CN107057770B - A kind of downstriker pyrolysis prepares the device and method of coal tar oil and gas with up flow type gasification coupling - Google Patents
A kind of downstriker pyrolysis prepares the device and method of coal tar oil and gas with up flow type gasification coupling Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
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Abstract
A kind of downstriker pyrolysis prepares the device and method of coal tar oil and gas with up flow type gasification coupling, belong to carbonaceous material chemical technology field, the specifically coal gas of high temperature of the mixed gas entrance access up flow type gasification reactor output of downstriker pyrolysis reactor, heat in gasification reaction product can be efficiently used in pyrolytic reaction, the process to cool down to the coal gas of high temperature as gasification reaction product is in turn avoided simultaneously, part high temperature carbonaceous material in pyrolytic reaction product is exported by returning charge to be sent into gasification reactor, gasification reaction is participated in as gasified raw material, heat needed for being capable of providing gasification reaction, to reduce the consumption of the oxygen in gasification, gasification reaction is of coupled connections with pyrolytic reaction, it will complete gasification and the product of pyrolytic reaction be filtered dedusting, simplify dedusting number, by gasification and the energy after pyrolytic reaction Amount rationally utilizes, the whole energy consumption of alleviator, save the cost.
Description
Technical field
The invention belongs to carbonaceous material chemical technology fields, and in particular to a kind of pyrolysis of downstriker and up flow type gasification coupling
Prepare the device and method of coal tar oil and gas.
Background technique
Carbonaceous material can generate coal tar oil and gas by pyrolytic reaction, carry out pyrolysis process to carbonaceous material, be by
Carbonaceous material is classified sub-prime and can be by a kind of important way of its high-efficiency cleaning utilize.
The detailed process of pyrolysis is to heat carbonaceous material in the absence of air conditions, and carbonaceous material is different
At a temperature of occur a column physical change and chemical reaction complex process, needed during being pyrolyzed to carbonaceous material outer
Boundary provides a large amount of heat, and also can the carbon containing object of the lower high temperature of a large amount of volatility of output in the product of carbonaceous material pyrolysis
Material, pyrolysis can be roughly divided into slow pyrolysis, fast pyrogenation and flashing speed oven according to the difference of its rate of heat addition, theoretically hot
The yield of the more high then coal tar of the rate of heat addition of solution is bigger, but to improve the heating efficiency of pyrolysis, needs to further increase outer
Boundary's heat supply can significantly improve the refinement cost of coal tar in this way.
Carbonaceous material can obtain coal gas product by gasification reaction, and gasification is also to be made full use of to carbonaceous material to be made
A kind of effective mode of coal gas.The detailed process of carbonaceous material gasification is to carry out thermalization to carbonaceous material by using gasifying agent
Processing is learned, is coal gas by the carbon conversion in carbonaceous material.It can be generated during carrying out gasification reaction to carbonaceous material a large amount of
Heat, and use high temperature carbonaceous material as gasification raw material, can also reduce the oxygen demand in gasification.
Application No. is 201110143741.1 granted patent " semi-coke powder gasification with reform gas pyrolysis coupling coal tar and
The device and method of coal gas " in disclose a kind of gasification reaction and pyrolytic reaction are coupled to efficiently use reaction product and mention
The device and method of high oil product yield includes semicoke heating system in device, and entire reaction system is complex, and due to adopting
It is invested larger with the upper gasification and pyrolysis reactor for the formula that connects so that preparation process energy consumption is higher.
Summary of the invention
The embodiment of the present invention provides a kind of pyrolysis of carbonaceous material and gasification coupling prepares device and the side of coal tar oil and gas
Method is able to solve in the preparation process of coal tar oil and gas the problem that system complex, energy consumption are higher, cost is larger.
In order to achieve the above objectives, the embodiment of the present invention adopts the following technical scheme that
A kind of downstriker pyrolysis prepares the device of coal tar oil and gas with up flow type gasification coupling comprising:
Gasification reactor be up flow type structure, including for carrying out gasification reaction gasification furnace and with the gasification furnace bottom
The ash cellar of portion's connection, the ash cellar bottom end is provided with feed opening, is provided with feeding inlet and gas outlet on the gasification furnace, it is described enter
Material mouth is used to be blended with oxygen-containing gas/air and the high temperature carbonaceous material of steam is sent into the gasification furnace, by gasified reverse
The coal gas of high temperature answered is exported by gas outlet；
Pyrolysis reactor is downstriker structure, including reaction chamber and the mixed gas being arranged on the reaction chamber
Entrance, carbonaceous material entrance and material outlet, the mixed gas entrance are connected by pipeline with the gas outlet of gasification furnace, to
Mixed gas is passed through in the reaction chamber, the carbonaceous material entrance inputs carbonaceous material, the material outlet discharge pyrolysis
Reaction product, the pyrolytic reaction product include raw coke oven gas and high temperature carbonaceous material；
The lower end of the reaction chamber, and the material outlet with the reaction chamber is arranged in expansion chamber, the expansion chamber
It is connected, cyclone separator and stripper plant is provided in the expansion chamber, the cyclone separator is set to described heavy
The neighboring area for dropping ceiling portion, for carrying out separating treatment to the raw coke oven gas being passed through, the raw coke oven gas after separation is filled by cyclonic separation
Set that upper end outlet discharge expansion chamber is outer, high temperature carbonaceous material is discharged into expansion chamber, the stripper plant is set to the whirlwind point
Bottom from device, the high temperature carbonaceous material after receiving pyrolysis are stripped, and the bottom of the expansion chamber is provided with returning charge outlet
And product offtake, the indoor high temperature carbonaceous material of sedimentation are discharged by returning charge outlet and product offtake respectively；Wherein, institute
Returning charge outlet is stated to be connected to by pipeline and the returning charge valve being arranged on the pipeline with the feeding inlet of the gasification furnace；
Filter collector is connected with the upper end outlet of the cyclone separator, is dusted to the raw coke oven gas being passed through
Processing；
Oil scrubber, the oil scrubber are connected by pipeline with the filter collector, the raw coke oven gas for that will input point
From exporting for coal gas and coal tar and respectively.
Further preferably, the filter collector is film tube type filter collector or gravel bed filter.
Further preferably, the reaction chamber of the pyrolysis reactor be hollow tube-shape, the lower end of the reaction chamber also
It is connected with accelerating sections, expanding reach and downlink section, the barrel of the accelerating sections is in convergence type, and the barrel of the expanding reach is in expansion
Type, the barrel of the downlink section restrain tapered tubulose, and expanding reach and downlink section extend in expansion chamber.
Further preferably, the cyclone separator is 2~6, and uniformly distributed along the expanding reach periphery of pyrolysis reactor, rotation
The raw coke oven gas entrance of wind separator is connected to the barrel of the expanding reach of pyrolysis reactor, is further revolved to the raw coke oven gas after acceleration
Wind separation.
Further preferably, it is additionally provided with flutter valve on the lower dipleg of the cyclone separator, guides solid in raw coke oven gas
The sedimentation of grain.
Further preferably, above-mentioned apparatus further includes air and gas mixer, and air and gas mixer includes that mixing chamber and setting exist
Coal gas of high temperature access port, circulating gas access port and mixed gas outlet in the mixing chamber, the coal gas of high temperature access
Mouth is connected with the gas outlet of the gasification furnace, and circulating gas access port passes through the gas exit of circulating gas pipeline and oil scrubber
Connection, mixed gas outlet are connected to the mixed gas entrance of pyrolysis reactor.
Further preferably, above-mentioned stripper plant includes cone bucket and is arranged in cone above cone bucket and opposite with cone bucket bottom
Shape drainage tube, the ring type steam pipe that cone bucket bottom is arranged in, offer air hole in cone bucket and taper drainage tube, cone bucket is straight
One end that the biggish one end of diameter and taper drainage tube are relatively large in diameter is opposite, and the cone angle of cone bucket is 55~75 °, the cone of taper drainage tube
Angle is 125~105 °.
A method of coal tar oil and gas is prepared using above-mentioned device comprising,
S101, the high temperature carbonaceous material for being blended with oxygen-containing gas and steam, which are passed through in gasification reactor, carries out whole gasifications
Reaction, wherein the temperature of gasification is 1300~1700 DEG C, pressure is 0.001~8MPa, gas velocity is 5~16m/s, gasification reaction
Melting ash afterwards is discharged into ash cellar；
Coal gas of high temperature after S102, gasification reaction is passed through in air and gas mixer, is 25~80 DEG C with temperature, pressure is
The pyrolysis cyclical coal gas of 0.001~8MPa mixes, and the mixed gas that chilling is 750~950 DEG C, the first in pyrolysis cyclical coal gas
Alkane is activated；
Mixed gas after S103, activation is passed through in the reaction chamber of pyrolysis reactor, and into the pyrolysis reactor
It is passed through carbonaceous material and carries out pyrolytic reaction, wherein the temperature of pyrolytic reaction is 480~750 DEG C, pressure is lower than the gasification reaction
Pressure, gas velocity in device are 3~12m/s；
Raw coke oven gas is generated after S104, pyrolytic reaction and high temperature carbonaceous material, the raw coke oven gas enter in cyclone separator
Separating treatment is carried out, the high temperature carbonaceous material is fallen in expansion chamber, and stripper plant carries out vapour to the high temperature carbonaceous material
It mentions, the temperature of the high temperature carbonaceous material is 480~750 DEG C, wherein high temperature carbonaceous material a part and steam after stripping are mixed
It is sent into gasification reactor after conjunction and participates in gasification reaction, another part is discharged as product；
Raw coke oven gas after S105, separating treatment, which is passed through in filter collector, is dusted processing；
Separating treatment is carried out in raw coke oven gas input oil scrubber after S106, dedusting, coal gas is obtained after separation and coal tar produces
Product, wherein part coal gas product is passed through in air and gas mixer as pyrolysis cyclical coal gas and mixes instead with the coal gas of high temperature after gasification
It answers.
It further limiting, above-mentioned steps S104 further includes,
The raw coke oven gas and high temperature carbonaceous material generated after S1041, pyrolytic reaction is carried out by the accelerating sections of pyrolysis reactor
Accelerate；
The expanding reach that raw coke oven gas and high temperature carbonaceous material after S1042, acceleration pass through pyrolysis reactor；
S1043, raw coke oven gas enter cyclone separator along expanding reach side wall, and high temperature carbonaceous material is since inertial settling is in heavy
Drop is indoor.
It further limits, above-mentioned carbonaceous material is lignite, bituminous coal, coal slime, liquefied residue, stalk, oil shale, tire, stone
Any one or a few mixture in oil coke, biomass, waste plastics and other carbonaceous materials.
The embodiment of the present invention provides a kind of pyrolysis of carbonaceous material and gasification coupling prepares device and the side of coal tar oil and gas
Heat in gasification reaction product can be efficiently used in pyrolytic reaction, while in turn avoided to as gasification reaction by method
The process that the coal gas of high temperature of product cools down, the part high temperature carbonaceous material in pyrolytic reaction product pass through returning charge and export
It is sent into gasification reactor, participates in gasification reaction, heat needed for being capable of providing gasification reaction, to reduce gas as gasified raw material
Oxygen consumption during change, gasification reaction are of coupled connections with pyrolytic reaction, are not necessarily to intermediate treatment link, and simplification of flowsheet is reduced
Oxygen consumption in gasification, substantially increases the utilization rate of carbonaceous material and the yield of coal tar, and the purity of products obtained therefrom
It is higher, in addition, will complete to gasify to be filtered dedusting with the product of pyrolytic reaction, dedusting number is simplified, it will gasification and pyrolysis
Energy after reaction rationally utilizes, the whole energy consumption of alleviator, save the cost, achievees the purpose that energy-saving, reduction operation
Cost, while the oil product of the lighting of high added value, high yield can be produced, it is suitable for industrial applications.
Detailed description of the invention
Fig. 1 is the dress that a kind of carbonaceous material pyrolysis provided in an embodiment of the present invention and gasification coupling prepare coal tar oil and gas
The structural schematic diagram set.
Fig. 2 is the structural schematic diagram of pyrolysis reactor 2.
Appended drawing reference:
1- gasification furnace；2- pyrolysis reactor；2-1- reaction chamber；2-2- accelerating sections；2-3- expanding reach；2-4- downlink section；
3- cyclone separator；4- stripper plant；4-1- ring type steam pipe；4-2- taper drainage tube；4-3 cone bucket；5- expansion chamber；6- mistake
Filtering dust remover；7- oil scrubber；8- ash cellar；9- air and gas mixer；10- flutter valve.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
As shown in Figure 1, the present embodiment provides the dresses that a kind of pyrolysis of carbonaceous material and gasification coupling prepare coal tar oil and gas
It sets, including gasification reactor, gasification reactor includes gasification furnace 1 for carrying out gasification reaction and connects with 1 bottom of gasification furnace
Logical ash cellar 8,8 bottom end of ash cellar are provided with feed opening, feeding inlet and gas outlet are provided on gasification furnace 1, feeding inlet will be for that will mix
Conjunction has the high temperature carbonaceous material of oxygen-containing gas and steam to be sent into gasification furnace 1, by the coal gas of high temperature of gasification reaction by gas outlet
Output.Air and gas mixer 9 connects including mixing chamber and the coal gas of high temperature access port, the circulating gas that are arranged in mixing chamber
Entrance and mixed gas outlet, coal gas of high temperature access port is connected with the gas outlet of gasification furnace 1, by coal gas of high temperature and circulating gas
It is exported after the pyrolysis cyclical coal gas mixing of access port access by gas exit.Pyrolysis reactor 2, including reaction chamber 2-1 and
Mixed gas entrance, carbonaceous material entrance and material outlet on reaction chamber 2-1 are set, and mixed gas entrance passes through pipeline
It is connected with the outlet of the mixed gas of air and gas mixer 9, mixed gas is passed through into reaction chamber 2-1, carbonaceous material entrance is defeated
Enter carbonaceous material, pyrolytic reaction product is discharged in material outlet, and pyrolytic reaction product includes raw coke oven gas and high temperature carbonaceous material.Sedimentation
Room 5, the lower end of reaction chamber 2-1 is arranged in expansion chamber 5, and is connected with the material outlet of reaction chamber 2-1, in expansion chamber 5
It is provided with cyclone separator 3 and stripper plant 4, stripper plant 4 is set to the bottom of cyclone separator 3, receives
High temperature carbonaceous material in pyrolytic reaction product is stripped, and cyclone separator 3 is set to the peripheral region at 5 top of expansion chamber
Domain, for carrying out separating treatment to the raw coke oven gas being passed through, it is heavy that the raw coke oven gas after separation is discharged by 3 upper end outlet of cyclone separator
Drop room 5 is outer, high temperature carbonaceous material is fallen in expansion chamber 5 by lower end outlet, the bottom of expansion chamber 5 be provided with returning charge outlet with
Product offtake, the high temperature carbonaceous material in expansion chamber 5 are discharged by returning charge outlet and product offtake respectively.Wherein, returning charge goes out
Mouth is connected to by pipeline and the returning charge valve being arranged on pipeline with the feeding inlet of gasification furnace 1.Filter collector 6, with whirlwind point
Outlet from device 3 is connected, and is dusted processing to the raw coke oven gas being passed through.Oil scrubber 7, oil scrubber 7 pass through pipeline and filtering
Deduster 6 is connected, for the raw coke oven gas of input to be separated into coal gas and coal tar and is exported respectively, wherein coal gas includes producing
Product output end and circulation conveying end, circulation conveying end are connected to the circulating gas access port of air and gas mixer 9.
It should be noted that first, the gasification reactor in the present invention selects up flow type entrained flow gasification reactor, pyrolysis
Reactor 2 selects downstriker air flow bed pyrolysis reactor 2, and up flow type entrained flow gasification reactor and the pyrolysis of downstriker air flow bed are anti-
Device 2 is answered to be connected, so that the coal gas of high temperature product in gasification reactor by the reaction that is gasified totally is passed directly into downstriker
Pyrolytic reaction is participated in air flow bed pyrolysis reactor 2, thus on the one hand the heat in coal gas of high temperature can be made full use of, it is another
Aspect also eliminates the required processing step that cooling processing is carried out to coal gas of high temperature product after the completion of gasification reaction.
Second, the setting position of the air and gas mixer 9 is set in the present invention without specifically limiting as long as meeting
Between gasification reactor and pyrolysis reactor 2, pass through pipe for a part of final product coal gas as pyrolysis cyclical coal gas
Road inputs in air and gas mixer 9, mix with the coal gas of high temperature generated after gasification reaction, the temperature of pyrolysis cyclical coal gas for 25~
80 DEG C, pressure be 0.001~8MPa, during being mixed with coal gas of high temperature can to coal gas of high temperature generate chilling effect,
In the process, the methane in pyrolysis cyclical coal gas is activated.
Third, the present invention in carbonaceous material refer to lignite, bituminous coal, coal slime, liquefied residue, stalk, oil shale, wheel
Tire, petroleum coke, biomass, waste plastics and other carbonaceous materials or several mixtures.
The coal gas of high temperature of the mixed gas entrance access gasification reactor output of the present embodiment pyrolysis reactor 2, can incite somebody to action
Heat in gasification reaction product efficiently uses in pyrolytic reaction, while in turn avoiding to the high temperature as gasification reaction product
The process that coal gas cools down, the part high temperature carbonaceous material in pyrolytic reaction product pass through returning charge outlet and are sent into gasified reverse
It answers in device, participates in gasification reaction, heat needed for being capable of providing gasification reaction, to reduce in gasification as gasified raw material
Oxygen consumption.Gasification reaction is of coupled connections with pyrolytic reaction, will complete gasification and the product of pyrolytic reaction is filtered dedusting, simplify
Dedusting number rationally utilizes gasification with the energy after pyrolytic reaction, the whole energy consumption of alleviator, save the cost.
Preferably, filter collector 6 is film tube type filter collector 6 or gravel bed filter.
Film tube type filter collector 6 and gravel bed filter can remove raw coke oven gas suitable for apparatus of the present invention
The work of dirt, and above two deduster has the advantages of the operation is stable, high dust collection efficiency.
Further, as shown in Fig. 2, the reaction chamber 2-1 of pyrolysis reactor 2 is hollow tube-shape, in the reaction chamber
The lower end of 2-1 is also connected with the barrel of accelerating sections 2-2, expanding reach 2-3 and downlink section 2-4, the accelerating sections 2-2 in convergence
Type, the barrel of the expanding reach 2-3 are in expanding, and the barrel of the downlink section 2-4 restrains tapered tubulose, expanding reach 2-3 with
Downlink section 2-4 is extended in expansion chamber 5.
So, after mixed gas completes pyrolytic reaction in the reaction chamber 2-1 of pyrolysis reactor 2, downlink first
The raw coke oven gas of generation and mixing for high temperature carbonaceous material are reacted since the barrel of accelerating sections 2-2 is in convergence shape by accelerating sections 2-2
Object is closed by gradually being gathered during accelerating sections 2-2 and accelerating to decline, then mixture, which continues traveling downwardly, passes through expanding reach
The barrel of 2-3, expanding reach 2-3 and the barrel shape of accelerating sections 2-2 are on the contrary, be in divergent shape, the mixture after gathering effect
In the expanding reach 2-3 increased rapidly by barrel, the solid material (high temperature carbonaceous material) in mixture is due to the work of inertia
With along downlink section 2-4 tube wall free-falling, directly fall in expansion chamber 5, the gaseous matter (raw coke oven gas) in mixture is then
Inner wall along expanding reach 2-3 flows into cyclone separator 3.
Stripper plant 4 is provided in expansion chamber 5, stripper plant 4 is carried out to the solid material in expansion chamber 5 plus steam vapour
It mentions, stripping can come out the Oil-gas Separation between the particle and particle of solid material and inside particle.Stripper plant 4 be by
Cone bucket 4-3, ring type steam pipe 4-1 and taper drainage tube 4-2 composition, taper drainage tube 4-2 are fixed on above cone bucket 4-3,
The one end being relatively large in diameter is downward, and the flaring face being relatively large in diameter with cone bucket 4-3, ring type steam pipe 4-1 is fixed on the bottom of cone bucket 4-3
Portion's outer exterior wall offers the air hole that diameter is 1mm or so, control on the side wall of taper drainage tube 4-2 and cone bucket 4-3
Its air penetrability is 80~90% or so, and the hot steam of ring type steam pipe 4-1 is made to sequentially pass through cone bucket 4-3 and taper drainage tube 4-2
The dispersion of air hole circumference, move upwards, and isolated high temperature carbonaceous material is met water vapour and aggravated through taper drainage tube 4-2 folding
Stream is deposited in the bottom of expansion chamber 5 into cone bucket 4-3 discharge, forms multiple baffling, improve steam stripping efficiency, accelerates gas solid separation.
Further, in order to guarantee that blanking is smooth, the cone angle of cone bucket 4-3 is 55~75 °, is preferred with 60 °, the cone of taper drainage tube 4-2
Angle is 125~105 °, is preferred with 120 °.
By the accelerating sections 2-2 and expanding reach 2-3 being arranged in pyrolysis reactor 2, can effectively improve and expanding reach 2-3
Lower end is connected and enters gas, solid separative efficiency and the reaction efficiency of the mixture in expansion chamber 5.
Preferably, as shown in Figure 1, cyclone separator 3 includes cyclone separator cylinder and lower dipleg, cyclone separator
3 raw coke oven gas entrance is connected to the barrel of the expanding reach 2-3 of pyrolysis reactor 2, can be by the raw coke oven gas after pyrolytic reaction
Sufficiently export, raw coke oven gas carry out separating treatment inside Membrane Separator Cylinder for CFB Boiler, pass through bottom by the solid material isolated in raw coke oven gas
The lower dipleg in portion is discharged into expansion chamber 5.Cyclone separator 3 is provided with multiple, and 2~6 are preferred, and along pyrolysis reactor 2
The distribution of the periphery expanding reach 2-3.
It is further preferred that since pyrolysis reactor 2 is usually hollow cylindrical shape, with 2 lower end of pyrolysis reactor
The cyclone separator 3 that is connected of expanding reach 2-3 be it is along the circumferential direction uniformly distributed, further match, have with expanding reach 2-3
Conducive to the quick export of raw coke oven gas.
Further, as shown in Figure 1, being additionally provided with flutter valve 10 on cyclone separator 3, flutter valve 10 is connected to cyclonic separation
On the lower dipleg of device 3, for guiding the sedimentation of solid particle in raw coke oven gas.Since flutter valve 10 is in addition to can be to the solid of downlink
Material guide direction also has opening and closing function, therefore, by the way that flutter valve 10 is arranged on cyclone separator 3, facilitates in whirlwind
Certain material envelope is held in separator blanking surrender, prevents from collaborating.
Preferably, the oxygen-containing gas being passed through to the feeding inlet of gasification furnace 1 is pure oxygen.The oxygen content of pure oxygen is greater than in air
Oxygen content is passed through pure oxygen into gasification furnace 1 and participates in gasification reaction, can be improved gasification reaction efficiency, increases gasification reaction product
Generate the yield of coal gas of high temperature.
The present invention also provides a kind of device systems that coal tar oil and gas is prepared with the pyrolysis of above-mentioned carbonaceous material and gasification coupling
Standby coal tar oil and gas, specific method, as shown in Figure 1, comprising:
S101, the high temperature carbonaceous material for being blended with oxygen-containing gas and steam, which are passed through in gasification reactor, carries out whole gasifications
Reaction, wherein the temperature of gasification is 1300~1700 DEG C, pressure is 0.001~8MPa, gas velocity is 5~16m/s, gasification reaction
Melting ash afterwards is discharged into ash cellar 8.
Coal gas of high temperature after S102, gasification reaction is passed through in air and gas mixer 9, is 25~80 DEG C with temperature, pressure is
The pyrolysis cyclical coal gas of 0.001~8MPa mixes, and the mixed gas that chilling is 750~950 DEG C, the first in pyrolysis cyclical coal gas
Alkane is activated.
Mixed gas after S103, activation is passed through in the reaction chamber 2-1 of pyrolysis reactor 2, and to the pyrolytic reaction
It is passed through carbonaceous material in device 2 and carries out pyrolytic reaction, wherein the temperature of pyrolytic reaction is 480~750 DEG C, pressure is lower than the gasification
Pressure, gas velocity in reactor are 3~12m/s.
Raw coke oven gas is generated after S104, pyrolytic reaction and high temperature carbonaceous material, the raw coke oven gas enter in cyclone separator 3
Separating treatment is carried out, the high temperature carbonaceous material is fallen in expansion chamber 5, and stripper plant 4 carries out the high temperature carbonaceous material
Stripping, the temperature of high temperature carbonaceous material are 480~750 DEG C, wherein high temperature carbonaceous material a part after stripping is mixed with steam
It is sent into gasification reactor afterwards and participates in gasification reaction, another part is discharged as product.
Raw coke oven gas after S105, separating treatment, which is passed through in filter collector 6, is dusted processing.
Separating treatment is carried out in raw coke oven gas input oil scrubber 7 after S106, dedusting, coal gas is obtained after separation and coal tar produces
Product, wherein part coal gas product is passed through in air and gas mixer 9 as pyrolysis cyclical coal gas and mixes instead with the coal gas of high temperature after gasification
It answers.
Gasification reaction is connected by method through the above steps when preparing coal tar oil and gas with pyrolytic reaction process,
The coal gas of high temperature that gasification reaction generates directly is participated in into pyrolytic reaction after mixing chilling, the heat in coal gas of high temperature is being pyrolyzed
It is effectively used in reaction, avoids the loss waste of heat, reduce the energy consumption of device.Meanwhile in quenching process, use
Methane in the pyrolysis cyclical coal gas mixed with coal gas of high temperature is activated, and the methane of activation can also play in pyrolytic reaction
Improve the effect of pyrolytic reaction efficiency.A part after pyrolytic reaction as the high temperature carbonaceous material of product discharge passes through vapor
It pushes in gasification reaction, and the consumption of the oxygen in gasification reaction, safety and environmental protection can be effectively reduced.
In addition, gasification reaction and pyrolytic reaction are of coupled connections, after the completion of gasification reaction and pyrolytic reaction are carried out continuously,
The gaseous product of output is dusted again, simplifies and is required to after gasification reaction and pyrolytic reaction to output in the prior art
The tedious steps that gaseous product is dusted, improve production efficiency.
Further, as shown in Fig. 2, step S104 further includes,
The raw coke oven gas and high temperature carbonaceous material generated after S1041, pyrolytic reaction passes through the accelerating sections 2-2 of pyrolysis reactor 2
Accelerated.
Raw coke oven gas and high temperature carbonaceous material after S1042, acceleration pass through the expanding reach 2-3 of pyrolysis reactor 2.
S1043, raw coke oven gas enter cyclone separator 3 along expanding reach 2-3 side wall, and high temperature carbonaceous material is due to inertial settling
In in expansion chamber 5.
So, can significantly improve pyrolytic reaction generation mixture in expansion chamber 5 gas, the efficiency separated admittedly,
And then improve the production efficiency and purity of target product coal gas and coal tar.
In above-mentioned the illustrating of device for preparing coal tar oil and gas for carbonaceous material pyrolysis and gasification coupling,
Method process through using the device to prepare coal tar oil and gas is described in detail, and details are not described herein again.
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
Those familiar with the art in the technical scope disclosed by the present invention, can easily think of the change or the replacement, and should all contain
Lid is within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (10)
1. the device that a kind of downstriker pyrolysis and up flow type gasification coupling prepare coal tar oil and gas, characterized by comprising:
Gasification reactor be up flow type structure, including for carrying out gasification reaction gasification furnace (1) and with the gasification furnace (1)
The ash cellar (8) of bottom connection, ash cellar (8) bottom end are provided with feed opening, and feeding inlet is provided on the gasification furnace (1) and is gone out
Port, the feeding inlet is used to be blended with oxygen-containing gas/air and the high temperature carbonaceous material of steam is sent into the gasification furnace (1)
It is interior, it is exported by the coal gas of high temperature of gasification reaction by gas outlet；
Pyrolysis reactor (2) is downstriker structure, including reaction chamber (2-1) and setting are on the reaction chamber (2-1)
Mixed gas entrance, carbonaceous material entrance and material outlet, the mixed gas entrance gone out by pipeline and gasification furnace (1)
Port is connected, and mixed gas is passed through in Xiang Suoshu reaction chamber (2-1), and the carbonaceous material entrance inputs carbonaceous material, institute
Material outlet discharge pyrolytic reaction product is stated, the pyrolytic reaction product includes raw coke oven gas and high temperature carbonaceous material；
Expansion chamber (5), the expansion chamber (5) are arranged in the lower end of the reaction chamber (2-1), and with the reaction chamber (2-
1) material outlet is connected, and is provided with cyclone separator (3) and stripper plant (4), the whirlwind in the expansion chamber (5)
Separator (3) is set to the neighboring area at the top of the expansion chamber (5), for carrying out separating treatment to the raw coke oven gas being passed through,
Raw coke oven gas after separation by cyclone separator (3) upper end outlet discharge expansion chamber (5) outside, high temperature carbonaceous material be discharged into expansion chamber
(5) in, the stripper plant (4) is set to the bottom of the cyclone separator (3), the high temperature carbonaceous material after receiving pyrolysis
It is stripped, the bottom of the expansion chamber (5) is provided with returning charge outlet and product offtake, the high temperature in the expansion chamber (5)
Carbonaceous material is discharged by returning charge outlet and product offtake respectively；Wherein, the returning charge outlet by pipeline and is arranged in institute
The returning charge valve stated on pipeline is connected to the feeding inlet of the gasification furnace (1)；
Filter collector (6) is connected with the upper end outlet of the cyclone separator (3), removes to the raw coke oven gas being passed through
Dirt processing；
Oil scrubber (7), the oil scrubber (7) are connected by pipeline with the filter collector (6), the waste coal for that will input
Gas is separated into coal gas and coal tar and exports respectively.
2. the dress that a kind of downstriker pyrolysis according to claim 1 and up flow type gasification coupling prepare coal tar oil and gas
It sets, which is characterized in that the filter collector (6) is film tube type filter collector or gravel bed filter.
3. the dress that a kind of downstriker pyrolysis according to claim 1 and up flow type gasification coupling prepare coal tar oil and gas
It sets, which is characterized in that the reaction chamber (2-1) of the pyrolysis reactor (2) is hollow tube-shape, at the reaction chamber (2-1)
Lower end be also connected with accelerating sections (2-2), expanding reach (2-3) and downlink section (2-4), the barrel of the accelerating sections (2-2) is in
Convergence type, the barrel of the expanding reach (2-3) are in expanding, and the barrel of the downlink section (2-4) is restrained tapered tubulose, expanded
Section (2-3) and downlink section (2-4) are extended in expansion chamber (5).
4. the dress that a kind of downstriker pyrolysis according to claim 3 and up flow type gasification coupling prepare coal tar oil and gas
It sets, which is characterized in that the cyclone separator (3) is 2~6, and along the expanding reach of pyrolysis reactor (2) (2-3) periphery
Uniformly distributed, the barrel of the expanding reach (2-3) of the raw coke oven gas entrance and pyrolysis reactor (2) of cyclone separator (3) is connected to, to acceleration
The further cyclonic separation of raw coke oven gas afterwards.
5. the dress that a kind of downstriker pyrolysis according to claim 4 and up flow type gasification coupling prepare coal tar oil and gas
It sets, which is characterized in that be additionally provided with flutter valve (10) on the lower dipleg of the cyclone separator (3), guide solid in raw coke oven gas
The sedimentation of particle.
6. the dress that a kind of downstriker pyrolysis according to claim 1 and up flow type gasification coupling prepare coal tar oil and gas
It sets, which is characterized in that further include air and gas mixer (9), air and gas mixer (9) includes mixing chamber and is arranged in the mixing
Coal gas of high temperature access port, circulating gas access port on chamber and mixed gas outlet, the coal gas of high temperature access port with it is described
The gas outlet of gasification furnace (1) is connected, and circulating gas access port is connected by circulating gas pipeline and the gas exit of oil scrubber (7)
Logical, mixed gas outlet is connected to the mixed gas entrance of pyrolysis reactor (2).
7. the dress that a kind of downstriker pyrolysis according to claim 1 and up flow type gasification coupling prepare coal tar oil and gas
Set, which is characterized in that the stripper plant (4) include cone bucket (4-3) and setting above the cone bucket (4-3) and with cone bucket (4-
3) the opposite taper drainage tube (4-2) in bottom, setting the bottom cone bucket (4-3) ring type steam pipe (4-1), at cone bucket (4-3)
With air hole is offered on taper drainage tube (4-2), one end that cone bucket (4-3) is relatively large in diameter and taper drainage tube (4-2) are straight
The biggish one end of diameter is opposite, and the cone angle of cone bucket (4-3) is 55~75 °, and the cone angle of taper drainage tube (4-2) is 125~105 °.
8. a kind of prepare coal tar using downstriker as described in any one of claims 1 to 7 pyrolysis and up flow type gasification coupling
The method for preparing coal tar oil and gas with the device of coal gas, which is characterized in that including,
S101, the high temperature carbonaceous material for being blended with oxygen-containing gas and steam, which are passed through in gasification reactor, carries out whole gasified reverses
It answers, wherein the temperature of gasification is 1300~1700 DEG C, pressure is 0.001~8MPa, gas velocity is 5~16m/s, after gasification reaction
Melting ash be discharged into ash cellar (8)；
Coal gas of high temperature after S102, gasification reaction is passed through in air and gas mixer (9), is 25~80 DEG C with temperature, pressure 0.001
The pyrolysis cyclical coal gas of~8MPa mixes, and the mixed gas that chilling is 750~950 DEG C, the methane quilt in pyrolysis cyclical coal gas
Activation；
Mixed gas after S103, activation is passed through in the reaction chambers (2-1) of pyrolysis reactor (2), and to the pyrolytic reaction
It is passed through carbonaceous material in device (2) and carries out pyrolytic reaction, wherein the temperature of pyrolytic reaction is 480~750 DEG C, pressure is lower than the gas
Change the pressure in reactor, gas velocity is 3~12m/s；
Generate raw coke oven gas and high temperature carbonaceous material after S104, pyrolytic reaction, the raw coke oven gas enter in cyclone separator (3) into
Row separating treatment, the high temperature carbonaceous material are fallen in expansion chamber (5), stripper plant (4) to the high temperature carbonaceous material into
Row stripping, the temperature of the high temperature carbonaceous material are 480~750 DEG C, wherein high temperature carbonaceous material a part and steaming after stripping
It is sent into gasification reactor after vapour mixing and participates in gasification reaction, another part is discharged as product；
Raw coke oven gas after S105, separating treatment is passed through in filter collector (6) and is dusted processing；
Separating treatment is carried out in raw coke oven gas input oil scrubber (7) after S106, dedusting, coal gas is obtained after separation and coal tar produces
Product, wherein part coal gas product is passed through in air and gas mixer (9) as pyrolysis cyclical coal gas and mixes with the coal gas of high temperature after gasification
Reaction.
9. the device according to claim 8 for preparing coal tar oil and gas using downstriker pyrolysis and up flow type gasification coupling
The method for preparing coal tar oil and gas, which is characterized in that step S104 further includes,
The raw coke oven gas and high temperature carbonaceous material generated after S1041, pyrolytic reaction passes through the accelerating sections (2-2) of pyrolysis reactor (2)
Accelerated；
Raw coke oven gas and high temperature carbonaceous material after S1042, acceleration pass through the expanding reach (2-3) of pyrolysis reactor (2)；
S1043, raw coke oven gas enter cyclone separator (3) along expanding reach (2-3) side wall, and high temperature carbonaceous material is due to inertial settling
In expansion chamber (5).
10. the dress according to claim 8 for preparing coal tar oil and gas using downstriker pyrolysis and up flow type gasification coupling
Set the method for preparing coal tar oil and gas, which is characterized in that the carbonaceous material is lignite, bituminous coal, coal slime, liquefied residue, oil
Any one or a few mixture in shale, tire, petroleum coke, biomass, waste plastics and other carbonaceous materials.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB656517A (en) * | 1946-09-28 | 1951-08-22 | Standard Oil Dev Co | Improvements in or relating to the conversion of carbonaceous solids into gaseous orvaporous products |
| US4323446A (en) * | 1979-08-30 | 1982-04-06 | Hydrocarbon Research, Inc. | Multi-zone coal conversion process using particulate carrier material |
| CN102994136A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Pyrolysis liquification equipment of downstream circulating fluidized bed of oil shales |
| CN104745222A (en) * | 2015-04-01 | 2015-07-01 | 曲靖众一精细化工股份有限公司 | Moving bed self-heating type pressure gasification hydrogen-rich environment dry distillation furnace and dry distillation method thereof |
| CN103773447B (en) * | 2012-10-18 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of heavy oil contact cracking method contacts cracking unit with heavy oil |
| CN106281383A (en) * | 2016-09-28 | 2017-01-04 | 尚柳彤 | Fine coal fast pyrogenation and char Gasification combined unit and process thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2851570B1 (en) * | 2003-02-24 | 2007-07-27 | Inst Francais Du Petrole | INSTALLATION AND METHOD FOR MULTI-STAGE GASIFICATION OF A LOAD COMPRISING ORGANIC MATTER |
-
2017
- 2017-01-17 CN CN201710031662.9A patent/CN107057770B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB656517A (en) * | 1946-09-28 | 1951-08-22 | Standard Oil Dev Co | Improvements in or relating to the conversion of carbonaceous solids into gaseous orvaporous products |
| US4323446A (en) * | 1979-08-30 | 1982-04-06 | Hydrocarbon Research, Inc. | Multi-zone coal conversion process using particulate carrier material |
| CN102994136A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Pyrolysis liquification equipment of downstream circulating fluidized bed of oil shales |
| CN103773447B (en) * | 2012-10-18 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of heavy oil contact cracking method contacts cracking unit with heavy oil |
| CN104745222A (en) * | 2015-04-01 | 2015-07-01 | 曲靖众一精细化工股份有限公司 | Moving bed self-heating type pressure gasification hydrogen-rich environment dry distillation furnace and dry distillation method thereof |
| CN106281383A (en) * | 2016-09-28 | 2017-01-04 | 尚柳彤 | Fine coal fast pyrogenation and char Gasification combined unit and process thereof |
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