Present method comprises that also control is discharged to the flow rate of the mixture 11 of acceptable response device (not drawing) through container 16A, 16B outlet opening 24A, 24B separately with the method for control through first gas (for example nitrogen, synthetic gas or other carrier gas), 31 flow rates of container 16A, 16B base wall 18.With the method for above-mentioned control first gas 31 flow rates, mixture 11 is flowed out from outlet opening 24A, the 24B of container 16A, 16B simultaneously, an outflow from container 16A, 16B, with (or) flow out from container 16A, 16B with different speed.
The pressure of keeping pressurizing vessel 12 is higher than the pressure of acceptable response device (not drawing), so that solids input acceptable response device.
Referring to Fig. 4, this figure represents that mass flow rate fluctuation that a kind of frequency that is used to make at least one burner 12 of being transported to gasifier 13 to go is about 0.1～100 hertz flammable solid particle and gaseous mixture is reduced to the equipment of minimum level.This equipment comprises the multiple exit feeder 15 that is used to accept mixture 11.This feeder has the downward cone-shaped wall 32 of awl point and is positioned at the outlet orifice 34 that is used to discharge mixture 11 of wall 32 bottoms.Feeder 15 bottoms can be conical its angle can be less than 90 °.
Be used to control the favorable method of the discharge flow rate of the mixture 11 that comes out from feeder 15, comprise for example nitrogen, carbonic acid gas or synthetic gas by injecting gas 36() make the inflation of feeder 15 bottoms to form the injection section (see figure 4).
In addition, inflation can also separate into several parts and carries out.The inflation of feeder 15 bottoms can be dwindled the diameter of outlet orifice 34 and use the less transfer lime 46 of diameter.
The structure of above-mentioned feeder 15 shown in Figure 4, and make top mixture 11 these two factors of inflation of feeder 15 bottoms make and can under the situation that is much higher than the suspensoid density (for example being higher than 200kg/cm) that can reach, coal grain and gaseous mixture 11 be transported to feeder everywhere with fluidization system fluid coal grain and gaseous mixture.For the coal grain and the gaseous mixture that are used for gasification, this has Special Significance, because the gas inert often of inflation usefulness plays thinner, thereby reduces the calorific value of every standard cubic foot in product gas.
In addition, being used to control the device that mixture 11 discharges flow rates also can be the device (for example Thumper, horn or technical well-known any other pattern device) that can make the mixture mechanical oscillation.
The device (for example various valve) that general purpose control is discharged flow rate is worthless, because of these devices hinder the transportation of coal grain, thereby the mass flow rate of the coal grain of the burner that is sent to gasifier is fluctuateed.
Equipment shown in Figure 4 comprises the instrument 40 that is used for keeping feeder 11 solids charge levels, generally keep 50% place of charge level at least about height more than outlet orifice, the available instrument has the level measuring apparatus of radiant light densometer, ultrasonoscope or mechanical detector or technical any its pattern of knowing.
Keep charge level at least at about 50% place, can reduce charge level and drain from feeder 15 effusive influences, this can have influence on the coal grain and flow to burner.
The minimum differntial pressure of keeping between feeder 15 and the gasifier 13 is at least about 2～20 crust, enters feeder 15 to prevent fire or synthetic gas, to keep the burner 12 that the coal grain flows to gasifier 13.The device of keeping pressure reduction that the present invention adopts is not the device of using always (for example adorning a valve between feeder 15 and gasifier 13).The present invention has adopted the instrument (for example pressure sensing parallel operation 78 that communicates with differential pressure controller 79) that is used to measure feeder 15 pressure; Be used to measure the instrument (for example pressure transmitter 80 that communicates with controller 79) of gasifier 13 pressure; Instrument by 79 comparative measurement pressure; Be used to regulate the device of the pressure in the feeder 15, for example improve or reduces the interior pressure of container 15 by variable valve 81,82 and 83.
Keep the pressure reduction between feeder 15 and the gasifier 13, part is by realizing in the pressurization gas cap district on gas injecting feeding device 15 tops.Pressure in the feeder 15 is to control with independent controller 79, this independent controller 79 is to import the gas of superchargings by valve 81 at least about the speed of 0.1 crust/min, or discharge gases by valve 82 with this speed, obtain suitable control to guarantee the pressure in the feeder 15.
Near the partial inflation (for example the inflation cover 91) of feeder 15 outlet orifices 34 upper sections, can prevent owing to the pressure reduction of keeping between feeder 15 and the gasifier 13 causes the coal grain in the mixture 11 to build bridge or obstruction at feeder.Solids are blocked in feeder 15 bottoms, can make unstable or do not have coal and flow out from the flow rate of feeder 15 effusive coals.
Favourable way is, guarantee separately to supply with injecting gas and keep feeder 15 and gasifier 13 between pressure reduction (as shown in Figure 4) so that the variation of the pressure in a S.P. or flow can not involve other.
With the pneumatic transport method gas mixture 11 is delivered to the utensil of gasifier from feeder 15, comprise that the transfer lime 46(with import and exit portion 47,48 sees Fig. 4).Inlet part 47 circulates with feeder 15 bottoms, and exit portion 48 is that fluid is logical with the burner 12 of gasifier 13.Realize for example nitrogen, carbonic acid gas or synthetic gas gas 49() under the pressure and transfer lime 46 more at least on the device of injection mixture 11 are technical well-known devices.Be implemented in the pulsation of gas 49 under particular amplitude and the frequency, available loudspeaker (seeing 102 among Fig. 4), or technical any other method of knowing with variable frequency.Can also inject first gas 49 of pulsing along transfer lime 46 other points (not drawing), with the tamper or the sludge of coal grain and gaseous mixture in the dispersion transfer lime 46 with particular amplitude and frequency.The suitable injection phase of first gas 49 is to select according to the amplitude that tamper increases.
Preferably do not inject first gas,, make the mixture that to discharge coal grains and gas equably from feeder 15 because injecting gas can improve the back pressure at feeder 15 discharge places in unusual place near the relief outlet 34 of feeder 15.
Transfer lime 46 should be slick as far as possible, promptly without hindrance any protuberance of mixture 11 mobile and minimum recessed and curved part.Any curved part of transfer lime 46 should have 1.20m or 10 times of radius-of-curvature to transfer lime 46 diameters (selecting bigger in the two size), so that the coal dust in the transfer lime 46 remains on suspended state.
The diameter of transfer lime is preferably 4-150mm, particularly 6～100mm.Helping reaching in transfer lime in above-mentioned diameter range at a high speed, for example, is the mixture of 100～500kg/m for suspension density, and speed can reach 15m/sec.Can impel mixed uniformly coal dust and gaseous mixture to enter in the burner of gasifier at a high speed.When adopting diameter greater than the transfer lime of 150mm, the coal grain of conveying and the degree of mixing of gas do not reach the needed homodisperse degree of roasting kiln of gasifier, and diameter can cause then that less than the transfer lime of 4mm the coal grain builds bridge in transfer lime 46.
The suspension density of coal grain and gaseous mixture, because of the type of used coal different.For example the suspension density of No. 5 coal grains in Illinois generally is at 225 25kg/m
3Scope in, suspension density is 350kg/m preferably
3Under extreme conditions suspension density can be at 50～800kg/m
3Scope in the change.
Fig. 4 shows, being used for controlling selectively the utensil of density that is transported to the mixture 11 of gasifier 13 by feeder 15 comprises: be used for directly or indirectly being determined at feeder 15 discharge places or near the instrument of the suspension density of the mixture at this place, for example pressure transmitter 66, electric capacity photodensitometer 90, ultrasonoscope,
-ray photodensitometer, opacity electromagnetic radiator; Be used for the instrument that the suspension density that will be measured and preselected density compare, for example controller 70; Instrument with the suspension density that is used to regulate mixture 11, amplitude and frequency.
Come the signal of self-controller 70 to be sent to the device (for example valve 83) of the flow rate that is used to regulate and be used to regulate the amplitude of gas 36 pulses of the bottom of injecting the device that receives described mixture 15 and the instrument of frequency, for example loudspeaker 100.
Equally, come the signal of self-controller 70 to be sent to be used to regulate device (for example valve 74) and the amplitude of this gas 49 of adjusting and the instrument of frequency of the flow rate of the gas 49 that injects transfer lime 46, for example loudspeaker 102.In addition, the instrument that comes the signal of self-controller 70 to be sent to be used to regulate the amplitude of the gas 65 that injects right cylinder 50 and frequency loudspeaker 101 for example.Favourable way is to be used for the amplitude of adjustments of gas 36,65 and 49 and the instrument of frequency is separately controllable.
Gasifier should be in the reducing atmosphere.The instrument that is used for controlling selectively oxygen and the mixture weight ratio that enters gasifier 13 is indispensable.Should keep such ratio, it should make oxygen is 0.6～1.2 to the ratio of moisture and ashless coal, more preferably 0.8～0.9.The control of this ratio can realize by the whole bag of tricks, for example the signal that comes self-controller 70 is sent to the mechanism (for example valve 76) of the speed that is used for controlling selectively the oxygen-containing gas 71 that enters gasifier 13.If the mass flow rate of coal grain that flows to burner 12 that optical density meter 90 records and gaseous mixture 11 is lower than the mass flow rate of being scheduled to mass flow rate controller 70, the mass flow rate of oxygen-containing gas 71 is descended and (or) rate of injection of first and second gas 49,65 is descended.
Shown in Figure 6 is a kind of alternative scheme of Fig. 4 embodiment.Reference among Fig. 6 digital with Fig. 4 in used identical, just do not have 66,100,101 and 102.
Above description is intended to the explanation to laying down a definition property of the present invention.Under the prerequisite of spirit of the present invention, can do various changes to the details of described equipment and method within the scope of the appended claims.
Claims (25)
1, a kind ofly be used to make the solids that are discharged to the acceptable response device equably and gas flow rate of mixture to keep stable feeder equipment, this equipment is characterised in that:
The bottom has the pressurizing vessel of the relief outlet that is used to discharge described solids and gaseous mixture;
At least two geometrical shape containers identical, that have the downward cone-shaped wall of awl point;
Described container respectively has an inlet hole of accepting described mixture on its top, an outlet opening of discharging described mixture is respectively arranged in its bottom;
The position of described container is adjacent one another are and crossing, forms between the total plane of the void between the two in joining, and the bottom of this intersection has on the specific range of horizontal plane in the void perpendicular to this two containers relief outlet.
2, a kind of equipment, the container that it is characterized in that these two geometrical shapies are identical, has a downward cone-shaped wall of awl point is installed in the described pressurizing vessel basically, and described container has parallel with the longitudinal axis of the described pressurizing vessel basically longitudinal axis separately.
3, equipment according to claim 2 is characterized in that described container is conical, and its angle is less than 90 °.
4, equipment according to claim 2 is characterized in that placing the rigid plate-like dividing plate along the total plane of the void between between described container, and the bottom of described dividing plate is near the bottom of described intersection.
5, equipment according to claim 4 is characterized in that described dividing plate can take away.
6, equipment according to claim 2, the diameter of described outlet opening that it is characterized in that each container is greater than the maximum bridge formation diameter of described solids.
7, equipment according to claim 2 is characterized in that the diameter of the described outlet opening of each container, is about solids and the gaseous mixture of 200～500kg/m for density, is about 45～61cm.
8, equipment according to claim 2 is characterized in that at least in the inflation of the bottom of described container.
9, equipment according to claim 8 is characterized in that the diameter of the described outlet opening of each container, is about solids and the gaseous mixture of 200～500kg/m for density, approximately less than 2.5cm.
10, equipment according to claim 2 is characterized in that stating in the passage place of described pressurizing vessel the distance between the described outlet opening center of container, is substantially equal to the radius of described pressurizing vessel.
11, equipment according to claim 2 is characterized in that the distance between described vessel top and the described pressurizing vessel top, equals 1.5 times of diameter of described pressurizing vessel at least substantially.
12, equipment according to claim 2 is characterized in that the bottom of described intersection part and the distance between the described pressurizing vessel top, equals 1.5 times of diameter of described pressurizing vessel at least substantially.
13, equipment according to claim 4, the minimum constructive height that it is characterized in that described dividing plate are that 1.5 times described pressurizing vessel diameter adds 0.5 times the maximum bridge formation size of described solids in described container.
14, equipment according to claim 4 is characterized in that the maximum height of described dividing plate is gone the maximum bridge formation size of 1.0 times of described solids in described container for 1.5 demultiplications of the diameter of the described pressurizing vessel at the described container of installation place in described pressurizing vessel.
15, a kind ofly be used to make the solids that are aligned to pressurization acceptable response device equably and the flow rate of gaseous mixture to keep stable method.The method is characterized in that and have the following step:
Mixture is introduced pressurizing vessel, and this pressurizing vessel has at least two geometrical shapies identical and be installed in container in this pressurizing vessel basically, and each container all is useful on the outlet opening of the described mixture of discharge;
The control mixture is by the flow rate of described container outlet opening separately, and its method is the flow rate of control via first gas of the wall injection of container bottom;
Through described outlet of container hole, mixture is discharged to described acceptable response device;
Keep the pressure of described pressurizing vessel, make the pressure that is higher than described acceptable response device.
16, method according to claim 15 is characterized in that controlling the flow rate of injecting first gas of described pressurizing vessel with selected speed, makes it be no more than solids terminal falling velocity in described container.
17, method according to claim 15 is characterized in that keeping certain volume, comprises the charge level indicator that is provided for monitoring the volume of described mixture in described container.
18, method according to claim 15 is characterized in that keeping the selected upwards step of superfacial velocity and comprises and maintain and be at least about 2mm/sec be about speed in the described pressurizing vessel of 1m at diameter.
19, method according to claim 15 is characterized in that the step of controlling gas mixture flow rate in the pressurizing vessel comprises from described pressurizing vessel release gas.
20, method according to claim 15 is characterized in that described mixture is from described two containers discharge.
21, method according to claim 15 is characterized in that described mixture is from described all containers discharges.
22, method according to claim 12 is characterized in that described mixture is to discharge from described container with different speed.
23, method according to claim 15 is characterized in that the volume of keeping interior solids of described container and gaseous mixture makes it be at least about 50% of described container volume.
24, method according to claim 15 is characterized in that keeping the selected downward superfacial velocity of second gas in having the pressurizing vessel of selected diameter.
25, method according to claim 15 is characterized in that second gas being injected the top of described pressurizing vessel to be no more than the speed of the terminal falling velocity of described solids in described container.
Applications Claiming Priority (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US098,590 | 1987-09-18 | ||
| US07/098,590 US4844663A (en) | 1987-09-18 | 1987-09-18 | Feed line-ultrasonic activated gas injection |
| US098,588 | 1987-09-18 | ||
| US07/098,152 US4869622A (en) | 1987-09-18 | 1987-09-18 | Feed hopper design |
| US098,589 | 1987-09-18 | ||
| US098,152 | 1987-09-18 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1032746A true CN1032746A (en) | 1989-05-10 |
| CN1017873B CN1017873B (en) | 1992-08-19 |
Family
ID=26794255
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 88106710 Expired CN1017873B (en) | 1987-09-18 | 1988-09-16 | Feeding device of coal gasifier |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1017873B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1090040C (en) * | 1996-11-19 | 2002-09-04 | 法国石油公司 | Apparatus for pressure equalisation and flushing in vessel |
| CN101909738A (en) * | 2008-01-16 | 2010-12-08 | 国际壳牌研究有限公司 | Method to the pressurised reactor particular solid material |
| CN101328434B (en) * | 2008-07-17 | 2011-06-22 | 中国科学技术大学 | Dry coal powder airflow bed gasification furnace |
| CN102105567A (en) * | 2008-08-01 | 2011-06-22 | 科林工业有限公司 | Method and apparatus for starting up gasifying reactors operated with combustible dust |
| CN101152932B (en) * | 2006-09-27 | 2011-12-14 | 华东理工大学 | Feed device of carbonaceous solid powder with a plurality of discharge doors and feed method thereof |
| CN102844496A (en) * | 2010-04-16 | 2012-12-26 | 约瑟夫福格勒公司 | Charger |
| US9266688B2 (en) | 2010-09-30 | 2016-02-23 | General Electric Company | Feed vessels and systems for pneumatically conveying solid particles |
| CN106241382A (en) * | 2016-09-08 | 2016-12-21 | 东南大学 | A kind of pressure sending type height densification phase multichannel air conveying issuance of materials tank and induction system thereof |
| CN109847653A (en) * | 2019-01-21 | 2019-06-07 | 西安交通大学 | A kind of fuel combination pressurization continuous feeding system and method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103383001B (en) | 2012-05-03 | 2016-04-27 | 通用电气公司 | Apparatus for feeding |
-
1988
- 1988-09-16 CN CN 88106710 patent/CN1017873B/en not_active Expired
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1090040C (en) * | 1996-11-19 | 2002-09-04 | 法国石油公司 | Apparatus for pressure equalisation and flushing in vessel |
| CN101152932B (en) * | 2006-09-27 | 2011-12-14 | 华东理工大学 | Feed device of carbonaceous solid powder with a plurality of discharge doors and feed method thereof |
| CN101909738A (en) * | 2008-01-16 | 2010-12-08 | 国际壳牌研究有限公司 | Method to the pressurised reactor particular solid material |
| CN101328434B (en) * | 2008-07-17 | 2011-06-22 | 中国科学技术大学 | Dry coal powder airflow bed gasification furnace |
| CN102105567B (en) * | 2008-08-01 | 2015-03-18 | 西门子公司 | Method and apparatus for starting up gasifying reactors operated with combustible dust |
| CN102105567A (en) * | 2008-08-01 | 2011-06-22 | 科林工业有限公司 | Method and apparatus for starting up gasifying reactors operated with combustible dust |
| US9670428B2 (en) | 2008-08-01 | 2017-06-06 | Siemens Aktiengesellschaft | Method and device for starting up gasifying reactors operated with combustible dust |
| CN102844496A (en) * | 2010-04-16 | 2012-12-26 | 约瑟夫福格勒公司 | Charger |
| CN102844496B (en) * | 2010-04-16 | 2015-07-15 | 约瑟夫福格勒公司 | Charger |
| US9266688B2 (en) | 2010-09-30 | 2016-02-23 | General Electric Company | Feed vessels and systems for pneumatically conveying solid particles |
| CN106241382A (en) * | 2016-09-08 | 2016-12-21 | 东南大学 | A kind of pressure sending type height densification phase multichannel air conveying issuance of materials tank and induction system thereof |
| CN109847653A (en) * | 2019-01-21 | 2019-06-07 | 西安交通大学 | A kind of fuel combination pressurization continuous feeding system and method |
| CN109847653B (en) * | 2019-01-21 | 2020-10-27 | 西安交通大学 | Mixed fuel pressurization continuous feeding system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1017873B (en) | 1992-08-19 |
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