CN109652146B - Downer bed-turbulent bubbling bed pyrolysis-gasification integrated method and device - Google Patents
Downer bed-turbulent bubbling bed pyrolysis-gasification integrated method and device Download PDFInfo
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- CN109652146B CN109652146B CN201710946678.2A CN201710946678A CN109652146B CN 109652146 B CN109652146 B CN 109652146B CN 201710946678 A CN201710946678 A CN 201710946678A CN 109652146 B CN109652146 B CN 109652146B
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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
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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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
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
- C10J3/487—Swirling or cyclonic gasifiers
Abstract
The invention relates to a downer-turbulent bubbling bed pyrolysis-gasification integrated method and device, and mainly solves the problems that in the prior art, tar yield is low, low-rank coal is difficult to utilize and the like. The invention adopts the combination of the downer pyrolysis furnace and the turbulent bubbling bed gasification furnace, and comprises the following steps: raw materials are added into the upper part of the downer pyrolysis furnace and are heated by gasification product gas from the turbulent bubbling bed gasification furnace to generate pyrolysis gas and coal coke; through separation and rapid cooling, condensable gas is cooled into tar, non-condensable gas is further purified to finally obtain product synthetic gas, coal coke is sent into a turbulent bubbling bed gasification furnace and is contacted with a catalyst and a gasification agent to carry out gasification reaction to generate gasification product gas and gasification residues, and high-temperature gasification product gas is sent into a downer pyrolysis furnace to be used as a heat source required by pyrolysis, so that the energy consumption of the whole circulation system is effectively reduced, and the method can be used in the technical field of coal chemical industry.
Description
Technical Field
The invention belongs to the technical field of coal pyrolysis-gasification grading utilization. In particular to a method for realizing the co-production of tar and methane-rich synthesis gas by using low-rank coal through gasification-pyrolysis integration.
Background
China is a country which takes coal as a main energy structure and cannot change for a long time in the future, and according to statistics, coal reaches 66% in the primary energy consumption structure of China. With the increasing shortage of petroleum resources, the effective utilization of coal resources has become a strategy for sustainable development of energy in China. The reserve of low-rank coal in China accounts for more than 55% of the total amount of coal resources, but the low-rank coal has high water content, low coalification degree and low direct combustion efficiency, thereby not only wasting resources, but also polluting the environment and causing the emission of acid rain, PM2.5, SOx, NOx and other greenhouse gases.
At present, the low-rank coal has 75-90% of carbon content and 10-40% of volatile matters. The relative density is 1.25-1.35, and the heat value is about 27170-. The classification utilization of low-rank coal is one of important methods for clean and efficient utilization of the low-rank coal. According to the composition and structural characteristics of the low-rank coal, a certain successful experience is obtained by organically combining pyrolysis, combustion, gasification and other processes of the low-rank coal, organic matter volatile components and fixed carbon in the coal are effectively separated by utilizing the low-rank coal in a grading manner, and coal tar, coal gas and chemicals with high added values are obtained. The low-rank coal grading utilization technology mainly comprises low-rank coal quality improvement, pyrolysis gasification grading conversion, pyrolysis combustion grading conversion and the like, but the processes of quality improvement and coal coke reconversion need to be carried out in different reaction equipment, the coupling of material flow and heat flow cannot be carried out, and the energy consumption is large.
In order to solve the problems, the Chinese patent CN102504842A takes high-temperature circulating ash as a solid heat carrier and three fluidized beds of pyrolysis, combustion and gasification as core devices according to the characteristic that different components in coal have different reactivities in different conversion stages, and aims to improve the conversion rate and the utilization efficiency of the coal. However, the process has the following defects: firstly, the particle size of high-temperature circulating ash is very small, so that the problem of high dust content of pyrolysis gas exists; secondly, high-temperature circulating ash is adopted as a heat carrier, the heat value of the ash is low, the density is small, and the heat transfer efficiency is not high. The university of Tokyo (Chemical Engineering Journal,164(2010) 221-229; Chemical Engineering Science,66(2011)4212-4220) of Japan proposes a gasification pyrolysis graded utilization process, realizes the precise control of pyrolysis time, simultaneously realizes the separation of pyrolysis gas-solid products in front of a gasification furnace, avoids the inhibiting effect of volatile components on the gasification of the semicoke to prepare synthesis gas, but the process adopts quartz sand as a heat-carrying substance, which causes the serious abrasion of equipment. The Chinese patent CN104789245A adopts a three-tower high-flux semicoke circulating fluidized bed process, and takes high-temperature circulating semicoke particles as a heat carrier, thereby improving the heat transfer efficiency and simultaneously realizing the effective separation of gas-solid products.
Although the existing pyrolysis-gasification integrated technology solves the defect that the traditional coal conversion technology cannot effectively and cleanly utilize low-rank coal to a certain extent, the problems of overlarge energy consumption, equipment damage, low carbon conversion rate and the like occur due to the limitation of the process flow or the addition of a heat carrier. Therefore, how to reasonably improve the heat transfer efficiency and further improve the tar yield is the development key of the methane-rich synthesis gas-tar co-production technology for realizing pyrolysis-gasification graded utilization in the real sense.
Disclosure of Invention
One of the technical problems solved by the invention is to overcome the defects of difficult utilization of low-rank coal and low tar yield in the prior art, provide a descending bed-turbulent bubbling bed pyrolysis-gasification integrated device suitable for high-efficiency utilization of low-rank coal, effectively improve the heat transfer efficiency and realize the characteristic of diversified gasification products.
The second technical problem to be solved by the invention is a downer bed-turbulent bubbling bed pyrolysis-gasification integrated method corresponding to the first technical problem.
In order to solve the technical problem, the invention provides a downer bed-turbulent bubbling bed pyrolysis-gasification integrated device, which is characterized in that: comprises a downer pyrolysis furnace 1, a gas-solid separator 2, a condensing device 3, a turbulent bubbling bed gasification furnace 5 and a slag hopper 6; the top of the downer pyrolysis furnace 1 is provided with an inlet of a raw material A, the middle upper part of the downer pyrolysis furnace 1 is provided with an inlet of a gasification product gas B, the bottom of the downer pyrolysis furnace 1 is connected with a gas-solid separator 2, a gas outlet at the top of the gas-solid separator 2 is connected with a condensing device 3, a solid outlet at the bottom of the gas-solid separator 2 is connected with a pyrolysis semicoke storage bin 4, the bottom of the pyrolysis semicoke storage bin 4 is connected with a turbulent bubbling bed gasification furnace 5, the middle upper part of the turbulent bubbling bed gasification furnace 5 is provided with a gasification product gas (B) outlet, the middle lower part of the turbulent bubbling bed gasification furnace is provided with a catalyst F inlet, the lateral lower part of the turbulent.
In the technical scheme, the gasification product gas (B) inlet is arranged at the position of the downer pyrolysis furnace (1) from 1/30-1/5 of the top of the furnace. .
Preferably, the downer pyrolysis furnace 1 is provided with an inlet for the gasified product gas B at a distance from the furnace top 1/20-1/15.
In the technical scheme, the condensing device (3) adopts a direct contact condenser, and is selected from one of a spray type condenser, a jet type condenser or a plate-type condenser.
In the technical scheme, the turbulent bubbling bed gasification furnace 5 adopts the design of reducing the pipe diameter of the upper layer and the lower layer, and the inner diameter of the upper layer space is larger than that of the lower layer space and is between 1.2 times and 1.5 times of that of the lower layer space; the height of the upper layer space is equal to that of the lower layer space.
In the technical scheme, the position of the turbulent bubbling bed gasification furnace (5) from 1/20 to 1/5 of the top of the furnace is provided with an outlet of a gasification product gas (B), and the top of the turbulent bubbling bed gasification furnace (5) is connected with a pyrolysis semicoke storage bin (4).
In the technical scheme, inlets of gasifying agents (G) are arranged at positions, away from 1/20-1/10, of the turbulent bubbling bed (5), and inlets of catalysts (F) are arranged at positions, away from 1/5-1/4, of the turbulent bubbling bed (5).
In order to solve the second technical problem, the invention provides a downer turbulent bubbling bed pyrolysis-gasification integrated method which is characterized by comprising the following steps of:
a. reaction in the downer pyrolysis furnace 1: the raw material A is added from the top of the downer pyrolysis furnace 1 and is mixed with CH-containing gas from the turbulent bubbling bed gasification furnace 54、CO、H2The high-temperature gasification product gas B of the reducing gas is contacted and rapidly heated to realize rapid pyrolysis, and volatile matters are separated out to generate pyrolysis semicoke C; the pyrolysis semicoke C is carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis and enters the gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, wherein condensable gas becomes tar E after being cooled, and is discharged from the bottom of the condensing device 3 and collected, while non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified, and finally, a product synthetic gas D is obtained; the pyrolysis semicoke C is used as a gasification raw material of the turbulent bubbling bed gasification furnace 5 to continue to react;
b. reaction in the turbulent bubbling bed gasifier 6: the pyrolysis semicoke C in the pyrolysis semicoke storage bin 4 is conveyed by gas to enter the turbulent bubbling bed gasification furnace 5, contacts with a catalyst F input from the middle part of the turbulent bubbling bed gasification furnace 5 and a gasification agent G input from a gas inlet at the lower side part in the turbulent bubbling bed gasification furnace 5, and generates a violent catalytic gasification reaction to generate gasification product gas B and gasification residues; the gasification residue falls into the slag hopper 6 by gravity and is collected.
The raw material A is low-grade coal, the catalyst F is at least one of cheap papermaking black liquor, industrial waste alkali or plant ash, and the mass ratio of the raw material A to the catalyst F is 100: (5-10), the particle sizes of the raw material A and the catalyst F are both less than 1 mm.
The downer pyrolysis furnace 1 adopts a flash pyrolysis technology, and the linear speed in the furnace is 20-30 m/s. Preferably, the linear speed in the downer pyrolysis furnace 1 is 25 to 28 m/s.
The linear speed of the lower layer space of the turbulent bubbling bed gasification furnace 5 is 0.70-0.90m/s, and the linear speed of the corresponding upper layer space is 0.30-0.6 m/s.
Brief description of the invention
The invention couples gasification and pyrolysis into a whole, carries out pyrolysis in the downer pyrolysis furnace, carries out gasification reaction of pyrolysis semicoke particles in the turbulent bubbling bed gasification furnace, and circularly enters the pyrolysis furnace as a heat source for pyrolysis by taking gasified product gas as a heat source and a pyrolysis medium required by pyrolysis, thereby reducing the energy consumption of the whole circulating system and saving the cost of an external heat carrier in the traditional process. The catalyst of the system adopts cheap industrial waste, and the carbon conversion rate (95%) is improved and the current situation that low-grade inferior coal is difficult to utilize is solved through reasonable proportioning of the catalyst and raw materials.
By adopting the technical scheme of the invention, through the integrated arrangement of gasification and pyrolysis, under the processes of high linear speed of the pyrolysis furnace, short stay of particles and quick cooling of product gas, and in the structure with variable diameters of the upper layer structure and the lower layer structure of the turbulent bubbling bed gasification furnace, the gas stay time is prolonged, and the co-production of methane-rich synthesis gas and tar is realized. The yield of tar in the product can reach 36 percent, and CH in the gas product4The content of the carbon dioxide reaches 15 percent, and the carbon dioxide has high gasification strength and energy utilizationHigh efficiency, low pollution and the like, greatly reduces the production cost and has good application prospect.
Drawings
Fig. 1 is a schematic view of a downer bed-turbulent bubbling bed pyrolysis-gasification integrated apparatus provided by the present invention.
In the figure, 1-a downer pyrolysis furnace; 2-gas-solid separator; 3-a condensing unit; 4-pyrolysis semicoke storage; 5-turbulent bubbling bed gasification furnace; 6-a slag hopper; a-raw materials; b-gasifying the product gas; c-pyrolysis semicoke; d-synthesis gas; e-tar; f-catalyst; g-gasifying agent.
The raw materials are conveyed into a hearth of the downer pyrolysis furnace 1 from a raw material inlet A above the downer pyrolysis furnace through feeding equipment, and are in contact with the gasified product gas B to perform pyrolysis reaction, and the pyrolyzed semicoke C is carried by mixed gas formed by the gasified product gas B and pyrolyzed gas generated by pyrolysis and enters a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, wherein condensable gas becomes tar E after cooling, while non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthetic gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, and is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with a catalyst F and a gasification agent G to form a large amount of synthesis gas and gasification residues. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 to be used as a heat source and a pyrolysis medium required by pyrolysis.
Detailed Description
The features of the invention will be described in more detail below with reference to the accompanying drawings and examples.
[ example 1 ]
Lignite is conveyed into a hearth of the downer pyrolysis furnace 1 from a raw material inlet A above the downer pyrolysis furnace through feeding equipment, gasification product gas B is introduced from a single-pipe jet distributor at a position 1/5 away from the top of the downer pyrolysis furnace 1, contacts and flows with lignite raw materials in parallel, pyrolysis reaction is carried out at the operating temperature of normal pressure and 650 ℃ at the linear speed of 30m/s, and pyrolysis semicoke C is gasifiedThe mixed gas composed of the product gas B and pyrolysis gas generated by pyrolysis is carried and enters a gas-solid separator 2 through the bottom of a downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 16 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from a position 1/5 away from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet 1/20 away from the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.2 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 850 ℃, the linear speed of the lower layer space is 0.9m/s, and the linear speed of the corresponding upper layer space is 0.6 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/5 from the top of the fixed-bed gasification furnace 5 as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 95 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 38.7%, 21.9%, and 12.0%, respectively, and the results are shown in Table 1.
[ example 2 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/5 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 650 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, and the condensing device 3 adoptsThe condensable gas in the tower plate type condenser is cooled to form tar E, and the tar yield reaches 16%. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from a position 1/5 away from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet 1/20 away from the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 850 ℃, the linear speed of the lower layer space is 0.9m/s, and the linear speed of the corresponding upper layer space is 0.4 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/5 from the top of the fixed-bed gasification furnace 5 as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 95 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 35.0%, 20.9%, and 14.5%, respectively, and the results are shown in Table 1.
[ example 3 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/5 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 650 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 18 percent. The non-condensable gas is discharged from the gas outlet at the middle upper part of the condensing device 3 and is further purifiedFinally obtaining a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from a position 1/5 away from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet 1/20 away from the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.2 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 850 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.5 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/5 from the top of the fixed-bed gasification furnace 5 as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 94 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 37.0%, 21.5% and 13.3%, respectively, and the results are shown in Table 1.
[ example 4 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/5 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 650 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 18 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, and is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is thrown from a position 1/5 away from the bottom of the turbulent bubbling bed gasification furnace 5The catalytic gasification reaction is carried out on the papermaking black liquor (the ratio of the substance to the lignite is 10:100) as the catalyst and the gasifying agent G (oxygen and water vapor) entering from the gas inlet at the bottom 1/20 of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthetic gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 850 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/5 which is arranged at the top of the fixed bed gasification furnace 5 to be used as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 94 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 36.2%, 20.6%, and 14.5%, respectively, and the results are detailed in Table 1.
[ example 5 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/30 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 500 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 28 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, and is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from a position 1/5 away from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet at a position 1/20 away from the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthetic semicokeGas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 700 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/20 which is arranged at the top of the fixed bed gasification furnace 5 to be used as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 92 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 35.7%, 21.2%, and 16.1%, respectively, and the results are detailed in Table 1.
[ example 6 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/30 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 500 ℃ at a linear speed of 20m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 26 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from a position 1/5 away from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet 1/20 away from the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 700 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. Gasification ofThe residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is fed into the downer pyrolysis furnace 1 through a gas outlet 1/20 from the top of the fixed-bed gasification furnace 5 as a heat source and a pyrolysis medium required for pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 92 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 35.2%, 21.3%, and 16.0%, respectively, and the results are shown in Table 1.
[ example 7 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/15 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 500 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 30 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from 1/5 which is far from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet which is far from 1/20 of the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 700 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/20 at the top of the fixed bed gasification furnace 5 to be used as a heat source and heat required by pyrolysisAnd (5) decomposing the medium. The carbon conversion rate of the whole circulation reaction system reaches 92 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 34.6%, 20.6%, and 15.0%, respectively, and the results are detailed in Table 1.
[ example 8 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/15 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 500 ℃ at a linear speed of 25m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 33 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from 1/5 which is far from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet which is far from 1/20 of the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 700 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/20 which is arranged at the top of the fixed bed gasification furnace 5 to be used as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 92 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents are 34.9%, 20.7% and 15.0%, respectively, and the results are detailed inTable 1.
[ example 9 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/15 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 500 ℃ at a linear speed of 25m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a spray condenser, the condensable gas becomes tar E after being cooled, and the tar yield reaches 34 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from 1/5 which is far from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet which is far from 1/10 of the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 700 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/20 which is arranged at the top of the fixed bed gasification furnace 5 to be used as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 92 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 34.3%, 20.4%, and 15.1%, respectively, and the results are detailed in Table 1.
[ example 10 ]
Lignite is conveyed into a hearth of the downer pyrolysis furnace 1 from a raw material inlet A above the downer pyrolysis furnace through feeding equipment, and product gas is gasifiedB is introduced from a single-tube jet type distributor at the position 1/15 away from the top of the downer pyrolysis furnace 1, contacts and flows with the lignite raw material in a parallel way, and carries out pyrolysis reaction at the operating temperature of 500 ℃ at the linear speed of 25m/s under normal pressure, and the pyrolysis semicoke C is carried by mixed gas consisting of gasification product gas B and pyrolysis gas generated by pyrolysis and enters a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a spray condenser, the condensable gas becomes tar E after being cooled, and the tar yield reaches 36 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from 1/4 which is far from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet which is far from 1/10 of the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.5 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 700 ℃, the linear speed of the lower layer space is 0.7m/s, and the linear speed of the corresponding upper layer space is 0.3 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/20 which is arranged at the top of the fixed bed gasification furnace 5 to be used as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 92 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 33.1%, 21.1%, and 15.2%, respectively, and the results are detailed in Table 1. [ COMPARATIVE EXAMPLE 1 ]
Adopts a traditional Lurgi furnace pressurization fixed bed gasification device, the raw material adopts brown coal with the grain diameter of 5-30mm, the gasification temperature is 850 ℃, and the linear speed is high<0.3m/s, CO + H in the exit gas component2The content was 61.0% and the methane content was 8.3%, and although gasification also yielded a certain amount of tar product, the yield was only 11% and the carbon conversion was only 90%, the results are detailed in table 1.
[ COMPARATIVE EXAMPLE 2 ]
Adopting a new Olympic group PDU gasification reaction device, adopting lignite as a raw material, adding 10 percent potassium carbonate as a catalyst, and adopting a linear speed<10m/s, operation temperature 800 ℃, CO + H in outlet gas component obtained by gasification256% content, 14% methane content, but with a carbon conversion of 90% and no tar product formation, the results are detailed in table 1.
[ COMPARATIVE EXAMPLE 3 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/5 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 650 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 11 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into the turbulent bubbling bed gasification furnace 5 through gas, and is subjected to gasification reaction with a gasification agent G (oxygen and water vapor) entering from a gas inlet at 1/20 position from the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.2 times of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 850 ℃, the linear speed of the lower layer space is 0.9m/s, and the linear speed of the corresponding upper layer space is 0.6 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/5 from the top of the fixed-bed gasification furnace 5 as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 91 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 37.9%, 20.1%, and 4.7%, respectively, and the results are shown in Table 1.
[ COMPARATIVE EXAMPLE 4 ]
Conveying lignite into a hearth from a raw material inlet A above a downer pyrolysis furnace 1 through feeding equipment, introducing a gasification product gas B from a single-tube jet distributor at a position 1/5 away from the top of the downer pyrolysis furnace 1, contacting and co-flowing with the lignite raw material, performing pyrolysis reaction at an operating temperature of 650 ℃ at a linear speed of 30m/s under normal pressure, and allowing pyrolysis semicoke C to be carried by mixed gas consisting of the gasification product gas B and pyrolysis gas generated by pyrolysis to enter a gas-solid separator 2 through the bottom of the downer pyrolysis furnace 1; after gas-solid separation, the mixed gas is sent to a condensing device 3 for rapid cooling, the condensing device 3 adopts a tower plate type condenser, the condensable gas becomes tar E after being cooled, and the yield of the tar reaches 12 percent. The non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device 3 and is further purified to finally obtain a product synthesis gas D; the pyrolysis semicoke C is separated and then sent into a pyrolysis semicoke storage bin 4, is conveyed into a turbulent bubbling bed gasification furnace 5 through gas, and is subjected to catalytic gasification reaction with catalyst papermaking black liquor (the proportion of the substance to lignite is 10:100) fed from 1/4 which is far from the bottom of the turbulent bubbling bed gasification furnace 5 and gasification agent G (oxygen and water vapor) fed from a gas inlet which is far from 1/10 of the bottom of the turbulent bubbling bed gasification furnace 5 to form a large amount of synthesis gas and gasification residues. The inner diameter of the upper layer space of the gasification furnace is 1.0 time of the inner diameter of the lower layer space. The operation temperature of the gasification furnace is 850 ℃, and the linear speed is 0.6 m/s. The gasification residue falls into the slag hopper 6 by gravity and is collected, and the high-temperature gasification product gas B is sent into the downer pyrolysis furnace 1 through a gas outlet 1/5 from the top of the fixed-bed gasification furnace 5 as a heat source and a pyrolysis medium required by pyrolysis. The carbon conversion rate of the whole circulation reaction system reaches 95 percent, and the effective component H in the synthesis gas D is finally obtained2CO and CH4The contents were 38.1%, 19.8%, 5.3%, respectively, and the results are detailed in Table 1.
TABLE 1
Claims (6)
1. The utility model provides a downing bed-turbulent bubbling bed pyrolysis-gasification integrated device which characterized in that: comprises a downer pyrolysis furnace (1), a gas-solid separator (2), a condensing device (3), a turbulent bubbling bed gasification furnace (5) and a slag hopper (6); the top of the downer pyrolysis furnace (1) is provided with an inlet of a raw material (A), the middle upper part of the downer pyrolysis furnace (1) is provided with an inlet of gasified product gas (B), the bottom of the downer pyrolysis furnace (1) is connected with a gas-solid separator (2), a gas outlet at the top of the gas-solid separator (2) is connected with a condensing device (3), a solid outlet at the bottom of the gas-solid separator (2) is connected with a pyrolysis semicoke storage bin (4), the bottom of the pyrolysis semicoke storage bin (4) is connected with a turbulent bubbling bed gasification furnace (5), a gasified product gas (B) outlet is arranged at a position, away from the top 1/20-1/5, of the turbulent bubbling bed gasification furnace (5), the middle lower part of the turbulent bubbling bed gasification furnace is provided with a catalyst (F) inlet, the lateral lower part of the turbulent bubbling bed gasification furnace (5) is;
wherein, the turbulent bubbling bed gasification furnace (5) adopts the design of reducing the pipe diameter of the upper layer and the lower layer, and the inner diameter of the upper layer space is larger than that of the lower layer space and is between 1.2 times and 1.5 times of the inner diameter of the lower layer space; the height of the upper layer space is equal to that of the lower layer space;
inlets of gasifying agents (G) are arranged at positions from 1/20 to 1/10 of the turbulent bubbling bed gasification furnace (5) to the bottom of the furnace, and inlets of catalysts (F) are arranged at positions from 1/5 to 1/4 of the turbulent bubbling bed gasification furnace (5) to the bottom of the furnace;
the raw material (A) is low-rank coal, the catalyst (F) is at least one of cheap papermaking black liquor, industrial waste alkali or plant ash, and the mass ratio of the raw material (A) to the catalyst (F) is 100: (5-10);
the linear speed of the lower layer space of the turbulent bubbling bed gasification furnace (5) is 0.70-0.90m/s, and the linear speed of the corresponding upper layer space is 0.30-0.55 m/s; the downer pyrolysis furnace (1) adopts a flash pyrolysis technology, and the linear speed in the furnace is 20-30 m/s.
2. The downer-turbulent bubbling bed pyrolysis-gasification integrated apparatus of claim 1, wherein: the downer pyrolysis furnace (1) is provided with gasification product gas (B) inlets at positions 1/30-1/5 away from the top of the furnace.
3. The downer-turbulent bubbling bed pyrolysis-gasification integrated apparatus of claim 1, wherein: the condensing device (3) adopts a direct contact condenser, and is selected from one of a spray type condenser, a jet type condenser or a plate type condenser.
4. The downer-turbulent bubbling bed pyrolysis-gasification integrated apparatus of claim 1, wherein: the top of the turbulent bubbling bed gasification furnace (5) is connected with a pyrolysis semicoke storage bin (4).
5. A downer-turbulent bubbling bed pyrolysis-gasification integrated method, which adopts a downer-turbulent bubbling bed pyrolysis-gasification integrated device as claimed in any one of claims 1 to 4, and is characterized by comprising the following steps:
a. reaction in the downer pyrolysis furnace (1): the raw material (A) is added from the top of the downer pyrolysis furnace (1) and is mixed with CH-containing gas from the turbulent bubbling bed gasification furnace (5)4、CO、H2The high-temperature gasification product gas (B) of the reducing gas is contacted and rapidly heated to realize rapid pyrolysis, and volatile matters are separated out to generate pyrolysis semicoke (C); the pyrolysis semicoke (C) is carried by mixed gas consisting of the gasification product gas (B) and pyrolysis gas generated by pyrolysis and enters the gas-solid separator (2) through the bottom of the downer pyrolysis furnace (1); after gas-solid separation, the mixed gas is sent to a condensing device (3) for rapid cooling, wherein condensable gas becomes tar (E) after being cooled, and is discharged from the bottom of the condensing device (3) and collected, while non-condensable gas is discharged from a gas outlet at the middle upper part of the condensing device (3), and is further purified, and finally, the product synthetic gas (D) is obtained) (ii) a The pyrolysis semicoke (C) is used as a gasification raw material of the turbulent bubbling bed gasification furnace (5) to continue to react;
b. reaction in the turbulent bubbling bed gasifier (5): the pyrolysis semicoke (C) in the pyrolysis semicoke storage bin (4) is conveyed to a turbulent bubbling bed gasification furnace (5) through gas, contacts with a catalyst (F) entering from a catalyst inlet and a gasification agent (G) entering from a gasification agent inlet, and generates a violent catalytic gasification reaction to generate gasification product gas (B) and gasification residues; the gasification residue falls into a slag hopper (6) due to the action of gravity and is collected.
6. The downer-turbulent bubbling bed pyrolysis-gasification integrated process of claim 5, wherein: the temperature of the turbulent bubbling gasification furnace (5) is 700-850 ℃; the temperature of the downer pyrolysis furnace (1) is 500-650 ℃.
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