CN207581747U - Catalytic gasification rough coal gas processing system - Google Patents
Catalytic gasification rough coal gas processing system Download PDFInfo
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- CN207581747U CN207581747U CN201721429277.1U CN201721429277U CN207581747U CN 207581747 U CN207581747 U CN 207581747U CN 201721429277 U CN201721429277 U CN 201721429277U CN 207581747 U CN207581747 U CN 207581747U
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- 238000002309 gasification Methods 0.000 title claims abstract description 122
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 37
- 239000003034 coal gas Substances 0.000 title claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims description 102
- 239000010881 fly ash Substances 0.000 claims description 47
- 238000001816 cooling Methods 0.000 claims description 15
- 230000007704 transition Effects 0.000 claims description 12
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 230000007246 mechanism Effects 0.000 claims description 7
- 230000003213 activating effect Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 93
- 239000002245 particle Substances 0.000 abstract description 21
- 239000000428 dust Substances 0.000 abstract description 9
- 230000004913 activation Effects 0.000 abstract description 5
- 238000005243 fluidization Methods 0.000 abstract description 5
- 150000003384 small molecules Chemical class 0.000 abstract description 4
- 239000002737 fuel gas Substances 0.000 abstract 2
- 230000008676 import Effects 0.000 abstract 2
- 230000009466 transformation Effects 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 230000008569 process Effects 0.000 description 13
- 239000003245 coal Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000002956 ash Substances 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 230000003749 cleanliness Effects 0.000 description 3
- 239000002817 coal dust Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 238000004886 process control Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000007781 pre-processing Methods 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
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- Industrial Gases (AREA)
Abstract
The utility model provides a kind of catalytic gasification rough coal gas processing system, which includes：Pretreatment unit, its import is connected with the outlet of gasification furnace, pretreatment unit is used to receive the raw gas of gasification furnace output, and raw gas is pre-processed, so that the heavy tar activation in raw gas, and combine catalyst and flying dust in raw gas and reach the state into supercritical gasification system；The import of supercritical gasification system is connected with the outlet of pretreatment unit, supercritical gasification system is used for the heavy tar after the catalyst, flying dust and activation that receive pretreatment unit output, and flying dust is made to gasify and the heavy tar after activation is made to be decomposed into fuel gas.The utility model makes raw gas preprocessed device and the processing of supercritical gasification system successively, the heavy tar in raw gas is made to be broken down into the fuel gas of small molecule, the little particle flying dust that gasification is taken out of by fluidisation simultaneously, the transformation efficiency of flying dust is improved, increases the yield of tar light oil and gasification product.
Description
Technical Field
The utility model relates to a coal catalytic gasification technical field particularly, relates to a catalytic gasification coarse coal gas processing system.
Background
The coal catalytic gasification technology is an important mode for clean and efficient utilization of coal, and a high-pressure fluidized bed technology is adopted, so that coal and gasifying agents (steam and oxygen) are subjected to gasification reaction under certain conditions under the action of catalysts (alkali metals and alkaline earth metals) to generate methane gas and by-product tar. Referring to fig. 1, in the conventional catalytic gasification process, coal enters a gasification furnace 1 'from a feeding system and undergoes a gasification reaction, and in the gasification furnace 1', tar produced by pyrolysis and a large amount of small-particle fly ash brought along with fluidization, as well as a part of volatilized alkali metal catalyst enter a cyclone system 2 'along with crude gas at an outlet of the gasification furnace 1'. In the cyclone system 2 ', the small particle fly ash is collected by the cyclone system 2', enters the ash returning system 3 'firstly, and then returns to the gasification furnace 1' for secondary gasification. The crude gas at the outlet of the cyclone system 2 ' enters a tar separation system 4 ', and the tar separation system 4 ' condenses and collects tar in the crude gas. The effect of separating dust and tar by adopting the conventional process is poor, mainly because the tar components are complex and the content of heavy tar is high, while the heavy tar has the characteristics of high dew point, high separation and utilization difficulty and the like, and the small-particle fly ash carried along with the heavy tar is very easy to mix and condense in the cyclone system 2 ', which can cause the blockage of pipelines of the cyclone system 2 ' and the ash returning system 3 '. After the cyclone system 2 'and the ash returning system 3' are out of work due to the condensation of heavy tar, a large amount of small-particle fly ash can enter the subsequent tar separation system 4 'and the coal gas cooling system 5', and further the problem of oil-dust blending blockage of a reactor and a pipeline in the subsequent working section can be directly caused to explode in a large area, and further the accident of system shutdown is caused.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides a catalytic gasification raw gas processing system, aim at solving present dust tar separation effect poor, the difficult problem of using.
The utility model provides a catalytic gasification raw gas processing system, this system includes: the inlet of the pretreatment device is communicated with the outlet of the gasification furnace, and the pretreatment device is used for receiving the crude gas output by the gasification furnace and pretreating the crude gas so as to activate heavy tar in the crude gas and combine a catalyst and fly ash in the crude gas to reach a state of entering a supercritical gasification system; the inlet of the supercritical gasification system is communicated with the outlet of the pretreatment device, and the supercritical gasification system is used for receiving the catalyst, the fly ash and the activated heavy tar output by the pretreatment device, gasifying the fly ash and decomposing the activated heavy tar into combustible gas.
Further, in the above catalytic gasification raw gas treatment system, the pretreatment apparatus includes: the inlet of the first reaction chamber is communicated with the outlet of the gasification furnace, and the first reaction chamber is provided with certain pressure and temperature so as to activate heavy tar in the crude gas and pyrolyze fly ash; the temperature is lower than the first reaction chamber and the pressure is equal to the second reaction chamber of the first reaction chamber, the inlet of the second reaction chamber is communicated with the outlet of the first reaction chamber, the outlet of the second reaction chamber is communicated with the inlet of the supercritical gasification system, the second reaction chamber is used for leading the catalyst to take fly ash as a carrier, and further leading the fly ash to bring the catalyst into the supercritical gasification system.
Furthermore, in the above catalytic gasification raw gas treatment system, a baffle mechanism is arranged in the first reaction chamber to increase the residence time of the raw gas in the first reaction chamber.
Further, in the above-mentioned crude gas treatment system for catalytic gasification, the baffle mechanism includes: the first baffles and the second baffles are arranged along the flowing direction of the crude gas; the first end of each first baffle plate is connected to the top wall of the first reaction chamber, and a gap is formed between the second end of each first baffle plate and the bottom wall of the first reaction chamber; the first end of each second baffle is connected to the bottom wall of the first reaction chamber, and the second end of each second baffle has a gap with the top wall of the first reaction chamber.
Furthermore, in the catalytic gasification raw gas treatment system, the first baffle and the second baffle are alternately arranged along the flowing direction of the raw gas.
Furthermore, in the catalytic gasification raw gas treatment system, fins are arranged on the surface of at least one first baffle; and/or the surface of at least one second baffle is provided with fins.
Furthermore, in the above-mentioned crude gas treatment system for catalytic gasification, a cooling device is disposed on the inner wall or the outer wall of the second reaction chamber, so that the temperature of the second reaction chamber is lower than that of the first reaction chamber.
Furthermore, in the catalytic gasification raw gas treatment system, the diameter of the second reaction chamber is 2-4 times of that of the first reaction chamber.
Furthermore, in the catalytic gasification crude gas treatment system, the outlet of the first reaction chamber is communicated with the inlet of the second reaction chamber through the transition region, and the diameter of the transition region is gradually increased along the flowing direction of the crude gas.
Further, in the above catalytic gasification raw gas treatment system, further comprising: and the outlet of the gasification furnace is communicated with the inlet of the pretreatment device through the compression system.
Further, in the above catalytic gasification raw gas treatment system, further comprising: and the inlet of the coal gas cooling system is communicated with the gas outlet of the supercritical gasification system, and the coal gas cooling system is used for receiving and cooling the gas output by the supercritical gasification system.
Compared with the prior art, the utility model discloses in, through install preprocessing device and supercritical gasification system additional at the gasifier export to replace original cyclone system and tar piece-rate system, make the coarse coal gas of gasifier export get into preprocessing device, thereby make heavy matter tar activation in the coarse coal gas, and make catalyst and the flying ash in the coarse coal gas combine to reach the required state of entering supercritical gasification system; then the catalyst, the fly ash and the activated heavy tar at the outlet of the pretreatment device enter a supercritical gasification system, and the activated heavy tar is completely decomposed into small-molecule combustible gas through certain process control, so that the separation of the fly ash and the heavy tar is realized, and meanwhile, the small-particle fly ash brought out by fluidization can be gasified, thereby improving the conversion efficiency of the solid fly ash. It can be seen that before the gas is cooled after the gasification furnace, the fly ash and the heavy tar can be effectively separated through the pretreatment device and the supercritical gasification system, the heavy tar and the fly ash with poor economy are treated, the gas with good cleanliness is obtained, the yield of the light tar and the gasification products is increased, and the overall economy of the process is improved. In addition, the original cyclone system and tar separation system are omitted, so that the process flow of the process system is simplified.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of a catalytic gasification raw gas treatment device in the prior art;
FIG. 2 is a schematic structural diagram of a catalytic gasification raw gas treatment system provided by an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a pretreatment device in a catalytic gasification raw gas treatment system provided by an embodiment of the present invention;
fig. 4 is a schematic structural diagram of a baffle mechanism in a catalytic gasification raw gas treatment system provided by an embodiment of the present invention;
FIG. 5 is a schematic view of another structure of a catalytic gasification raw gas treatment system according to an embodiment of the present invention;
fig. 6 is a schematic structural diagram of another structure of the catalytic gasification raw gas treatment system provided by the embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
Referring to fig. 2, a preferred structure of the catalytic gasification raw gas treatment system provided by the present embodiment is shown. As shown, the system includes: a pretreatment device 1 and a supercritical gasification system 2.
Wherein, the inlet 11 of the pretreatment device 1 is communicated with the outlet 31 of the gasification furnace 3, the pretreatment device 1 can receive the crude gas output by the gasification furnace 3 and pretreat the crude gas, namely, heavy tar in the crude gas is activated to generate small molecular oil, and then the catalyst volatilized in the gasification furnace 3 is trapped and fixed by the small particle fly ash, so that the catalyst and the fly ash in the crude gas are combined to reach the state required by entering the supercritical gasification system 2. The inlet 21 of the supercritical gasification system 2 is communicated with the outlet 12 of the pretreatment device 1, the supercritical gasification system 2 can receive the catalyst, the fly ash and the activated heavy tar output by the pretreatment device 1, gasify the fly ash, and decompose the activated heavy tar into combustible gas, i.e. the heavy tar which is difficult to react in the crude gas can be further decomposed into small molecular hydrocarbon gas by utilizing the characteristic of the supercritical medium in the supercritical gasification system 2, and the pretreated small particle fly ash can be quickly gasified with the supercritical medium under the action of the catalyst. In specific implementation, the supercritical medium can be water, carbon dioxide or other medium with supercritical characteristics, and supercritical water is preferred. The reaction temperature can be set between 500 ℃ and 700 ℃, and the pressure of the reaction system can be between 20MPa and 25 MPa. In addition, a small amount of oxygen can be introduced into the supercritical gasification system 2 to maintain the reaction temperature, the residual residue after gasification can be discharged out of the system along with the supercritical medium, and the residual clean coal gas can enter the subsequent system for cooling.
It should be noted that the structure of the supercritical gasification system 2 is well known to those skilled in the art and will not be described herein.
Compared with the prior art, in the embodiment, the pretreatment device 1 and the supercritical gasification system 2 are additionally arranged at the outlet 31 of the gasification furnace 3 to replace the original cyclone system and tar separation system, so that the crude gas at the outlet of the gasification furnace 3 enters the pretreatment device 1, the heavy tar in the crude gas is activated, and the catalyst and the fly ash in the crude gas are combined to reach the state required by entering the supercritical gasification system 2; then the catalyst, the fly ash and the activated heavy tar at the outlet of the pretreatment device 1 enter a supercritical gasification system 2, and the activated heavy tar is completely decomposed into small molecule combustible gas through certain process control, so that the separation of the fly ash and the heavy tar is realized, and meanwhile, the small particle fly ash brought out by fluidization can be gasified, thereby improving the conversion efficiency of the solid fly ash. It can be seen that, after the gasification furnace 3, before the gas is cooled, the fly ash and the heavy tar can be effectively separated through the pretreatment device 1 and the supercritical gasification system 2, and the heavy tar and the fly ash with poor economy are treated, so that the gas with good cleanliness is obtained, and the yield of the light tar and the gasification products is increased, thereby improving the overall economy of the process. In addition, the original cyclone system and tar separation system are omitted, so that the process flow of the process system is simplified.
Referring to fig. 3, there is shown a preferred structure of the pretreatment device 1 provided in the present embodiment. As shown, the pretreatment device 1 may include: a first reaction chamber 13 and a second reaction chamber 14. Wherein, the inlet 131 of the first reaction chamber 13 is communicated with the outlet 31 of the gasification furnace 3, the first reaction chamber 13 makes hydrogen and water vapor in the crude gas and the heavy tar undergo hydrogenation reaction by setting certain pressure and temperature, in the process, water plays the role of an activating agent, and hydrogen is taken as a reaction medium to undergo hydrogenation reaction with active components of the heavy tar, so that the heavy tar is activated to generate a small molecular oil product with high economy, and further the economy of the whole process is improved. In the first reaction chamber 13, the small particle fly ash is pyrolyzed in the environment of hydrogen, carbon monoxide and water vapor, and the pyrolysis in the high-pressure hydrogen environment slows down the separation process of volatile matters and causes the particle volume of the pyrolyzed small particle fly ash to expand, so that the specific surface area of the particles is increased, and the particles are more easily activated by-OH functional groups in the water vapor. The inlet of the second reaction chamber 14 communicates with the outlet of the first reaction chamber 13, and the outlet 141 of the second reaction chamber 14 communicates with the inlet 21 of the supercritical gasification system 2. The diameter of the second reaction chamber 14 may be 2-4 times the diameter of the first reaction chamber 13, the temperature may be lower than the temperature of the first reaction chamber 13 and the pressure may be equal to the pressure of the first reaction chamber 13. The expanded small particle fly ash has an ultra-high specific surface area and adsorption performance through the activation of the first reaction chamber 13, and the temperature of the second reaction chamber 14 is reduced, so that the curing rate of the catalyst is far greater than the volatilization rate of the catalyst. In the second reaction chamber 14, the catalyst volatilized from the gasification furnace 3 is trapped and fixed by the small particle fly ash, and the activated heavy tar and the fly ash carrying the catalyst enter the supercritical gasification system 2 through the crude gas coming out from the second reaction chamber 14. In the supercritical gasification gas 2, the activated heavy tar is decomposed into combustible gas, and simultaneously, the fly ash can be quickly gasified with the supercritical medium under the action of the catalyst.
When the long flame coal is catalytically gasified, the temperature of the first reaction chamber 13 may be 850 ℃, and the pressure may be 20 MPa; the temperature of the second reaction chamber 14 can be 700 ℃, the pressure can be 20MPa, and the gas velocity of the second reaction chamber 14 can be 0.5 time of the gas velocity of the first reaction chamber 13; the temperature of the supercritical gasification system 2 can be 500 ℃, and the pressure can be 20 MPa; the system realizes continuous and stable operation, and the outlet of the supercritical gasification system 2 has no tar and coal dust particles.
When the lignite is catalytically gasified, the temperature of the first reaction chamber 13 may be 750 ℃, and the pressure may be 22 MPa; the temperature of the second reaction chamber 14 can be 600 ℃, the pressure can be 22MPa, and the gas velocity of the second reaction chamber 14 can be 0.3 time of the gas velocity of the first reaction chamber 13; the temperature of the supercritical gasification system 2 can be 700 ℃, and the pressure can be 22 MPa; the system realizes continuous and stable operation, and the outlet of the supercritical gasification system 2 has no tar and coal dust particles.
When bituminous coal is catalytically gasified, the temperature of the first reaction chamber 13 may be 700 ℃, and the pressure may be 25 MPa; the temperature of the second reaction chamber 14 can be 650 ℃, the pressure can be 25MPa, and the gas velocity of the second reaction chamber 14 can be 0.35 times of the gas velocity of the first reaction chamber 13; the temperature of the supercritical gasification system 2 can be 650 ℃, and the pressure can be 25 MPa; the system realizes continuous and stable operation, and the outlet of the supercritical gasification system 2 has no tar and coal dust particles.
Since the first reaction chamber 13 needs to be set at a certain temperature, the specific surface area of the first reaction chamber 13 should be reduced as much as possible to reduce the heat dissipation of the apparatus. At the same time, in order to meet the reaction requirement, the residence time of the raw gas in the first reaction chamber 13 should be increased as much as possible, i.e. the baffle mechanism 4 can be arranged in the first reaction chamber 13. The baffle mechanism 4 may include: a plurality of first baffles 41 and a plurality of second baffles 42. Wherein each first baffle plate 41 and each second baffle plate 42 can be arranged along the flowing direction of the raw gas, and a first end (an upper end shown in fig. 3) of each first baffle plate 41 can be connected to the top wall of the first reaction chamber 13, and a second end (a lower end shown in fig. 3) of each first baffle plate 41 can have a gap with the bottom wall of the first reaction chamber 13; a first end (an upper end shown in fig. 3) of each second baffle plate 42 may be connected to the bottom wall of the first reaction chamber 13, and a second end (a lower end shown in fig. 3) of each second baffle plate 42 may have a gap with the top wall of the first reaction chamber 13. In addition, the first baffles 41 and the second baffles 42 may be alternately arranged along the flow direction of the raw gas to form serpentine gas passages, thereby further increasing the residence time of the raw gas in the first reaction chamber 13. Meanwhile, in order to increase the residence time of the gas and the degree of turbulence of the gas, fins 43 may be provided on the surface of at least one first baffle plate 41 and/or the surface of at least one second baffle plate 42 to improve the reaction efficiency of the gas in the first reaction chamber 13.
Referring to fig. 4, the inner or outer wall of the second reaction chamber 14 may be provided with a cooling means so that the temperature of the second reaction chamber 14 is lower than that of the first reaction chamber 13. In a specific implementation, the cooling device may be a jacket 5, the jacket 5 is sleeved on the outer wall of the second reaction chamber 14, and low-temperature steam with a temperature lower than that of the first reaction chamber 13 flows through the jacket 5. The temperature of the second reaction chamber 14 can be controlled to be lower than that of the first reaction chamber 13 by controlling the low-temperature steam quantity, and the method is simple and easy to implement.
In the above embodiments, the outlet of the first reaction chamber 13 may be communicated with the inlet of the second reaction chamber 14 through the transition region 15, and the diameter of the transition region 15 gradually increases along the flowing direction of the raw gas, i.e. the transition region 15 is arranged in a conical shape, so that the gas from the outlet of the first reaction chamber 13 enters the second reaction chamber 14 after achieving a better mixing transition. In specific implementation, the diameter of the inlet of the transition zone 15 may be equal to the diameter of the first reaction chamber 13, the diameter of the outlet of the transition zone 15 may be equal to the diameter of the second reaction chamber 14, and the generatrix of the transition zone 15 may form an angle of 30 ℃ to 60 ℃ with the symmetry axis direction of the transition zone 15.
Referring to fig. 5, the system may further include: a compression system 6. The outlet 31 of the gasification furnace 3 can be communicated with the inlet 11 of the pretreatment device 1 through the compression system 6, and the crude gas at the outlet of the gasification furnace 3 can enter the pretreatment device 1 after passing through the compression system 6. It should be noted that when the pressure of the raw gas meets the requirement, the raw gas can be directly fed into the pretreatment device 1 without passing through the compression system 6.
Referring to fig. 6, the system may further include: a gas cooling system 7. The inlet 71 of the gas cooling system 7 can be communicated with the gas outlet 22 of the supercritical gasification system 2, after being treated by the supercritical gasification system 2, the gas enters the gas cooling system 7, and the solid small particle fly ash is discharged along with the supercritical medium, so that the effects of crude gas oil-dust separation and comprehensive utilization are achieved, and finally, dust-free and oil-free clean gas is obtained.
In summary, compared with the prior art, in the embodiment, the pretreatment device and the supercritical gasification system are additionally arranged at the outlet of the gasification furnace to replace the original cyclone system and the tar separation system, so that the raw gas at the outlet of the gasification furnace enters the pretreatment device, the heavy tar in the raw gas is activated, and the catalyst and the fly ash in the raw gas are combined to reach the state required by entering the supercritical gasification system; then the catalyst, the fly ash and the activated heavy tar at the outlet of the pretreatment device enter a supercritical gasification system, and the activated heavy tar is completely decomposed into small-molecule combustible gas through certain process control, so that the separation of the fly ash and the heavy tar is realized, and meanwhile, the small-particle fly ash brought out by fluidization can be gasified, thereby improving the conversion efficiency of the solid fly ash. It can be seen that before the gas is cooled after the gasification furnace, the fly ash and the heavy tar can be effectively separated through the pretreatment device and the supercritical gasification system, the heavy tar and the fly ash with poor economy are treated, the gas with good cleanliness is obtained, the yield of the light tar and the gasification products is increased, and the overall economy of the process is improved. In addition, the original cyclone system and tar separation system are omitted, so that the process flow of the process system is simplified.
It will be apparent to those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (11)
1. A catalytic gasification raw gas treatment system, comprising:
the pretreatment device (1) is communicated with an inlet (11) of the gasification furnace (3) and is used for receiving the crude gas output by the gasification furnace (3) and pretreating the crude gas to activate heavy tar in the crude gas and combine a catalyst and fly ash in the crude gas to enter a supercritical gasification system (2);
an inlet (21) of the supercritical gasification system (2) is communicated with an outlet (12) of the pretreatment device (1), and the supercritical gasification system (2) is used for receiving the catalyst, the fly ash and the activated heavy tar output by the pretreatment device (1), gasifying the fly ash and decomposing the activated heavy tar into combustible gas.
2. The catalytic gasification raw gas treatment system according to claim 1, wherein the pretreatment device (1) comprises:
a first reaction chamber (13), an inlet (131) of which is communicated with an outlet (31) of the gasification furnace (3), wherein the first reaction chamber (13) is used for activating heavy tar in the crude gas and pyrolyzing the fly ash by setting certain pressure and temperature;
and the inlet of the second reaction chamber (14) is communicated with the outlet of the first reaction chamber (13), the outlet (141) of the second reaction chamber (14) is communicated with the inlet (21) of the supercritical gasification system (2), and the second reaction chamber (14) is used for enabling the catalyst to take the fly ash as a carrier so as to bring the catalyst into the supercritical gasification system (2).
3. The catalytic gasification raw gas treatment system according to claim 2,
a baffle mechanism (4) is arranged in the first reaction chamber (13) to increase the residence time of the crude gas in the first reaction chamber (13).
4. The catalytic gasification raw gas treatment system according to claim 3, wherein the baffle mechanism (4) comprises: a plurality of first baffles (41) and a plurality of second baffles (42) arranged along the flowing direction of the raw gas; wherein,
the first end of each first baffle plate (41) is connected to the top wall of the first reaction chamber (13), and the second end of each first baffle plate (41) has a gap with the bottom wall of the first reaction chamber (13);
the first end of each second baffle plate (42) is connected to the bottom wall of the first reaction chamber (13), and the second end of each second baffle plate (42) has a gap with the top wall of the first reaction chamber (13).
5. The catalytic gasification raw gas treatment system according to claim 4,
the first baffle plates (41) and the second baffle plates (42) are alternately arranged along the flowing direction of the crude gas.
6. The catalytic gasification raw gas treatment system according to claim 4 or 5,
the surface of at least one first baffle (41) is provided with fins (43); and/or
The surface of at least one of the second baffles (42) is provided with fins (43).
7. The catalytic gasification raw gas treatment system according to any one of claims 2 to 5,
the inner wall or the outer wall of the second reaction chamber (14) is provided with a cooling device so that the temperature of the second reaction chamber (14) is lower than the temperature of the first reaction chamber (13).
8. The catalytic gasification raw gas treatment system according to any one of claims 2 to 5,
the diameter of the second reaction chamber (14) is 2-4 times the diameter of the first reaction chamber (13).
9. The catalytic gasification raw gas treatment system according to any one of claims 2 to 5,
the outlet of the first reaction chamber (13) is communicated with the inlet of the second reaction chamber (14) through a transition region (15), and the diameter of the transition region (15) is gradually increased along the flowing direction of the raw gas.
10. The catalytic gasification raw gas treatment system of any one of claims 1 to 5, further comprising:
a compression system (6), wherein the outlet (31) of the gasification furnace (3) is communicated with the inlet (11) of the pretreatment device (1) through the compression system (6).
11. The catalytic gasification raw gas treatment system of any one of claims 1 to 5, further comprising:
and an inlet (71) of the coal gas cooling system (7) is communicated with the gas outlet (22) of the supercritical gasification system (2), and the coal gas cooling system (7) is used for receiving and cooling the gas output by the supercritical gasification system (2).
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