CN104178227B - A kind of fluidized bed dry distillation method and device of coal dust - Google Patents
A kind of fluidized bed dry distillation method and device of coal dust Download PDFInfo
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- CN104178227B CN104178227B CN201310210239.7A CN201310210239A CN104178227B CN 104178227 B CN104178227 B CN 104178227B CN 201310210239 A CN201310210239 A CN 201310210239A CN 104178227 B CN104178227 B CN 104178227B
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Abstract
The invention discloses the fluidized bed dry distillation method and device of a kind of coal dust.Method for destructive distillation comprises the steps: that A. coal dust raw material absorbs the heat that combustion reaction generates in gasification combustor (11) in coal dust raw material preheating pipe (12) and preheats；B. the coal dust raw material after preheating carries out dry distillation reactor in bed formula fluidized bed dry distillation reactor (9), generates oil gas and coal dust semicoke, and coal dust semicoke is stripped out entrained oil gas in stripper (18)；C. the coal dust semicoke after stripping enters gasification combustor, carries out combustion reaction with oxygen；D. the coal dust semicoke through the burning of step C portion carries out water gas reaction with water vapour in riser gasification reactor (2)；E. step D generates coal gas and high temperature coal ash enter coal ash coal gas separator (1) and carry out gas solid separation.The invention discloses the powder fluidized bed destructive distillation device for realizing said method.The present invention can be used for the dry distilling processing of multiple coal dust.
Description
Technical field
The invention belongs to coal dust retorting technique field, relate to the fluidized bed dry distillation method and device of a kind of coal dust.
Background technology
The crude oil demand that China quickly increases has pulled the quick growth of crude oil import amount, and external dependence degree is continuous
Improving, the energy security guarantee to China brings the biggest hidden danger.The shortage of petroleum resources and demand promote,
The cost making a lot of petrochemical materials also remains high.Coal Chemical Industry and petrochemical industry have being substituted for each other property,
Development of Novel Coal Chemical Industry well can be supplemented as petrochemical industry, necessary.Coal Chemical Industry refers to
Raw material, makes coal be converted into the process of gas, liquid and solid fuel and chemicals through chemical process；Mainly
Including coal gasification, liquefaction, dry distilling, and tar production and carbide acetylene chemical industry etc..
Dry distillation of coal technology is one of significant process of Coal Chemical Industry.Coal low temperature distillation can extract low temperature tar, and
Produce semicoke and coalitenessity producer gas.Tar yield is higher, and composition, based on alkane, can be processed further out
Senior liquid fuel (the such as vehicle fuel such as gasoline, diesel oil) and industrial chemicals；Semicoke can be used as solid fuel
Or gasified raw material, coal gas is then good fuel and chemosynthesis raw material.Dry distillation of coal technology can be divided into moving bed
Dry distilling, fluidized bed dry distillation etc..Wherein the fluidized bed dry distillation of coal dust be block coal is pulverized for fine powder (particle diameter≤
3mm), the direct contact heat transfer under fluidized state with high-temp solid heat carrier (coal ash) or high-temperature gas heat carrier
The process of concurrent heat decomposition reaction；Have calorific intensity height, dry distillation rate is fast, the oil gas time of staying is short, gas
Admittedly can the feature such as sharp separation, be a kind of preferably coal processing and utilization mode.
Chinese patent CN101328415A discloses a kind of piston type fluidized bed low temperature dry distillation technological process, permissible
Dry distilling for coal dust.This process utilizes lifting tube flowing catalytic cracking device principle, anti-with riser
Answering device is carbonization reactor, with catalyst regenerator for high-temperature water gas generator, is dry with high-temperature water gas
Evaporate fluidizing agent and the heat carrier of raw material.Dry distilling feedstock transportation is done in riser fluidized-bed reactor
Evaporating reaction, after reaction, oil gas carries out isolated retorted product.Pyrolysis Char enters water gas generator, dry
Evaporate the carbon in semicoke, the oxygen in air and water vapour to carry out aoxidizing and water gas reaction, obtain water gas.Should
Process is primarily present following deficiency: (1) uses high-temperature water gas (about 620～900 DEG C) as retort process
Fluidizing agent and heat carrier, need to be transported to from water gas generator by high-temperature water gas with gas compressor
Riser carbonization reactor.Conveying high-temperature water gas can propose higher material requirement to gas compressor；Separately
Outer gas compressor is in high harsh operating condition all the time, will have influence on the long-term operation of destructive distillation device.(2)
Compressed air and water vapour simultaneously enter the bottom of high-temperature water gas generator, at the same area and Pyrolysis Char
Carry out combustion reaction and water gas reaction simultaneously, cause and influence each other between two kinds of reactions；Burning and water gas
Reaction can not fully be carried out, and can cause the productivity reduction generating water gas from Pyrolysis Char.
Summary of the invention
It is an object of the invention to provide the fluidized bed dry distillation method and device of a kind of coal dust, to solve existing coal
Existing for powder fluidized bed dry distillation technology needing use gas compressor conveying retort process needed for high temperature fluidized
Medium and gas heat carrier, combustion reaction and water gas reaction are carried out and interactional at the same area simultaneously
Problem.
For solving the problems referred to above, the technical solution used in the present invention is: a kind of fluidized bed dry distillation method of coal dust,
It is characterized in that: the method in turn includes the following steps:
A. pulverize after coal dust raw material through coal dust material feeding tube enter coal dust raw material preheating pipe bottom, by
Under the effect of the lift gas that lift gas jet pipe is passed through up along coal dust raw material preheating pipe, absorb stripping after
Coal dust semicoke carries out the heat of combustion reaction generation in gasification combustor and preheats, and the coal dust after preheating is former
Expect to enter bed formula fluidized bed dry distillation reactor through coal dust raw material riser；
B. coal dust raw material dry distilling close phase section bed in bed formula fluidized bed dry distillation reactor carries out dry distilling anti-
Should, generate oil gas and coal dust semicoke, the oil gas first group of rotation in being located at bed formula fluidized bed dry distillation reactor
It is defocused by the oil gas vent pipe flow of bed formula fluidized bed dry distillation reactor head that coal dust half isolated by wind separator
Going out, the coal dust semicoke in dry distilling close phase section bed flows downward, and enters and is located at the reaction of bed formula fluidized bed dry distillation
Stripper below device, is passed through stripping steam in stripper, is stripped off coal dust semicoke entrained oil gas；
C. the coal dust semicoke after stripping in stripper enters gasification combustor, with warp through coal dust semicoke conveying pipe
The oxygen that burning gases distributor is passed through in gasification combustor carries out combustion reaction, the oxidation generated after burning
Carbon, carbon dioxide carry together with atomized water steam and flow up through partially combusted coal dust semicoke, enter
Riser gasification reactor；
D. in riser gasification reactor, enter in riser gasification reactor through partially combusted coal
Powder semicoke and atomized water steam and the gasified water steam that is passed through in riser gasification reactor are along riser gasified reverse
Answering that device is up carries out water gas reaction, the coal gas of generation and high temperature coal ash enter coal ash coal gas separator；
E., in coal ash coal gas separator, coal gas and high temperature coal ash carry out gas-solid in second group of cyclone separator
Separating, isolated coal gas is flowed out by the gas outlet tube at coal ash coal gas separator top.
For realizing the fluidized bed dry distillation device of the coal dust of above-mentioned method for destructive distillation, be provided with fluidized bed dry distillation reactor,
Pyrolysis Char burning and gasification reactor, fluidized bed dry distillation reactor is provided with coal dust material feeding tube, its feature
It is: carbonization reactor is bed formula fluidized bed dry distillation reactor, is provided with first group of cyclone separator in it,
Top is provided with oil gas collection chamber, oil gas vent pipe, and lower section is coaxial therewith being provided with stripper, sets in stripper
Having stripping baffles, bottom to be provided with stripped vapor distributor, Pyrolysis Char burning includes gasification with gasification reactor
Burner and riser gasification reactor, gasification combustor is positioned at the lower section of riser gasification reactor, gasification
The housing of burner includes the cylindrical drum of bottom and the round table surface shape cylinder on top, the side of cylindrical drum
It is provided with coal dust semicoke conveying pipe between face and the bottom bulkhead of stripper, is coaxial therewith in gasification combustor arranging
Having coal dust raw material preheating pipe, the bottom of coal dust raw material preheating pipe is stretched out by the bottom of gasification combustor, described
Coal dust material feeding tube is located at the bottom of coal dust raw material preheating pipe, and the bottom of coal dust raw material preheating pipe is provided with lifting
Gas spray pipe, the top exit of coal dust raw material preheating pipe is connected with connecting tube, and connecting tube is stretched by gasification combustor
Going out, its top exit is connected with the bottom inlet of coal dust raw material riser, and the top of coal dust raw material riser goes out
Mouth is connected with horizontal pipeline section, and the outlet of horizontal pipeline section is positioned at the dilute phase section of bed formula fluidized bed dry distillation reactor,
The bottom of gasification combustor is provided with burning gases distributor, and burning gases distributor is connected with air inlet pipe, air inlet
Pipe racks has oxygen intake and atomized water steam inlet, and riser gasification reactor is the vertical of circular in cross-section
Pipe, its bottom inlet is connected with the top exit of gasification combustor, and bottom is provided with gasified water steam inlet tube,
Bed formula fluidized bed dry distillation reactor be arranged over coal ash coal gas separator, be provided with second group of whirlwind in it and divide
From device, the top exit of riser gasification reactor is connected by one section of horizontal tube and second group of cyclone separator,
The top of coal ash coal gas separator is provided with coal gas collection chamber, gas outlet tube, and bottom is provided with fluidizing gas distribution
Device.
Use the present invention, there is following beneficial effect: the retort process of (1) present invention uses bed formula fluidisation
Bed carbonization reactor, coal dust raw material absorbs the coal dust semicoke after stripping in gasification combustion in coal dust raw material preheating pipe
The heat carrying out combustion reaction generation in burner preheats, and does not use gas heat carrier.Coal dust raw material is done
Evaporate oil gas and the water vapour of generation, and in stripper, strip the defocused stripping steam of coal dust half and stripping
The oil gas gone out, can make the dry distilling close phase section bed in bed formula fluidized bed dry distillation reactor be in aerated flow
Change state, so need not provide specially fluidizing agent.In a word, the present invention need not use gas compressor
Carry high temperature fluidized medium and heat carrier for retort process, do not exist and gas compressor is proposed higher material
Problem that matter requires and make gas compressor be in high harsh operating condition all the time and to have influence on destructive distillation device long
The problem of period run.The present invention does not the most use high-temp solid heat carrier to heat coal dust raw material, such that it is able to carry
The treating capacity of high destructive distillation device coal dust raw material.(2) present invention, combustion reaction is carried out in gasification combustor, water
Coal gas reaction is carried out in riser gasification reactor, and two kinds of reactions are carried out in the most independent region, between
Do not influence each other.Combustion reaction can be that water gas reaction provides enough heats；At riser gasification reaction
In device, water gas reaction can fully be carried out, and is conducive to improving the productivity generating water gas from coal dust semicoke.
(3) present invention, through dry distilling and water gas reaction, coal dust raw material can be fully used；Coal dust raw material is
The solid product of rear generation is coal ash, such that it is able to reduce the reserve of coal ash coal gas separator so that it is structure chi
Very little less, reduce investment outlay.
The present invention can be used for the dry distilling processing of multiple coal dust, and the course of processing can continuously and stably be carried out, and adjusts
Joint is flexible, treating capacity is big, and oil gas is high with the yield of coal gas.
The present invention is further detailed explanation with detailed description of the invention below in conjunction with the accompanying drawings.Accompanying drawing is with concrete
Embodiment is not limiting as the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of powder fluidized bed destructive distillation device of the present invention.
Detailed description of the invention
Seeing Fig. 1, the powder fluidized bed destructive distillation device (referred to as destructive distillation device) of the present invention is provided with fluidized bed dry distillation
The burning of reactor, Pyrolysis Char and gasification reactor, fluidized bed dry distillation reactor is provided with coal dust material feeding tube
15.Carbonization reactor is bed formula fluidized bed dry distillation reactor 9, the shell of bed formula fluidized bed dry distillation reactor 9
Body includes the cylindrical drum of upper and lower and the inverted round table face shape cylinder between the two cylinder
Body.It is provided with first group of cyclone separator 8, including the rotation of two series connection in bed formula fluidized bed dry distillation reactor 9
Wind separator, its dipleg stretches to the top within dry distilling close phase section bed.Bed formula fluidized bed dry distillation reacts
The top of device 9 is provided with oil gas collection chamber 6, oil gas vent pipe 7, and lower section is coaxial therewith being provided with stripper 18.Vapour
The housing carrying device 18 includes a cylindrical drum；Be provided with in stripper 18 stripping baffles (shown in Fig. 1 for people
Font stripping baffles), bottom is provided with stripped vapor distributor 17.
The Pyrolysis Char burning of the present invention includes gasification combustor 11 and riser gasification reaction with gasification reactor
Device 2, gasification combustor 11 is positioned at the lower section of riser gasification reactor 2.The housing of gasification combustor 11 includes
The end of the cylindrical drum of bottom and the round table surface shape cylinder on top, the side of cylindrical drum and stripper 18
Coal dust semicoke conveying pipe 16 it is provided with between portion's end socket.Coal dust semicoke conveying pipe 16 is provided with flow control valve 23,
To control the flow of the interior coal dust semicoke of pipe.
Be coaxial therewith in gasification combustor 11 being provided with coal dust raw material preheating pipe 12 (coal dust raw material preheating pipe 12
Main part is located in gasification combustor 11), the cylindrical drum of gasification combustor 11 and coal dust raw material preheating pipe
Circular passage 27 (shape of cross section is annular) is formed between 12.The bottom of coal dust raw material preheating pipe 12 is by gas
The bottom changing burner 11 is stretched out；Described coal dust material feeding tube 15 is located at coal dust raw material preheating pipe 12 times
Portion, the bottom of coal dust raw material preheating pipe 12 is provided with lift gas jet pipe 14.The top of coal dust raw material preheating pipe 12
Outlet is connected with connecting tube 20；Connecting tube 20 is stretched out by gasification combustor 11, its top exit and coal dust raw material
The bottom inlet of riser 10 is connected.The top exit of coal dust raw material riser 10 is connected with horizontal pipeline section 101,
The outlet 102 of horizontal pipeline section 101 is positioned at the dilute phase section of bed formula fluidized bed dry distillation reactor 9.Gasification combustor 11
Bottom be provided with burning gases distributor 13 around coal dust raw material preheating pipe 12；Burning gases distributor 13 with enter
Trachea 131 is connected, and air inlet pipe 131 is with oxygen intake and atomized water steam inlet.
Coal dust raw material preheating pipe 12, coal dust raw material riser 10 and riser gasification reactor 2 are cross section
Rounded vertical tube.The top exit phase of the bottom inlet of riser gasification reactor 2 and gasification combustor 11
Even, bottom is provided with gasified water steam inlet tube 201.Gasified water steam inlet tube 201 tilts upward, it is common that
It is uniformly arranged 2～6 around riser gasification reactor 2.Gasified water steam inlet tube 201 gasifies with riser
The center of reactor 2 interface is to riser gasification reactor 2 bottom inlet and gasification combustor 11 top exit
Vertical dimension b of junction, generally 0.5～1m (rice).
Bed formula fluidized bed dry distillation reactor 9 be arranged over coal ash coal gas separator 1, coal ash coal gas separator 1
Housing include the cylindrical drum of upper and lower and the inverted round table face shape between the two cylinder
Cylinder.Second group of cyclone separator 24 it is provided with, including the cyclonic separation of two series connection in coal ash coal gas separator 1
Device, its dipleg stretches to the top within coal ash dense-phase bed；The top exit of riser gasification reactor 2 leads to
Cross one section of horizontal tube 203 to be connected with second group of cyclone separator 24.The top of coal ash coal gas separator 1 is provided with coal
Gas collection chamber 25, gas outlet tube 26, bottom is provided with fluidizing gas distributor 4.
Coal ash coal gas separator 1 is provided with external warmer 22, external warmer 22 and the bottom of coal ash coal gas separator 1
Cement output tank 221 and recurrent canal 222 it is provided with between cylindrical drum.Cement output tank 221 is provided with flow control valve 23,
To control the flow of the interior coal ash of pipe.External warmer 22 is connected with coal ash tank 21 also by pipeline 223, coal ash tank 21
It it is a canister.The thermal medium that takes of external warmer 22 typically uses the water under ambient temperature.
Seeing Fig. 1, the height a of gasification combustor 11 is generally 2～10m, and the diameter of cylindrical drum is generally
1000～5000mm.The height h of riser gasification reactor 2 is generally 10～40m, riser gasification reactor
2 are typically gasification combustor 11 cylindrical drum cross-sectional area with the cross-sectional area of coal dust raw material preheating pipe 12
20%～50%.Above-mentioned cross-sectional area, presses riser gasification reactor 2, coal dust raw material preheating pipe 12 respectively
And the diameter of gasification combustor 11 cylindrical drum calculates.
The various equipment of destructive distillation device of the present invention, pipeline, component, all use metal material manufacture.Bed formula
In the housing of fluidized bed dry distillation reactor 9, stripper 18, gasification combustor 11, coal ash coal gas separator 1 etc.
Wall, riser gasification reactor 2, coal dust raw material riser 10 and other with solid particle (coal dust semicoke,
Coal ash etc.) inwall of pipeline that contacts, heat insulation and wear resistance layer (figure is slightly) can be arranged as required to.Coal dust raw material
Economizer bank 12 is not provided with heat insulation and wear resistance layer, but within it, outer wall is respectively provided with heat conduction wearing layer (material is carbonization
Silicon, corundum etc., figure is slightly).The shape of cross section of various pipelines is circle.The diameter that the present invention mentions, all
For cylinder or the interior diameter of pipeline；The cylinder of heat insulation and wear resistance layer or pipeline are provided with for inwall and inwall is provided with
The coal dust raw material preheating pipe 12 of heat conduction wearing layer, diameter is heat insulation and wear resistance layer or the interior diameter of heat conduction wearing layer.
The diameter of each pipeline mainly calculates according to material in each pipeline and/or the flow of medium, density and determines.
Stripped vapor distributor 17, fluidizing gas distributor 4, burning gases distributor 13 can use conventional
Annular distributor or dendroid distributor.Flow control valve can use various conventional control granular solid
The flow control valve (such as guiding valve) of body grain flux.External warmer 22, cyclone separator etc. can use this
Field or near field are commonly used.
The destructive distillation device shown in Fig. 1 is used to carry out method (the referred to as dry distilling side of powder fluidized bed dry distilling of the present invention
Method), in turn include the following steps:
A. the coal dust raw material 150 after pulverizing enters coal dust raw material preheating pipe 12 times through coal dust material feeding tube 15
Portion, under the effect of the lift gas 140 being passed through by lift gas jet pipe 14 along coal dust raw material preheating pipe 12
OK, the coal dust semicoke after absorbing stripping carries out a part of heat of combustion reaction generation in gasification combustor 11
Preheat.Coal dust raw material 150 (together with lift gas 140) after preheating carries through connecting tube 20, coal dust raw material
Riser 10, horizontal pipeline section 101, entered bed formula fluidized bed dry distillation reactor by the outlet 102 of horizontal pipeline section 101
The dilute phase section of 9, drops downward in dry distilling close phase section bed.In Fig. 1, reference 19 represents dry distilling close phase section
The interface of bed；The lower section at this interface is dry distilling close phase section bed, is arranged above the reaction of bed formula fluidized bed dry distillation
The dilute phase section of device 9.
B. the coal dust raw material 150 dry distilling close phase section bed in bed formula fluidized bed dry distillation reactor 9 is done
Evaporate reaction, generate coal tar oil gas (referred to as oil gas) and coal dust semicoke.Oil gas flows up into bed formula stream
Change the dilute phase section of bed carbonization reactor 9, together with the lift gas 140 of this dilute phase section of entrance, through being located at bed formula
First group of cyclone separator 8 in fluidized bed dry distillation reactor 9 enters bed formula fluidisation after isolating coal dust semicoke
The oil gas collection chamber 6 at bed carbonization reactor 9 top, then the oil gas by bed formula fluidized bed dry distillation reactor 9 top
Outlet 7 flows out, and enters condensate recovery system.First group of cyclone separator 8 isolated coal dust semicoke is through material
Lower limb drops downward in dry distilling close phase section bed.
Coal dust semicoke in dry distilling close phase section bed flows downward, and enters and is located at the reaction of bed formula fluidized bed dry distillation
Stripper 18 below device 9.In stripper 18, stripping steam 170 it is passed through through stripped vapor distributor 17,
It is stripped off coal dust semicoke entrained oil gas.Stripping steam 170 after the oil gas being stripped off and stripping flows up
Enter bed formula fluidized bed dry distillation reactor 9, flow through dry distilling close phase section bed entrance bed formula fluidized bed dry distillation anti-
Answer the dilute phase section of device 9；Entrance oil gas collection chamber 6 after first group of cyclone separator 8 carries out gas solid separation, then by
Oil gas vent pipe 7 flows out.
C. the coal dust semicoke after stripping in stripper 18 enters gasification combustor through coal dust semicoke conveying pipe 16
11 (entering in circular passage 27).Oxygen intake in air inlet pipe 131 and atomized water steam inlet are respectively to combustion
It is passed through oxygen 132 and atomized water steam 133 in burning gas distributor 13, makes both at burning gases distributor 13
Spray after interior mixing, enter circular passage 27.In circular passage 27, the coal dust semicoke after above-mentioned stripping with
Oxygen 132 contacts with the mixture of atomized water steam 133, carries out combustion reaction with oxygen 132；Generate after burning
Carbon monoxide, carbon dioxide carries through partially combusted coal dust semicoke upwards together with atomized water steam 133
Flowing, enters and is located at the riser gasification reactor 2 above gasification combustor 11.Through partially combusted coal dust
Semicoke (i.e. only some participation combustion reaction of charcoal in coal dust semicoke after stripping) is to following step D
Water gas reaction provides the major heat carrier of heat.Atomized water steam 133 mainly makes the coal dust after stripping half
Jiao reaches spray pattern, so that coal dust semicoke can be sufficiently mixed with oxygen 132, burn.
The charcoal in coal dust semicoke after above-mentioned combustion reaction, mainly stripping and the reaction of oxygen 132.Burning
The gaseous product generated, mainly carbon monoxide and carbon dioxide.Coal dust semicoke after stripping is at gasification, and combustion
During carrying out combustion reaction in device 11, a part of self-contained heat and combustion gas are taken
The heat of band passes to the coal dust raw material in coal dust raw material preheating pipe 12 through the tube wall of coal dust raw material preheating pipe 12
150, coal dust raw material 150 is preheated.
D. in riser gasification reactor 2, enter in riser gasification reactor 2 through partially combusted
Coal dust semicoke and atomized water steam 133 and be passed through riser gasification reactor through gasified water steam inlet tube 201
Gasified water steam 202 in 2 carries out water gas reaction with plug flow along riser gasification reactor 2 is up.
The coal gas (being mainly composed of carbon monoxide and hydrogen) of water gas reaction generation and high temperature coal ash are through horizontal tube 203
Enter coal ash coal gas separator 1.A small amount of remaining water vapour (includes atomized water steam 133 and gasification water vapour
202) carbon monoxide that the step C combustion reaction and in entrance riser gasification reactor 2 generates is the most together
Enter coal ash coal gas separator 1.The carbon monoxide that the combustion reaction of step C generates also counts water gas reaction and is given birth to
In the coal gas become.
Above-mentioned water gas reaction is the endothermic reaction, and dominant response has the coal dust semicoke after stripping at gasification, and combustion
In device 11, the charcoal through part remaining after combustion (includes atomized water steam 133 and gasification water vapour with water vapour
202) reaction generates carbon monoxide and hydrogen, and the entrance also having this remaining charcoal and the combustion reaction of step C to generate carries
Carbon dioxide reaction in riser gasification reactor 2 generates carbon monoxide.After water gas reaction, described coal
Powder semicoke becomes high temperature coal ash (its carbon content is less than 0.05%).
E., in coal ash coal gas separator 1, coal gas and high temperature coal ash (the most a small amount of remaining water vapour) are second
Gas solid separation is carried out in group cyclone separator 24.Isolated coal gas (the most a small amount of remaining water vapour) enters
The coal gas collection chamber 25 at coal ash coal gas separator 1 top, then the gas exit by coal ash coal gas separator 1 top
Pipe 26 flows out, and enters gas recovery system；Isolated high temperature coal ash drops downward into coal ash dense bed through dipleg
In Ceng.It is passed through fluidizing gas 5 (typically to the bottom of coal ash coal gas separator 1 through fluidizing gas distributor 4
The water vapour of 450～550 DEG C), fluidizing gas 5 flows up through coal ash dense-phase bed, makes at coal ash dense-phase bed
In inflation fluidized state；The residue coal that coal ash in coal ash dense-phase bed can also be carried secretly by fluidizing gas 5 simultaneously
Gas is stripped off.The residual gas that fluidizing gas 5 is carried secretly together with the coal ash in the coal ash dense-phase bed being stripped off is
Flowing up into the dilute phase section of coal ash coal gas separator 1 eventually, the entrance on second group of cyclone separator 24 enters
Coal gas collection chamber 25 is entered after carrying out gas solid separation in entering second group of cyclone separator 24, then by gas outlet tube
26 flow out.In Fig. 1, reference 3 represents the interface of coal ash dense-phase bed；The lower section at this interface is that coal ash is close
Phase bed, is arranged above the dilute phase section of coal ash coal gas separator 1.
Above-mentioned step A～E are continuously, circulation carries out；Main operating condition is as follows:
In step A, the temperature after coal dust raw material 150 preheats in coal dust raw material preheating pipe 12 is 450～550 DEG C；
This temperature is measured at the outlet 102 of horizontal pipeline section 101.Coal dust raw material 150 is in coal dust raw material preheating pipe 12
The time of staying (i.e. carrying out the time preheated) is 0.5～3min (minute).Horizontal pipeline section 101 exports the pressure at 102
Power, should be slightly above the operation pressure at bed formula fluidized bed dry distillation reactor 9 top.
The coal dust raw material 150 that the present invention can process, can be brown coal, jet coal, bottle coal, non-caking coal or
Weakly caking coal etc.；Its particle diameter is not more than 3mm, and oil content is 6%～25%, and water content is not higher than 20%.Particle diameter is used
Sieve method measures, water content and oil content Ge Jinfa (the lattice gold low temperature distillation test of GB/T1341-2007 coal
Method) measure.
Lift gas 140 used by step A can be dry gas (key component is methane), is by under ambient temperature
The compression dry gas of dry gas compression, pressure is that 0.15～0.6MPa (pressure that the present invention mentions is table
Pressure).Lift gas 140 can also is that water vapour, and temperature is 200～400 DEG C.
In step B, the coal dust raw material 150 dry distillation reactor time in dry distilling close phase section bed is 2～10min,
The temperature (i.e. dry distillation reactor temperature) of dry distilling close phase section bed is 450～550 DEG C, and bed formula fluidized bed dry distillation is anti-
The operation pressure answering device 9 top is 0.1～0.4MPa, the gas of bed formula fluidized bed dry distillation reactor 9 dilute phase section
Linear speed is 0.2～1.2m/s (meter per second).The temperature of dry distilling close phase section bed, refers to dry distilling close phase section bed
Mean temperature.Gas in described linear gas velocity, the oil gas of mainly coal dust raw material dry distilling generation and water vapour,
And in stripper 18, strip the defocused stripping steam of coal dust half 170 and the oil gas being stripped off.
The dry distillation reactor time preferably 3～6min, the temperature of dry distilling close phase section bed preferably 470～530 DEG C.
The dry distillation reactor time is preferably 3.5～4.5min, and the temperature of dry distilling close phase section bed is preferably 490～510 DEG C.
The diameter of bed formula fluidized bed dry distillation reactor 9 top cylinder shape cylinder is mainly according to bed formula fluid bed
The mobility scale of carbonization reactor 9 dilute phase section linear gas velocity calculates and determines, the height of dry distilling close phase section bed is main
Anti-according to the coal dust raw material 150 dry distillation reactor time in dry distilling close phase section bed and bed formula fluidized bed dry distillation
Answer the reserve of coal dust semicoke in device 9 to calculate to determine, the height master of bed formula fluidized bed dry distillation reactor 9 dilute phase section
To calculate according to the settling height of coal dust semicoke and to determine.
In stripper 18, stripping temperature is 450～550 DEG C；This temperature is coal dust half coke bed in stripper 18
The mean temperature of layer.The coal dust semicoke entered in stripper 18 is stripped out entrained oil gas after stripping；Quilt
Being stripped off carrying secretly the coal dust semicoke of oil gas, its carbon content is generally 65%～85%.The percent that the present invention mentions,
It is percetage by weight.
In step C, the temperature of the atomized water steam 133 being passed through in burning gases distributor 13 is 450～550 DEG C,
The temperature of oxygen 132 is 100～400 DEG C.The time that coal dust semicoke carries out burning in gasification combustor 11 is
3～5min, ignition temperature is 800～900 DEG C (measuring at the top of gasification combustor 11), gasification combustor 11
The operation pressure at top is 0.15～0.5MPa.The flow of oxygen 132 should be controlled, make the coal dust semicoke after stripping
Only carry out part burning.Coal dust semicoke after stripping is after part burning, by the charcoal of burning-off 40%～60%.
In step D, through partially combusted coal dust semicoke in riser gasification reactor 2 with atomized water steam
133 and gasification water vapour 202 to carry out time of water gas reaction be 3～10s (seconds), riser gasification reactor 2
The temperature of top exit is lower than the temperature of bottom inlet 30～60 DEG C, riser gasification reactor 2 top exit
Operation pressure is 0.1～0.4MPa.The temperature of riser gasification reactor 2 bottom inlet, is substantially equal to gas
Change the ignition temperature in burner 11.
In step E, in coal ash coal gas separator 1, the mean temperature of coal ash dense-phase bed is 650～750 DEG C, coal
The operation pressure at ash coal gas separator 1 top is 0.1～0.4MPa, the gas of coal ash coal gas separator 1 dilute phase section
Linear speed is 0.2～1.2m/s.Gas in described linear gas velocity, mainly enters coal ash coal gas separator 1 dilute
The fluidizing gas 5 of section (carry secretly by the coal ash being also fluidized in the coal ash dense-phase bed that gas 5 is stripped off mutually
Residual gas).
The diameter of coal ash coal gas separator 1 top cylinder shape cylinder is mainly according to coal ash coal gas separator 1 dilute phase section
The mobility scale of linear gas velocity calculates and determines, the height of coal ash dense-phase bed is mainly according to coal ash coal gas separator 1
The reserve of interior coal ash calculates and determines, the height of coal ash coal gas separator 1 dilute phase section is mainly according to the sedimentation height of coal ash
Degree calculating determines.
In operation, by a part of high temperature coal ash warp in coal ash dense-phase bed in coal ash coal gas separator 1
Cement output tank 221 sends into external warmer 22, takes heat through external warmer 22, is cooled to 70～80 DEG C.Take heat, cooling
After coal ash, a part therein returns coal ash dense-phase bed through recurrent canal 222, to control coal ash dense-phase bed
Mean temperature at 650～750 DEG C, less than regulation temperature range.Heat, cooling is taken through external warmer 22
After another part coal ash, after pipeline 223 enters coal ash tank 21 timing discharge destructive distillation device.
Claims (3)
1. the fluidized bed dry distillation method of a coal dust, it is characterised in that: the method in turn includes the following steps:
A. the coal dust raw material (150) after pulverizing enters coal dust raw material preheating pipe (12) through coal dust material feeding tube (15)
Bottom, along coal dust raw material preheating under the effect of the lift gas (140) being passed through by lift gas jet pipe (14)
Pipe (12) is up, absorbs the coal dust semicoke after stripping and carries out combustion reaction generation in gasification combustor (11)
Heat preheats, and the coal dust raw material (150) after preheating enters bed formula fluidisation through coal dust raw material riser (10)
Bed carbonization reactor (9)；
In step A, coal dust raw material (150) preheat in coal dust raw material preheating pipe (12) after temperature be 450～
550℃；
B. the coal dust raw material (150) dry distilling close phase section bed in bed formula fluidized bed dry distillation reactor (9) enters
Row dry distillation reactor, generates oil gas and coal dust semicoke, and oil gas is in being located at bed formula fluidized bed dry distillation reactor (9)
First group of cyclone separator (8) to isolate coal dust half defocused by bed formula fluidized bed dry distillation reactor (9) top
Oil gas vent pipe (7) flow out, the coal dust semicoke in dry distilling close phase section bed flows downward, enter be located at bed
The stripper (18) of formula fluidized bed dry distillation reactor (9) lower section, is passed through stripping steam in stripper (18)
(170) coal dust semicoke entrained oil gas, it is stripped off；
In step B, the coal dust raw material (150) the dry distillation reactor time in dry distilling close phase section bed is 2～10min,
The temperature of dry distilling close phase section bed is 450～550 DEG C, the operation at bed formula fluidized bed dry distillation reactor (9) top
Pressure is 0.1～0.4MPa, the linear gas velocity of bed formula fluidized bed dry distillation reactor (9) dilute phase section be 0.2～
1.2m/s, is stripped out carrying secretly the coal dust semicoke of oil gas in stripper (18), and its carbon content is by weight
65%～85%；
C. the coal dust semicoke after stripping in stripper (18) enters gasification, and combustion through coal dust semicoke conveying pipe (16)
Device (11), burns with the oxygen (132) in being passed through gasification combustor (11) through burning gases distributor (13)
Reaction, the carbon monoxide, the carbon dioxide that generate after burning carry through part together with atomized water steam (133)
The coal dust semicoke of burning flows up, and enters riser gasification reactor (2)；
In step C, the time that coal dust semicoke carries out burning in gasification combustor (11) is 3～5min, burning
Temperature is 800～900 DEG C, and the operation pressure at gasification combustor (11) top is 0.15～0.5MPa, coal dust half
Burnt after part burning, by the charcoal of burning-off 40%～60%；
The housing of described gasification combustor (11) includes the cylindrical drum of bottom and the round table surface shape cylinder on top
Body, it is interior that the main part of coal dust raw material preheating pipe (12) is located at gasification combustor (11), coal dust raw material preheating pipe
(12) bottom is stretched out by the bottom of gasification combustor (11)；
D., in riser gasification reactor (2), firing through part in riser gasification reactor (2) is entered
The coal dust semicoke and the atomized water steam (133) that burn and the gasified water steam being passed through in riser gasification reactor (2)
(202) carrying out water gas reaction along riser gasification reactor (2) is up, coal gas and the high temperature coal ash of generation enter
Enter coal ash coal gas separator (1)；
E., in coal ash coal gas separator (1), coal gas and high temperature coal ash enter in second group of cyclone separator (24)
Row gas solid separation, isolated coal gas is flowed out by the gas outlet tube (26) at coal ash coal gas separator (1) top,
Isolated high temperature coal ash drops downward into coal ash dense-phase bed through dipleg, through fluidizing gas distributor (4) to coal ash
The bottom of coal gas separator (1) is passed through fluidizing gas (5), and fluidizing gas (5) flows up through coal ash dense-phase bed,
Coal ash dense-phase bed is made to be in inflation fluidized state, the residue simultaneously carried secretly by the coal ash in coal ash dense-phase bed
Coal gas is stripped off, after the residual gas being stripped off carries out gas solid separation in second group of cyclone separator (24)
Flowed out by gas outlet tube (26), the described water vapour that fluidizing gas (5) is 450～550 DEG C；
A part of high temperature coal ash in coal ash coal gas separator (1) interior coal ash dense-phase bed is through external warmer (22)
After taking heat, cooling, a part therein returns coal ash dense-phase bed, and another part discharges destructive distillation device.
Method for destructive distillation the most according to claim 1, it is characterised in that: in step D, through part burning
Coal dust semicoke in riser gasification reactor (2) with atomized water steam (133) and gasify water vapour (202)
The time carrying out water gas reaction is 3～10s, and the temperature of riser gasification reactor (2) top exit compares bottom
The temperature of entrance is low 30～60 DEG C, the operation pressure of riser gasification reactor (2) top exit be 0.1～
0.4MPa。
Method for destructive distillation the most according to claim 1 and 2, it is characterised in that: coal dust raw material (150) is brown
Coal, jet coal, bottle coal, non-caking coal or weakly caking coal, its particle diameter is not more than 3mm.
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| CN104946282B (en) * | 2015-06-15 | 2017-05-31 | 宋军 | A kind of handling process of smalls |
| CN105623744B (en) * | 2015-12-31 | 2018-06-12 | 西北大学 | The reactor and method of a kind of pyrolysis of coal coupling char Gasification of Driven by Solar Energy |
| CN107723012B (en) * | 2017-09-15 | 2019-08-23 | 王树宽 | The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling |
| CN108148609B (en) * | 2017-12-28 | 2020-06-02 | 胜帮科技股份有限公司 | Integrated pulverized coal pyrolysis reaction device and treatment method thereof |
| CN112625755B (en) * | 2019-09-24 | 2024-09-24 | 中国石油化工股份有限公司 | Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method |
| WO2021108395A1 (en) * | 2019-11-25 | 2021-06-03 | Wormser Energy Solutions, Inc. | Char preparation system and gasifier for all-steam gasification with carbon capture |
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| CN102876342A (en) * | 2012-10-24 | 2013-01-16 | 金先奎 | Method for producing coal tar through coal dry distillation and producing coal gas through coal semi-coke gasification |
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| CN102911686A (en) * | 2011-08-02 | 2013-02-06 | 中国石油化工股份有限公司 | Coal destructive distillation method and apparatus |
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