CN114806646B - Double-bed system and method for reducing tar content in synthesis gas - Google Patents
Double-bed system and method for reducing tar content in synthesis gas Download PDFInfo
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- CN114806646B CN114806646B CN202210456196.XA CN202210456196A CN114806646B CN 114806646 B CN114806646 B CN 114806646B CN 202210456196 A CN202210456196 A CN 202210456196A CN 114806646 B CN114806646 B CN 114806646B
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- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 124
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000000463 material Substances 0.000 claims abstract description 122
- 238000002309 gasification Methods 0.000 claims abstract description 117
- 238000002485 combustion reaction Methods 0.000 claims abstract description 102
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 67
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 66
- 238000000605 extraction Methods 0.000 claims abstract description 25
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 176
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 33
- 239000003546 flue gas Substances 0.000 claims description 32
- 238000007664 blowing Methods 0.000 claims description 19
- 238000000746 purification Methods 0.000 claims description 19
- 238000011084 recovery Methods 0.000 claims description 13
- 239000002918 waste heat Substances 0.000 claims description 13
- 230000009977 dual effect Effects 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims 2
- 239000003245 coal Substances 0.000 abstract description 13
- 239000002028 Biomass Substances 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 description 8
- 238000005336 cracking Methods 0.000 description 5
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 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
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
Images
Classifications
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- 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
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
- C10K3/003—Reducing the tar content
- C10K3/008—Reducing the tar content by cracking
-
- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The disclosure relates to the technical field of coal and biomass gasification, in particular to a double-bed system and a method for reducing tar content in synthesis gas. The double-bed system for reducing the tar content in the synthesis gas comprises a gasification furnace, a combustion furnace and a synthesis gas leading-out cylinder, wherein the gasification furnace is provided with a gasification furnace overflow port for leading return materials into the combustion furnace, the combustion furnace is used for heating the return materials to form high-temperature materials, and the synthesis gas leading-out cylinder is used for receiving the high-temperature materials. The method comprises the steps of separating out part of carbon in the return material M of the gasification furnace to the combustion furnace, adding the part of carbon into a synthesis gas extraction cylinder, feeding the other part of circulating material in the return material M of the gasification furnace into the combustion furnace through a return feeder, heating the circulating material in the combustion furnace, and feeding the heated circulating material into the synthesis gas extraction cylinder. The synthesis gas I can be cracked under the high-temperature environment and the carbon-rich working condition, so that the tar content in the synthesis gas I is greatly reduced.
Description
Technical Field
The disclosure relates to the technical field of coal and biomass gasification, in particular to a double-bed system and a method for reducing tar content in synthesis gas.
Background
The double fluidized bed gasification technology comprises two fluidized bed reactors, one is a gasification furnace, the other is a combustion furnace, high-temperature superheated steam is introduced into the gasification furnace to be fluidized gas and a gasification agent, air is introduced into the combustion furnace to be fluidized gas and a combustion improver, coal or biomass enters the gasification furnace through a feeder, the coal and the biomass are pyrolyzed at high temperature, carbon in the coal and the biomass and the steam are subjected to gasification reaction to generate carbon monoxide, hydrogen, carbon dioxide, methane and the like, unreacted carbon, inert bed materials, coal or biomass ash enter the combustion furnace through a return feeder to be combusted at high temperature, and the heated inert bed materials and the coal or biomass ash enter the gasification furnace through the return feeder to provide heat for pyrolysis and gasification of fuel in the gasification furnace. The reaction temperature of the gasification furnace is 700-800 ℃, and the reaction temperature of the combustion furnace is 950-1000 ℃.
The heat required by gasification in the gasification furnace of the double fluidized bed gasification technology is provided by high-temperature circulating materials generated after carbon in the combustion furnace is combusted, oxygen or air does not need to be introduced into the gasification furnace for combustion and heat release, and the combustible gas produced by the gasification furnace has high effective gas component, high heat value and better economic benefit.
In order to improve the cold gas efficiency of the double-bed coal and biomass gasification system, the optimal reaction temperature of the double-bed system gasification furnace is 700-800 ℃, but the synthetic gas generated by the gasification furnace at the temperature contains a certain amount of tar, when the temperature of the synthetic gas is reduced, the tar is easy to bond, so that the pipeline is blocked, and the treatment difficulty of the post-synthetic gas system is increased.
Disclosure of Invention
In order to solve the above technical problems, the present disclosure provides a dual bed system and method for reducing tar content in syngas.
The first aspect of the present disclosure provides a dual-bed system for reducing tar content in syngas, comprising a gasification furnace, a combustion furnace and a syngas extraction barrel;
the synthesis gas outlet cylinder comprises a first cylinder body and a second cylinder body which are arranged up and down, the first cylinder body is positioned outside the gasification furnace, and the first cylinder body is provided with a synthesis gas outlet;
the second cylinder is positioned in the gasification furnace, and a storage tank arranged around the second cylinder is arranged on the outer side of the second cylinder;
the second cylinder body is provided with a gas guide pipe for communicating the storage tank with the second cylinder body, so that the synthetic gas generated by the gasification furnace enters the storage tank, then enters the second cylinder body through the gas guide pipe and is discharged from the synthetic gas outlet;
the gasification furnace is provided with a gasification furnace overflow port for introducing the return material into the combustion furnace, the combustion furnace is used for heating the return material to form high-temperature material, and the synthesis gas leading-out cylinder is used for receiving the high-temperature material.
Furthermore, the double-bed system for reducing the tar content in the synthesis gas also comprises a carbon separator and a cyclone separator;
the feeding hole of the carbon separator is communicated with the overflow port of the gasification furnace, the first outlet of the carbon separator is communicated with the combustion furnace through a first return feeder, the second outlet of the carbon separator is communicated with the cyclone separator, and the cyclone separator is communicated with the first cylinder through a third return feeder.
Furthermore, the double-bed system for reducing the tar content in the synthesis gas further comprises a combustion furnace cyclone separator, wherein a feeding port of the combustion furnace cyclone separator is communicated with the combustion furnace, and a discharging port of the combustion furnace cyclone separator is communicated with the first cylinder through a second material returning device and is used for introducing high-temperature materials formed by the combustion furnace into the first cylinder.
Further, the combustion furnace cyclone separator is sequentially communicated with the first waste heat recovery device and the flue gas purification device, and the flue gas purification device is communicated with the carbon separator through a flue gas circulating fan.
Further, a material returning device in the furnace is arranged at the bottom of the second cylinder, and a material returning blowing air port is formed in the material returning device in the furnace;
the synthesis gas outlet is communicated with the second waste heat recovery device and the synthesis gas purification device in sequence, and the synthesis gas purification device is connected with the synthesis gas compressor and the return blowing air port in sequence.
Furthermore, the first cylinder is provided with an upper thermocouple and a lower thermocouple, and the upper thermocouple and the lower thermocouple are arranged at intervals along the height direction of the first cylinder.
Further, the distance L between the upper thermocouple and the lower thermocouple satisfies: l is more than or equal to 500mm and less than or equal to 1000mm.
Further, the gas guide pipe is inclined downwards along the direction from the storage tank to the synthesis gas leading-out cylinder;
the included angle alpha between the air duct and the horizontal direction meets the following requirements: alpha is more than or equal to 45 degrees.
Furthermore, the number of the air guide pipes is set to be a plurality, and the air guide pipes are uniformly distributed along the circumferential direction of the second cylinder body.
A second aspect of the present disclosure provides a method of reducing tar content in syngas, comprising:
the synthesis gas I generated by the gasification furnace returns downwards at the top of the gasification furnace, enters a storage tank and enters a synthesis gas leading-out cylinder filled with high-temperature circulating materials through a gas guide pipe;
adding part of carbon-containing return materials in the return materials M of the gasification furnace into the synthesis gas extraction cylinder; the residual part in the return material M of the gasification furnace is used as a circulating material and is sent into the combustion furnace through the return feeder, the circulating material is heated in the combustion furnace, the heated circulating material and the flue gas K pass through the cyclone separator of the combustion furnace, and the high-temperature circulating material separated by the cyclone separator of the combustion furnace enters the synthesis gas extraction cylinder through the second return feeder.
Further, controlling the air quantity C of the combustion furnace and the fluidized flue gas quantity D of the carbon separator, and maintaining the measured temperature of a thermocouple of the combustion furnace cyclone separator in the combustion furnace cyclone separator at 950-980 ℃;
controlling the material returning amount M of the gasification furnace to the combustion furnace, and maintaining the temperature measured by a thermocouple of the gasification furnace at 700-800 ℃;
when the temperature difference between the upper thermocouple in the synthesis gas leading-out cylinder and the thermocouple of the cyclone separator of the combustion furnace is within +/-20 ℃, the amount of the returned synthesis gas G in the returned synthesis gas blowing port is increased.
When the temperature difference between the upper thermocouple and the lower thermocouple in the synthesis gas leading-out cylinder and the gasifier thermocouple is within +/-20 ℃, the amount of the returned synthesis gas G in the returned synthesis gas blowing port is reduced.
Compared with the prior art, the technical scheme provided by the embodiment of the disclosure has the following advantages:
in the double-bed system and the method for reducing the tar content in the synthesis gas, the synthesis gas I generated by the gasification furnace is returned downwards at the top of the gasification furnace, passes through the gasification furnace storage tank filled with high-temperature circulating materials and the synthesis gas extraction cylinder and is discharged. The method comprises the steps of separating out part of carbon in the return material M of the gasification furnace to the combustion furnace, adding the part of carbon into a synthesis gas extraction cylinder, feeding the other part of circulating material in the return material M of the gasification furnace into the combustion furnace through a return feeder, heating the circulating material in the combustion furnace, and feeding the heated circulating material into the synthesis gas extraction cylinder. The synthesis gas I can be cracked under the high-temperature environment and the carbon-rich working condition, so that the tar content in the synthesis gas I is greatly reduced.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
FIG. 1 is a schematic diagram of a dual bed system for reducing tar content in syngas according to an embodiment of the present disclosure;
FIG. 2 is a schematic diagram of a gasifier in a dual bed system for reducing tar content in syngas according to an embodiment of the present disclosure.
Reference numerals: 1. a gasification furnace; 11. a high-temperature circulating material feeding hole; 12. a syngas lead-out; 13. a catalyst addition port; 14. an upper thermocouple; 15. a lower thermocouple; 16. a gasifier barrel; 17. a syngas extraction drum; 171. a first cylinder; 172. a second cylinder; 18. a storage tank; 19. a gasifier thermocouple; 110. a material returning device in the furnace; 111. a return blowing air port; 112. an air chamber; 113. a slag discharge pipe of the gasification furnace; 114. an overflow port; 115. an air duct; 116. introducing fine powder carbon; 2. a carbon separator; 3. a cyclone separator; 4. a third material returning device; 5. a first material returning device; 6. a combustion furnace; 7. a furnace cyclone; 71. a furnace cyclone thermocouple; 8. a second material returning device; 9. a flue gas circulating fan; 10. a synthesis gas compressor; 201. a first waste heat recovery device; 202. a flue gas purification device; 203. a second waste heat recovery device; 204. a syngas purification device.
Detailed Description
In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced in other ways than those described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.
Referring to fig. 1 and 2, a dual-bed system for reducing tar content in syngas according to an embodiment of the present disclosure includes a gasification furnace 1, a combustion furnace 6, and a syngas extraction cylinder 17; the gasification furnace 1 comprises a gasification furnace cylinder 16, the gasification furnace cylinder 16 is provided with a high-temperature circulating material feeding hole 11, the bottom of the gasification furnace cylinder 16 is provided with a gasification furnace slag discharging pipe 113, the gasification furnace cylinder 16 is internally provided with a gas chamber 112, and the side wall of the gasification furnace cylinder 16 is provided with a fine carbon powder inlet 116.
The synthetic gas leading-out cylinder 17 comprises a first cylinder 171 and a second cylinder 172 which are arranged up and down, the first cylinder 171 is positioned outside the gasification furnace 1, and the first cylinder 171 is provided with a synthetic gas leading-out port 12; the second cylinder 172 is positioned inside the gasification furnace 1, and a storage tank 18 arranged around the second cylinder 172 is arranged outside the second cylinder 172; the second cylinder 172 is provided with a gas guide pipe 115 for communicating the storage tank 18 and the second cylinder 172, so that the synthetic gas generated by the gasification furnace 1 enters the storage tank 18, then enters the second cylinder 172 through the gas guide pipe 115, and is discharged from the synthetic gas outlet 12; the gasification furnace 1 is provided with a gasification furnace overflow port 114 for introducing the return material into the combustion furnace 6, the combustion furnace 6 is used for heating the return material to form high-temperature material, and the synthesis gas outlet cylinder 17 is used for receiving the high-temperature material.
The synthesis gas I generated by the gasification furnace returns downwards at the top of the gasification furnace 1 and is discharged after passing through a gasification furnace storage tank 18 filled with high-temperature circulating materials and a synthesis gas leading-out cylinder 17. By feeding a part of the circulating material in the return M of the gasification furnace 1 through the first return feeder 5 into the combustion furnace 6, the circulating material is heated in the combustion furnace 6, and the heated circulating material enters the synthesis gas outlet cylinder 17. The synthesis gas I can be cracked under the high-temperature environment, so that the tar content in the synthesis gas I is greatly reduced.
The syngas in the embodiments of the present disclosure may be a gas generated after gasification of coal and/or biomass.
In some embodiments, the dual bed system for reducing tar content in syngas further comprises a carbon separator 2 and a cyclone 3; the feed inlet of the carbon separator 2 is communicated with the overflow port 114 of the gasification furnace, the first outlet of the carbon separator 2 is communicated with the combustion furnace 6 through a first return feeder 5, the second outlet of the carbon separator 2 is communicated with a cyclone separator 3, and the cyclone separator 3 is communicated with the first cylinder 171 through a third return feeder 4. Coal or biomass A is added into a fluidized bed gasification furnace 1, after gasification reaction is carried out between the coal or biomass A and water vapor B in the gasification furnace 1, return M containing residual semicoke enters a carbon separator 2 through an overflow port 114 of the gasification furnace, the return M generates a fluidized state in the carbon separator 2, fine-particle carbon N is carried out of the carbon separator 2 by fluidized flue gas D, the fluidized flue gas D1 carrying the fine-particle carbon N enters a cyclone separator 3, and the fine-particle carbon is separated and enters a synthetic gas leading-out cylinder 17 through a third return feeder 4, so that catalysis is carried out on cracking of tar in the synthetic gas.
The synthesis gas I generated by the gasification furnace returns downwards at the top of the gasification furnace 1 and is discharged after passing through a gasification furnace storage tank 18 filled with high-temperature circulating materials and a synthesis gas leading-out cylinder 17. A part of carbon in the return material M of the gasification furnace 1 to the combustion furnace 6 is separated, the carbon is also added into the synthesis gas extraction cylinder 17, a part of circulating material in the return material M of the gasification furnace 1 is sent into the combustion furnace 6 through the first return feeder 5, the circulating material is heated in the combustion furnace 6, and the heated circulating material enters the synthesis gas extraction cylinder 17. The synthesis gas I can be cracked under the high-temperature environment and the carbon-rich working condition, so that the tar content in the synthesis gas I is greatly reduced.
In some specific embodiments, the dual-bed system for reducing the tar content of the syngas further includes a combustion furnace cyclone 7, a feeding port of the combustion furnace cyclone 7 is communicated with the combustion furnace 6, a discharging port of the combustion furnace cyclone 7 is communicated with the first cylinder 171 through the second return feeder 8, and is used for introducing high-temperature materials formed in the combustion furnace 6 into the first cylinder 171, the circulating materials are heated in the combustion furnace 6, and the heated circulating materials enter the first cylinder 171 of the syngas discharge cylinder 17. The synthesis gas I can be cracked under the high-temperature environment and the carbon-rich working condition, so that the tar content in the synthesis gas I is greatly reduced.
In some specific embodiments, the furnace cyclone 7 is sequentially communicated with the first waste heat recovery device 201 and the flue gas purification device 202, and the flue gas purification device 202 is communicated with the carbon separator 2 through the flue gas circulating fan 9. The return material M is sent into a combustion furnace 6 through a first return feeder 5, residual carbon in the combustion furnace and air C are subjected to combustion reaction, the circulating material is heated in the combustion furnace, the heated circulating material and flue gas K pass through a combustion furnace cyclone separator 7, the flue gas led out from the upper part of the combustion furnace cyclone separator 7 is discharged into a chimney after passing through a first waste heat recovery device 201 and a flue gas purification device 202, and the high-temperature circulating material separated by the combustion furnace cyclone separator 7 enters a synthesis gas leading-out cylinder 17 through a second return feeder 8, so that a high-temperature environment is provided for tar cracking in the synthesis gas.
In some specific embodiments, the bottom of the second cylinder 172 is provided with an in-furnace return feeder 110, and the in-furnace return feeder 110 is provided with a return blowing air port 111; the syngas discharge port 12 is sequentially communicated with the second waste heat recovery device 203 and the syngas purification device 204, and the syngas purification device 204 is sequentially connected with the syngas compressor 10 and the return blowing air port 111. The return gas in the return blowing gas port 111 is selected as the synthesis gas G, and the synthesis gas G is sent into the return blowing gas port 111 through the synthesis gas compressor 10 after being cooled by the waste heat recovery device and purified by the synthesis gas purification device, and the advantage of selecting the synthesis gas is that the content of the effective gas in the synthesis gas can be reduced by selecting other gases.
Taking the combustion product as coal and the gas as coal gas as an example, the coal A is added into the fluidized bed gasification furnace 1, after gasification reaction with the water vapor B occurs in the gasification furnace 1, the return material M containing residual semicoke enters the carbon separator 2 through the gasification furnace overflow port 114, and the fluidized flue gas D passing through the flue gas purification device 202 enters the carbon separator 2 through the flue gas circulating fan 9 to be used as the fluidized gas of the carbon separator 2.
The return material M generates a fluidized state in the carbon separator 2, fine carbon particles N are carried out of the carbon separator 2 by the fluidized flue gas D, the fluidized flue gas D1 carrying the fine carbon particles N enters the cyclone separator 3, the fine carbon particles are separated and enter the synthesis gas leading-out cylinder 17 through the third return feeder 4 to play a catalytic role in the cracking of tar in the synthesis gas, and the fluidized flue gas D1 enters a flue gas pipeline between the cyclone separator 7 and the first waste heat recovery device 201 from the upper part of the cyclone separator 3.
The rest of the return materials M are sent into a combustion furnace 6 through a first return feeder 5, residual carbon in the combustion furnace and air C are subjected to combustion reaction, the circulating materials are heated in the combustion furnace 6, the heated circulating materials and smoke K pass through a combustion furnace cyclone separator 7, the smoke led out from the upper part of the combustion furnace cyclone separator 7 is discharged into a chimney after passing through a first waste heat recovery device 201 and a smoke purification device 202, and the high-temperature circulating materials separated by the combustion furnace cyclone separator 7 enter a synthesis gas leading cylinder 17 through a second return feeder 8, so that a high-temperature environment is provided for the cracking of tar in the synthesis gas.
Then the high-temperature circulating material enters the gasification furnace 1 through the vertical pipe at the bottom of the second cylinder 172 and the in-furnace material returning device 110 to provide heat for the gasification reaction in the gasification furnace 1, and then the circulating material M after the gasification reaction enters the carbon separator 2 device again to perform reciprocating circulation in sequence.
In some embodiments, the first cylinder 171 is provided with the upper thermocouple 14 and the lower thermocouple 15, and the upper thermocouple 14 and the lower thermocouple 15 are spaced apart in a height direction of the first cylinder 171.
In some embodiments, the spacing L between the upper thermocouple 14 and the lower thermocouple 15 satisfies: l is more than or equal to 500mm and less than or equal to 1000mm; the combustion furnace cyclone separator 7 is provided with a combustion furnace cyclone separator thermocouple 71; the gasification furnace 1 is provided with a gasification furnace thermocouple 19, and the synthesis gas extraction cylinder 17 thermocouple comprises an upper thermocouple 14 and a lower thermocouple 15. The small distance between the upper thermocouple 14 and the lower thermocouple 15 can cause repeated adjustment of the returned material blowing gas 111, the large distance between the upper thermocouple 14 and the lower thermocouple 15 can cause lag in adjustment, and the material level height of the synthesis gas leading-out cylinder 17 can ensure that the time for the synthesis gas to pass through the synthesis gas leading-out cylinder 17 is more than or equal to 10s.
In some embodiments, the gas duct 115 slopes downward in the direction from the storage tank 18 to the syngas extraction drum 17; the included angle alpha between the air duct 115 and the horizontal direction satisfies the following condition: alpha is more than or equal to 45 degrees. The lower part of the second cylinder 172 of the synthetic gas leading-out cylinder 17 is provided with a gas guide pipe 115, so that the synthetic gas I can enter the storage tank 18 of the gasification furnace through the gas guide pipe 115, the included angle formed by the gas guide pipe 115 and the horizontal line is more than or equal to 45 degrees, and the materials can be prevented from being accumulated in the gas guide pipe 115.
In some specific embodiments, the number of the air ducts 115 is provided in plurality, and the plurality of air ducts 115 are uniformly distributed along the circumference of the second cylinder 172. Optionally, the number of the gas guide pipes 115 is greater than or equal to 3, the gas guide pipes are uniformly distributed in the circumferential direction, the gas guide pipes 115 have certain resistance, so that gas can be uniformly distributed, the synthesis gas is uniformly introduced into the synthesis gas leading-out cylinder 17, and a gap does not exist at the contact position of the gasifier storage tank 18 and the bottom of the synthesis gas leading-out cylinder, so that the synthesis gas can completely enter the synthesis gas leading-out cylinder 17 through the gas guide pipes. The returned gas in the returned blowing gas port 111 is selected as the synthesis gas G, and the synthesis gas G is cooled by the second waste heat recovery device 203 and purified by the synthesis gas purification device 204, and then is sent into the returned blowing gas port 111 by the synthesis gas compressor 10.
The method for reducing the tar content in the synthesis gas provided by the embodiment of the disclosure comprises the following steps: the synthesis gas I generated by the gasification furnace 1 returns downwards at the top of the gasification furnace 1 and enters the storage tank 18 and enters the synthesis gas outlet cylinder 17 filled with high-temperature circulating materials through the gas guide pipe 115; separating part of carbon-containing return materials in the return materials M of the gasification furnace 1 through a carbon separator 2, and adding the separated carbon-containing return materials into a synthesis gas leading-out cylinder 17; the residual part in the return material M of the gasification furnace 1 is used as a circulating material and sent into a combustion furnace 6 through a first return feeder 5, the circulating material is heated in the combustion furnace 6, the heated circulating material and the flue gas K pass through a combustion furnace cyclone separator 7, and the high-temperature circulating material separated by the combustion furnace cyclone separator 7 enters a synthesis gas extraction cylinder 17 through a second return feeder 8.
The synthetic gas I generated by the gasification furnace returns downwards at the top of the gasification furnace and is discharged after passing through a gasification furnace storage tank 18 filled with high-temperature circulating materials and a synthetic gas leading-out cylinder 17. The carbon in the return material M of the gasification furnace to the combustion furnace is separated, the carbon is also added into the synthesis gas extraction cylinder 17, the other part of the circulating material in the return material M of the gasification furnace 1 is sent into the combustion furnace 6 through the second return feeder 8, the circulating material is heated in the combustion furnace 6, and the heated circulating material enters the synthesis gas extraction cylinder 17. The synthesis gas I can be cracked under the high-temperature environment and the carbon-rich working condition, so that the tar content in the synthesis gas I is greatly reduced.
In some embodiments, the amount of air C in furnace 6 and the amount of fluidized flue gas D in carbon separator 2 are controlled such that the measured temperature of furnace cyclone thermocouple 71 in furnace cyclone 7 is maintained at 950 ℃ to 980 ℃; controlling the material returning amount M of the gasification furnace 1 to the combustion furnace 6 to maintain the temperature measured by a thermocouple of the gasification furnace at 700-800 ℃; when the temperature difference between the upper thermocouple 14 in the synthesis gas leading cylinder 17 and the thermocouple 71 of the cyclone separator of the combustion furnace is within +/-20 ℃, the amount of the returned synthesis gas G in the returned synthesis gas blowing port 111 is increased; when the temperature difference between the upper thermocouple 14 and the lower thermocouple 15 in the syngas extraction cylinder 17 and the gasifier thermocouple 19 is within ± 20 ℃, the amount of the returned syngas G in the returned syngas blow-off port 111 is reduced. The embodiment can maintain the temperature of the high-temperature circulating material at 950-980 ℃; and the synthesis gas leading-out cylinder 17 is controlled to have a proper material level, so that the longer residence time of the synthesis gas is ensured, and the better tar decomposition effect is ensured.
Specifically, the air quantity C of the combustion furnace 6 and the fluidized flue gas quantity D of the carbon separator 2 are controlled, so that the temperature of the combustion furnace is controlled, the measured temperature of a thermocouple 71 of the cyclone separator of the combustion furnace in the cyclone separator 7 of the combustion furnace is maintained at 950-980 ℃, when the fluidized flue gas quantity D of the carbon separator 2 is increased, the carbon entering the combustion furnace 6 is reduced, and when the fluidized flue gas quantity D of the carbon separator 2 is reduced, the carbon entering the combustion furnace 6 is increased; the temperature of the gasification furnace can be controlled by controlling the material return quantity M of the gasification furnace 1 to the combustion furnace 6, the temperature difference between the gasification furnace and the combustion furnace can be reduced by increasing the circulating material quantity of the system, namely, the temperature of the gasification furnace can be increased, and the temperature measured by a thermocouple 19 of the gasification furnace is maintained at 700-800 ℃; when the temperature difference between the upper thermocouple 14 in the synthesis gas leading cylinder 17 and the thermocouple 71 of the cyclone separator of the combustion furnace is within +/-20 ℃, the material level in the synthesis gas leading cylinder 17 is higher, and the gas amount of the returned synthesis gas G in the returned material blowing gas port 111 is increased; when the temperature difference between the upper thermocouple 14 and the lower thermocouple 15 in the synthesis gas extraction cylinder 17 and the gasifier thermocouple 19 is within +/-20 ℃, the material level in the synthesis gas extraction cylinder 17 is low, and the amount of the returned synthesis gas G in the returned material blowing air port 111 is reduced; thereby ensuring that the synthesis gas leading-out cylinder of the gasification furnace has proper material level and longer residence time of the synthesis gas, and ensuring better tar decomposition effect.
Meanwhile, a catalyst having a tar cracking function, such as iron oxide, calcium oxide, or the like, may be added to the synthesis gas extraction cylinder 17 through the catalyst addition port 13.
In this example, the inert bed material may be replaced by a catalyst mainly composed of calcium oxide or iron oxide.
In summary, in the embodiment of the present disclosure, the syngas generated by the gasification furnace 1 is turned back downward at the top of the gasification furnace 1 and passes through the syngas discharge tube 17 filled with the high-temperature circulating material, and at the same time, part of carbon in the returned material of the gasification furnace 1 to the combustion furnace 6 is separated, and the carbon is also added into the syngas discharge tube 17, so that the syngas is cracked under high-temperature environment and carbon-rich working condition, and the tar content in the syngas is greatly reduced.
In the technical scheme of the patent, the temperature of the high-temperature circulating material is controlled to be kept at 950-980 ℃; and the synthesis gas leading-out cylinder 17 is controlled to have a proper material level, so that the longer residence time of the synthesis gas is ensured, and the better tar decomposition effect is ensured.
It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrases "comprising one of 8230; \8230;" 8230; "does not exclude the presence of additional like elements in a process, method, article, or apparatus that comprises the element.
The foregoing are merely exemplary embodiments of the present disclosure, which enable those skilled in the art to understand or practice the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A double-bed system for reducing the tar content in synthesis gas is characterized by comprising a gasification furnace (1), a combustion furnace (6) and a synthesis gas leading-out cylinder (17);
the synthetic gas leading-out barrel (17) comprises a first barrel (171) and a second barrel (172) which are arranged up and down, the first barrel (171) is positioned outside the gasification furnace (1), and the first barrel (171) is provided with a synthetic gas leading-out opening (12);
the second cylinder (172) is positioned in the gasification furnace (1), and a storage tank (18) arranged around the second cylinder (172) is arranged on the outer side of the second cylinder (172);
the second cylinder (172) is provided with a gas guide pipe (115) for communicating the storage tank (18) and the second cylinder (172), so that the synthetic gas generated by the gasification furnace (1) enters the storage tank (18), then enters the second cylinder (172) through the gas guide pipe (115), and is discharged from the synthetic gas outlet (12);
the gasification furnace (1) is provided with a gasification furnace overflow port (114) used for introducing return materials into the combustion furnace (6), the combustion furnace (6) is used for heating the return materials to form high-temperature materials, and the synthesis gas leading-out cylinder (17) is used for receiving the high-temperature materials.
2. The dual bed system for reducing tar content in syngas of claim 1, further comprising a carbon separator (2) and a cyclone separator (3);
the feeding hole of the carbon separator (2) is communicated with the overflow port (114) of the gasification furnace, the first outlet of the carbon separator (2) is communicated with the combustion furnace (6) through a first return feeder (5), the second outlet of the carbon separator (2) is communicated with the cyclone separator (3), and the cyclone separator (3) is communicated with the first cylinder (171) through a third return feeder (4).
3. The dual-bed system for reducing the tar content in the synthesis gas according to claim 2, further comprising a combustion furnace cyclone (7), wherein a feeding port of the combustion furnace cyclone (7) is communicated with the combustion furnace (6), and a discharging port of the combustion furnace cyclone (7) is communicated with the first cylinder (171) through a second return feeder (8) for feeding high-temperature materials formed by the combustion furnace (6) into the first cylinder (171).
4. The dual-bed system for reducing the tar content of synthesis gas according to claim 3, wherein the furnace cyclone (7) is in communication with a first waste heat recovery device (201) and a flue gas purification device (202) in sequence, and the flue gas purification device (202) is in communication with the carbon separator (2) through a flue gas recirculation fan (9).
5. The dual-bed system for reducing the tar content in the synthesis gas according to claim 2, wherein the bottom of the second cylinder (172) is provided with an in-furnace return feeder (110), and the in-furnace return feeder (110) is provided with a return blowing air port (111);
the synthesis gas outlet (12) is communicated with a second waste heat recovery device (203) and a synthesis gas purification device (204) in sequence, and the synthesis gas purification device (204) is connected with a synthesis gas compressor (10) and the returned material blowing air port (111) in sequence.
6. The dual bed system for reducing tar content in syngas according to claim 1, wherein the first cylinder (171) is provided with an upper thermocouple (14) and a lower thermocouple (15), the upper thermocouple (14) and the lower thermocouple (15) being spaced apart in the height direction of the first cylinder (171);
the distance L between the upper thermocouple (14) and the lower thermocouple (15) satisfies the following conditions: l is more than or equal to 500mm and less than or equal to 1000mm.
7. The dual bed system for reducing tar content in syngas according to any one of claims 1-6, characterized in that the gas duct (115) is inclined downwards in the direction from the storage tank (18) to the syngas takeoff drum (17);
the included angle alpha between the air duct (115) and the horizontal direction satisfies the following conditions: alpha is more than or equal to 45 degrees.
8. The dual-bed system for reducing the tar content in the synthesis gas according to claim 7, wherein the number of the gas-guide tubes (115) is provided in plurality, and the gas-guide tubes (115) are uniformly distributed along the circumference of the second cylinder (172).
9. A method of reducing tar content in syngas using the dual bed system for reducing tar content in syngas of any one of claims 1-8, comprising:
the synthesis gas I generated by the gasification furnace (1) returns downwards at the top of the gasification furnace (1) and enters a storage tank (18) and enters a synthesis gas leading-out cylinder (17) filled with high-temperature circulating materials through a gas guide pipe (115);
adding part of carbon-containing return materials in the return materials M of the gasification furnace (1) into a synthesis gas extraction cylinder (17); the residual part in the material return M of the gasification furnace (1) is used as a circulating material and is sent into a combustion furnace (6) through a first material return device (5), the circulating material is heated in the combustion furnace (6), the heated circulating material and the flue gas K pass through a combustion furnace cyclone separator (7), and the high-temperature circulating material separated by the combustion furnace cyclone separator (7) enters a synthesis gas extraction cylinder (17) through a second material return device (8).
10. The method for reducing the tar content of synthesis gas according to claim 9, wherein the amount of air C in the furnace (6) and the amount of fluidized flue gas D in the carbon separator (2) are controlled such that the measured temperature of the furnace cyclone thermocouple (71) in the furnace cyclone (7) is maintained at 950 ℃ to 980 ℃;
controlling the material returning quantity M of the gasification furnace (1) to the combustion furnace (6) to maintain the temperature measured by a thermocouple of the gasification furnace at 700-800 ℃;
when the temperature difference between an upper thermocouple (14) in a synthesis gas extraction cylinder (17) and a cyclone separator thermocouple (71) of a combustion furnace is within +/-20 ℃, increasing the amount of return synthesis gas G in a return blowing gas port (111);
when the temperature difference between the upper thermocouple (14) and the lower thermocouple (15) in the synthesis gas extraction cylinder (17) and the gasifier thermocouple (19) is within +/-20 ℃, the amount of the returned synthesis gas G in the returned synthesis gas blowing port (111) is reduced.
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| US5560900A (en) * | 1994-09-13 | 1996-10-01 | The M. W. Kellogg Company | Transport partial oxidation method |
| CN100445348C (en) * | 2006-02-08 | 2008-12-24 | 福州大学 | Low temperature distillation method and device for high volatile component weak viscosity coal |
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| CN101699187B (en) * | 2009-10-21 | 2012-06-13 | 东南大学 | Coal combustion apparatus capable of separating carbon dioxide and separation method thereof |
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| NL2013957B1 (en) * | 2014-12-11 | 2016-10-11 | Stichting Energieonderzoek Centrum Nederland | Reactor for producing a product gas from a fuel. |
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