CN101955799A - Method for comprehensively using powdered coal to prepare coal tar, coal gas and water vapor - Google Patents
Method for comprehensively using powdered coal to prepare coal tar, coal gas and water vapor Download PDFInfo
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Abstract
The invention relates to a method for comprehensively using powdered coal to prepare coal tar, coal gas and water vapor, which comprises the following steps of: preheating semicoke powder, drying powdered coal, primarily pyrolyzing the powdered coal, secondarily pyrolyzing the powdered coal, heating the semicoke powder, gasifying a part of semicoke powder, and producing water vapor by using a powered coke boiler. In the invention, the powdered coal is prepared into coal tar, coal gas and water vapor, the comprehensive utilization of the powdered coal is realized, energy sources are saved, and production cost is reduced; the fine chemicals of benzene, naphthalene, anthracene and the like can be produced by deeply processing the product coal tar, and the petroleum series products of gasoline, diesel oil, fuel oil and the like can be produced by further hydrogenating coal tar; the product coal gas can be used for producing synthetic ammonia and synthetic methanol and can also be used as clean fuel to be applied to power generation, industrial boilers and civil use; and the by-product ash can be used for producing a building material.
Description
Technical field
The invention belongs to technical field of coal chemical industry, be specifically related to the step method that a kind of fine coal prepares coal tar, coal gas, water vapour.
Background technology
Coal occupies an important position in world's Energy Mix, China's oil, natural gas source are abundant inadequately, but coal resources are comparatively sufficient, therefore in energy consumption structure, coal resources occupy bigger proportion (about 70%) all the time, and can not change in a very long time from now on.
In the last few years, in development Coal Chemical Industry process, coal was carried out multistage comprehensive utilization technique, both at home and abroad as the key that realizes energy sustainable development.Now the main method that coal is carried out multistage utilization is: (1) is the electric Poly-generation technology of basal heat with the pyrolysis of coal; (2) based on the thermoelectric gas Poly-generation technology of coal partial gasification; (3) be gasified totally with coal and be the thermoelectric gas Poly-generation technology on basis.Above-mentioned three kinds of technology, though its characteristics are respectively arranged, special emphasis makes the multistage utilization of coal be subjected to certain restriction for generating.
Summary of the invention
Technical problem to be solved by this invention provides a kind ofly carries out coupling with pyrolysis of coal, partial gasification technology, and the fine coal comprehensive utilization that technological process is simple, efficient is high, energy consumption is low prepares the method for coal tar, coal gas, water vapour.
The technical scheme that solves the problems of the technologies described above employing is made up of following step:
A. preheating semi-coke powder
The hot flue gas that adds thermogenesis with process furnace during running will enter heating riser tube particle diameter less than the heating that circulates of the semi-coke powder of 1mm from heating riser tube bottom, make it reach burning-point, close process furnace, enter from heating riser tube bottom with 8～15 meter per seconds with air and circulating flue gas and continue the heating semi-coke powder, the volume ratio of air and circulating flue gas is 1: 2～3.
B. dry fine coal
Particle diameter enters less than the fine coal of the 1mm lower sides from airflow drying tube, 500～550 ℃ circulating flue gas enters with the flow velocity of 8～15 meter per seconds bottom from airflow drying tube, fine coal to airflow drying tube carries out air stream drying, gas solid separation, flue gas is discharged from the airflow drying tube top, and dried fine coal enters one-level air-flow thermal decomposition tube by pipeline.
C. fine coal one-level pyrolysis
900～950 ℃ of semi-coke powders that the coal gas that feeds flow velocity and be 8～15 meter per seconds will heat riser tube are blown into one-level air-flow thermal decomposition tube, the mass ratio of fine coal and semi-coke powder is 1: 1.5～2.5, pyrolysis temperature is 510～550 ℃, fine coal is converted into semi-coke powder, raw gas, gas solid separation, semi-coke powder enter the secondary air flow thermal decomposition tube.Raw gas is discharged from one-level air-flow thermal decomposition tube top and is entered the raw gas refining plant, in the raw gas refining plant, raw gas is isolated coal tar, coal gas, coal tar is exported through pipeline from the bottom, and a part of coal gas is exported as product gas through interchanger heat exchange to 450～500 ℃ recycle, another part.
D. fine coal secondary pyrolysis
Flow velocity is that 900～950 ℃ of semi-coke powders that the circulating gas of 8～15 meter per seconds will heat riser tube are blown into the secondary air flow thermal decomposition tube, the mass ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 1～2, pyrolysis temperature is 700～750 ℃, the further pyrolysis of semi-coke powder, gas solid separation is raw gas and semi-coke powder, the raw gas that produces is discharged from the top and is entered the raw gas refining plant, isolate coal tar, coal gas, the coal gas that coal gas and one-level pyrolysis produce mixes afterwards a part of coal gas, and to output to the interchanger heat exchange through pipeline be 450～500 ℃ of recycles, another part coal gas is as the output of product gas, and semi-coke powder enters the heating riser tube.
E. semi-coke powder heating
Pyrogenous origin 750～800 ℃ of semi-coke powders of secondary air flow enter the heating riser tube by heating riser tube sidewall, flow velocity is that the air of 8～15 meter per seconds and 500～550 ℃ circulating flue gas enter from the bottom of heating riser tube, the volume ratio of air and flue gas is 1: 2～3, remaining semi-coke powder of semi-coke powder burning heating of 8%～12%, flue gas and semi-coke powder reach 900～950 ℃, gas solid separation, 900～950 ℃ of flue gases are discharged from the top of heating riser tube as circulating flue gas and are entered interchanger, in interchanger with 30～50 ℃ of circulating gas heat exchange, 900～950 ℃ of flue gases are reduced to 500～550 ℃, circulating gas is elevated to 450～500 ℃ by 30～50 ℃, 500～550 ℃ of circulating flue gas enter airflow drying tube, and 450～500 ℃ of circulating gas parts enter one-level air-flow thermal decomposition tube, another part enters the secondary air flow thermal decomposition tube; 900～950 ℃ of semi-coke powder parts enter one-level air-flow thermal decomposition tube and the recycle of secondary air flow thermal decomposition tube, another part entering part vapor lamp respectively as the circulation semi-coke powder.
F. part semi-coke powder gasification
Oxygen and water vapour are 8～15 meter per second entering part vapor lamps with flow velocity, the volume ratio of water vapour and oxygen is 1: 0.5～0.8, semi-coke powder to the entering part vapor lamp promotes, quality is 10%～40% semi-coke powder gasification reaction, the gasification reaction temperature is 950～1000 ℃, obtains water-gas and temperature and be 900～950 ℃ semi-coke powder; Water-gas is discharged from partial gasification pipe top and is entered waste heat boiler through pipeline, waste heat boiler turns to water vapour with the steam that enters, water-gas is discharged from the waste heat boiler top and is mixed the formation mixed gas with the purification coal gas of raw gas refining plant discharge and recycle, and water vapour is discharged from the waste heat boiler side.
G. coke breeze boiler for producing water vapour
900～950 ℃ of semi-coke powders after the gasification enter the coke breeze boiler, bubbling air is combustion-supporting, heating enters the water of coke breeze boiler, produce water vapour and lime-ash, a water vapour part is mixed and fed into the utilization of partial gasification pipe with the water vapour of discharging from waste heat boiler, another part is directly discharged, and lime-ash is discharged from coke breeze boiler bottom.
In preheating semi-coke powder steps A of the present invention, the optimum volume ratio of air and circulating flue gas is 1: 2.5; In fine coal one-level pyrolysis step C, the optimum quality ratio of fine coal and semi-coke powder is 1: 2; In fine coal secondary pyrolysis step D, the optimum quality ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 1.5; In semi-coke powder heating steps E, the optimum volume ratio of air and flue gas is 1: 2.5, and best in quality is remaining semi-coke powder of semi-coke powder burning heating of 10%; In part semi-coke powder gasification step F, the optimum volume ratio of water vapour and oxygen is 1: 0.65, and to the semi-coke powder lifting of entering part vapor lamp, best in quality is 10% semi-coke powder gasification reaction.
The present invention is prepared into coal tar, coal gas, water vapour with fine coal, realized the comprehensive utilization of fine coal, saved the energy, reduced production cost, product coal tar can be produced class fine chemical products such as benzene, naphthalene, anthracene after deep processing, the further hydrogenation of coal tar can be produced gasoline, diesel oil and fuel wet goods petroleum series product; Product coal gas can be used for producing synthetic ammonia and synthesizing methanol, also can be used as clean fuel and is used for generating, Industrial Boiler and civilian; The by product lime-ash can be used for producing material of construction.
Description of drawings
Fig. 1 is the schema that the fine coal comprehensive utilization prepares the method for coal tar, coal gas, water vapour.
Embodiment
The present invention is described in more detail below in conjunction with drawings and Examples, but the invention is not restricted to these embodiment.
The method steps of the fine coal comprehensive utilization preparation coal tar of present embodiment, coal gas, water vapour is as follows:
A. preheating semi-coke powder
The hot flue gas that adds thermogenesis with process furnace 9 during running will enter the semi-coke powder circulation heating of heating riser tube 5 particle diameters less than 1mm from heating riser tube 5 bottoms, make it reach burning-point, close process furnace 9, enter from heating riser tube 5 bottoms with 8～15 meter per seconds with air and circulating flue gas and continue the heating semi-coke powder, the volume ratio of air and circulating flue gas is 1: 2.5.
B. dry fine coal
Particle diameter enters less than the fine coal of the 1mm lower sides from airflow drying tube 1,500～550 ℃ circulating flue gas enters with the flow velocity of 8～15 meter per seconds bottom from airflow drying tube 1, fine coal to airflow drying tube 1 carries out air stream drying, gas solid separation, flue gas is discharged from airflow drying tube 1 top, and dried fine coal enters one-level air-flow thermal decomposition tube 2 by pipeline.
C. fine coal one-level pyrolysis
900～950 ℃ of semi-coke powders that the coal gas that feeds flow velocity and be 8～15 meter per seconds will heat riser tube 5 are blown into one-level air-flow thermal decomposition tube 2, the mass ratio of fine coal and semi-coke powder is 1: 2, pyrolysis temperature is 510～550 ℃, fine coal is converted into semi-coke powder, raw gas, gas solid separation, semi-coke powder enter secondary air flow thermal decomposition tube 4.Raw gas is discharged from one-level air-flow thermal decomposition tube 2 tops and is entered raw gas refining plant 3, in raw gas refining plant 3, raw gas is isolated coal tar, coal gas, coal tar is exported through pipeline from the bottom, and a part of coal gas is exported as product gas through interchanger 10 heat exchange to 450～500 ℃ of recycles, another part.
D. fine coal secondary pyrolysis
Flow velocity is that 900～950 ℃ of semi-coke powders that the circulating gas of 8～15 meter per seconds will heat riser tube 5 are blown into secondary air flow thermal decomposition tube 4, the mass ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 1.5, pyrolysis temperature is 700～750 ℃, the further pyrolysis of semi-coke powder, gas solid separation is raw gas and semi-coke powder, the raw gas that produces is discharged from the top and is entered raw gas refining plant 3, isolate coal tar, coal gas, the coal gas that coal gas and one-level pyrolysis produce mixes afterwards a part of coal gas, and to output to interchanger 10 heat exchange through pipeline be 450～500 ℃ of recycles, another part coal gas is as the output of product gas, and semi-coke powder enters heating riser tube 5.
E. semi-coke powder heating
Pyrogenous origin 750～800 ℃ of semi-coke powders of secondary air flow enter heating riser tube 5 by heating riser tube 5 sidewalls, flow velocity is that the air of 8～15 meter per seconds and 500～550 ℃ circulating flue gas enter from the bottom of heating riser tube 5, the volume ratio of air and flue gas is 1: 2.5, remaining semi-coke powder of semi-coke powder burning heating of 10%, flue gas and semi-coke powder reach 900～950 ℃, gas solid separation, 900～950 ℃ of flue gases are discharged from the top of heating riser tube 5 as circulating flue gas and are entered interchanger 10, in interchanger 10 with 30～50 ℃ of circulating gas heat exchange, 900～950 ℃ of flue gases are reduced to 500～550 ℃, circulating gas is elevated to 450～500 ℃ by 30～50 ℃, 500～550 ℃ of circulating flue gas enter 1,450～500 ℃ of circulating gas parts of airflow drying tube and enter one-level air-flow thermal decomposition tube 2, another part enters secondary air flow thermal decomposition tube 4.900～950 ℃ of semi-coke powder parts enter one-level air-flow thermal decomposition tube 2 and 4 recycles of secondary air flow thermal decomposition tube, another part entering part vapor lamp 7 respectively as the circulation semi-coke powder.
F. part semi-coke powder gasification
Oxygen and water vapour are 8～15 meter per second entering part vapor lamps 7 with flow velocity, the volume ratio of water vapour and oxygen is 1: 0.65, semi-coke powder to entering part vapor lamp 7 promotes, quality is 25% semi-coke powder gasification reaction, the gasification reaction temperature is 950～1000 ℃, obtains water-gas and temperature and be 900～950 ℃ semi-coke powder; Water-gas is discharged from partial gasification pipe 7 tops and is entered waste heat boiler 6 through pipeline, waste heat boiler 6 turns to water vapour with the steam that enters, water-gas is discharged from waste heat boiler 6 tops and is mixed the formation mixed gas with the purification coal gas of raw gas refining plant 3 discharges and recycle, and water vapour is discharged from waste heat boiler 6 sides.
G. coke breeze boiler for producing water vapour
900～950 ℃ of semi-coke powders after the gasification enter coke breeze boiler 8, bubbling air is combustion-supporting, heating enters the water of coke breeze boiler 8, produce water vapour and lime-ash, a water vapour part is mixed and fed into partial gasification pipe 7 with the water vapour of discharging from waste heat boiler 6 and utilizes, another part is directly discharged, and lime-ash is discharged from coke breeze boiler 8 bottoms.
The method steps of the fine coal comprehensive utilization preparation coal tar of present embodiment, coal gas, water vapour is as follows:
In preheating semi-coke powder steps A of the present invention, the volume ratio of air and circulating flue gas is 1: 2, and other step in this step is identical with embodiment 1.In fine coal one-level pyrolysis step 3, the mass ratio of fine coal and semi-coke powder is 1: 1.5, and other step in this step is identical with embodiment 1.In fine coal secondary pyrolysis step D, the mass ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 1, and other step in this step is identical with embodiment 1.In semi-coke powder heating steps E, the volume ratio of air and flue gas is 1: 2, remaining semi-coke powder of semi-coke powder burning heating of 8%, and other step in this step is identical with embodiment 1.In part semi-coke powder gasification step F, the volume ratio of water vapour and oxygen is 1: 0.5, and to the semi-coke powder lifting of entering part vapor lamp 7, quality is 10% semi-coke powder gasification reaction, and other step in this step is identical with embodiment 1.Other step is identical with embodiment 1.Be prepared into coal tar, coal gas, water vapour.
The method steps of the fine coal comprehensive utilization preparation coal tar of present embodiment, coal gas, water vapour is as follows:
In preheating semi-coke powder steps A of the present invention, the volume ratio of air and circulating flue gas is 1: 3, and other step in this step is identical with embodiment 1.In fine coal one-level pyrolysis step C, the mass ratio of fine coal and semi-coke powder is 1: 2.5, and other step in this step is identical with embodiment 1.In fine coal secondary pyrolysis step D, the mass ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 2, and other step in this step is identical with embodiment 1.In semi-coke powder heating steps E, the volume ratio of air and flue gas is 1: 3, remaining semi-coke powder of semi-coke powder burning heating of 12%, and other step in this step is identical with embodiment 1.In part semi-coke powder gasification step F, the volume ratio of water vapour and oxygen is 1: 0.8, and to the semi-coke powder lifting of entering part vapor lamp 7, quality is 40% semi-coke powder gasification reaction, and other step in this step is identical with embodiment 1.Other step is identical with embodiment 1.Be prepared into coal tar, coal gas, water vapour.
Claims (2)
1. fine coal comprehensive utilization prepares the method for coal tar, coal gas, water vapour, it is characterized in that it is made up of following step:
A. preheating semi-coke powder
The hot flue gas that adds thermogenesis with process furnace (9) during running will enter heating riser tube (5) particle diameter less than the heating that circulates of the semi-coke powder of 1mm from heating riser tube (5) bottom, make it reach burning-point, close process furnace (9), enter from heating riser tube (5) bottom with 8～15 meter per seconds with air and circulating flue gas and continue the heating semi-coke powder, the volume ratio of air and circulating flue gas is 1: 2～3;
B. dry fine coal
Particle diameter enters less than the fine coal of the 1mm lower sides from airflow drying tube (1), 500～550 ℃ circulating flue gas enters with the flow velocity of 8～15 meter per seconds bottom from airflow drying tube (1), fine coal to airflow drying tube (1) carries out air stream drying, gas solid separation, flue gas is discharged from airflow drying tube (1) top, and dried fine coal enters one-level air-flow thermal decomposition tube (2) by pipeline;
C. fine coal one-level pyrolysis
900～950 ℃ of semi-coke powders that the coal gas that feeds flow velocity and be 8～15 meter per seconds will heat riser tube (5) are blown into one-level air-flow thermal decomposition tube (2), the mass ratio of fine coal and semi-coke powder is 1: 1.5～2.5, pyrolysis temperature is 510～550 ℃, fine coal is converted into semi-coke powder, raw gas, gas solid separation, semi-coke powder enter secondary air flow thermal decomposition tube (4); Raw gas is discharged from one-level air-flow thermal decomposition tube (2) top and is entered raw gas refining plant (3), in raw gas refining plant (3), raw gas is isolated coal tar, coal gas, coal tar is exported through pipeline from the bottom, and a part of coal gas is exported as product gas through interchanger (10) heat exchange to 450～500 ℃ of recycles, another part;
D. fine coal secondary pyrolysis
Flow velocity is that 900～950 ℃ of semi-coke powders that the circulating gas of 8～15 meter per seconds will heat riser tube (5) are blown into secondary air flow thermal decomposition tube (4), the mass ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 1～2, pyrolysis temperature is 700～750 ℃, the further pyrolysis of semi-coke powder, gas solid separation is raw gas and semi-coke powder, the raw gas that produces is discharged from the top and is entered raw gas refining plant (3), isolate coal tar, coal gas, the coal gas that coal gas and one-level pyrolysis produce mixes afterwards a part of coal gas, and to output to interchanger (10) heat exchange through pipeline be 450～500 ℃ of recycles, another part coal gas is as the output of product gas, and semi-coke powder enters heating riser tube (5);
E. semi-coke powder heating
Pyrogenous origin 750～800 ℃ of semi-coke powders of secondary air flow enter heating riser tube (5) by heating riser tube (5) sidewall, flow velocity is that the air of 8～15 meter per seconds and 500～550 ℃ circulating flue gas enter from the bottom of heating riser tube (5), the volume ratio of air and flue gas is 1: 2～3, quality is remaining semi-coke powder of semi-coke powder burning heating of 8%～12%, flue gas and semi-coke powder reach 900～950 ℃, gas solid separation, 900～950 ℃ of flue gases are discharged from the top of heating riser tube (5) as circulating flue gas and are entered interchanger (10), in interchanger (10) with 30～50 ℃ of circulating gas heat exchange, 900～950 ℃ of flue gases are reduced to 500～550 ℃, circulating gas is elevated to 450～500 ℃ by 30～50 ℃, 500～550 ℃ of circulating flue gas enter airflow drying tube (1), and 450～500 ℃ of circulating gas parts enter one-level air-flow thermal decomposition tube (2), another part enters secondary air flow thermal decomposition tube (4); 900～950 ℃ of semi-coke powder parts enter one-level air-flow thermal decomposition tube (2) and secondary air flow thermal decomposition tube (4) recycle, another part entering part vapor lamp (7) respectively as the circulation semi-coke powder;
F. part semi-coke powder gasification
Oxygen and water vapour are 8～15 meter per second entering part vapor lamps (7) with flow velocity, the volume ratio of water vapour and oxygen is 1: 0.5～0.8, semi-coke powder to entering part vapor lamp (7) promotes, quality is 10%～40% semi-coke powder gasification reaction, the gasification reaction temperature is 950～1000 ℃, obtains water-gas and temperature and be 900～950 ℃ semi-coke powder; Water-gas is discharged from partial gasification pipe (7) top and is entered waste heat boiler (6) through pipeline, waste heat boiler (6) turns to water vapour with the steam that enters, water-gas is discharged from waste heat boiler (6) top and is mixed the formation mixed gas with the purification coal gas of raw gas refining plant (3) discharge and recycle, and water vapour is discharged from waste heat boiler (6) side;
G. coke breeze boiler for producing water vapour
900～950 ℃ of semi-coke powders after the gasification enter coke breeze boiler (8), bubbling air is combustion-supporting, heating enters the water of coke breeze boiler (8), produce water vapour and lime-ash, a water vapour part is mixed and fed into partial gasification pipe (7) utilization with the water vapour of discharging from waste heat boiler (6), another part is directly discharged, and lime-ash is discharged from coke breeze boiler (8) bottom.
2. prepare the method for coal tar, coal gas, water vapour according to the described fine coal comprehensive utilization of claim 1, it is characterized in that: in preheating semi-coke powder steps A, the volume ratio of air and circulating flue gas is 1: 2.5; In fine coal one-level pyrolysis step C, the mass ratio of fine coal and semi-coke powder is 1: 1.2; In fine coal secondary pyrolysis step D, the mass ratio of the semi-coke powder of 510～550 ℃ semi-coke powder and 900～950 ℃ is 1: 2.5; In semi-coke powder heating steps E, the volume ratio of air and flue gas is 1: 2.5, and quality is remaining semi-coke powder of semi-coke powder burning heating of 10%; In part semi-coke powder gasification step F, the volume ratio of water vapour and oxygen is 1: 0.65, and to the semi-coke powder lifting of entering part vapor lamp G, quality is 25% semi-coke powder gasification reaction.
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| CN102250646A (en) * | 2011-05-30 | 2011-11-23 | 王树宽 | Device for preparing coal tar and coal gas by coupling semi-coke powder gasification and reformed gas pyrolysis and method using same |
| CN102433166A (en) * | 2011-10-25 | 2012-05-02 | 陕西华祥能源科技集团有限公司 | Moving bed pulverized coal pyrolysis and fluidized bed coke powder gasification coupled device and coupling method thereof |
| CN102786966A (en) * | 2012-03-08 | 2012-11-21 | 大连理工大学 | Coal solid heat carrier pyrolysis method and system for guide type stripping reinforced oil gas accelerated introduction |
| CN103205283A (en) * | 2013-04-13 | 2013-07-17 | 何巨堂 | Powder dry distillation method using fluidized bed dry distillation chamber and supplementary dry distillation chamber in series |
| CN103305246A (en) * | 2013-06-08 | 2013-09-18 | 华电重工股份有限公司 | Pyrolytic poly-generation method of low-rank coal and system |
| CN105062592A (en) * | 2015-07-31 | 2015-11-18 | 赛鼎工程有限公司 | Comprehensive utilization technology used for production of gasoline and liquefied natural gas through methanol synthesis of crushed coal pressure gasification synthetic gas, and used for tar depth processing |
| CN105602593A (en) * | 2014-11-23 | 2016-05-25 | 陕西煤业化工集团(上海)胜帮化工技术有限公司 | Method for pyrolyzing fine coal by riser |
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Cited By (11)
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| CN102250646A (en) * | 2011-05-30 | 2011-11-23 | 王树宽 | Device for preparing coal tar and coal gas by coupling semi-coke powder gasification and reformed gas pyrolysis and method using same |
| CN102250646B (en) * | 2011-05-30 | 2014-02-05 | 王树宽 | Device for preparing coal tar and coal gas by coupling semi-coke powder gasification and reformed gas pyrolysis and method using same |
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| CN105062592B (en) * | 2015-07-31 | 2017-09-26 | 赛鼎工程有限公司 | Crushed coal pressure gasifying synthesis gas through methanol synthetic gasoline, co-production of liquefied natural gas and the comprehensive utilization process for tar deep processing |
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