CN110591745B - Pyrolysis-gasification integrated device and process - Google Patents
Pyrolysis-gasification integrated device and process Download PDFInfo
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- CN110591745B CN110591745B CN201910974441.4A CN201910974441A CN110591745B CN 110591745 B CN110591745 B CN 110591745B CN 201910974441 A CN201910974441 A CN 201910974441A CN 110591745 B CN110591745 B CN 110591745B
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- 238000002309 gasification Methods 0.000 title claims abstract description 186
- 238000000034 method Methods 0.000 title claims abstract description 51
- 230000008569 process Effects 0.000 title claims abstract description 49
- 238000000197 pyrolysis Methods 0.000 claims abstract description 123
- 239000003245 coal Substances 0.000 claims abstract description 52
- 238000004821 distillation Methods 0.000 claims abstract description 22
- 238000009833 condensation Methods 0.000 claims abstract description 19
- 230000005494 condensation Effects 0.000 claims abstract description 19
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 12
- 230000023556 desulfurization Effects 0.000 claims abstract description 12
- 239000003034 coal gas Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 77
- 239000002893 slag Substances 0.000 claims description 31
- 238000001816 cooling Methods 0.000 claims description 29
- 239000011449 brick Substances 0.000 claims description 16
- 239000003795 chemical substances by application Substances 0.000 claims description 15
- 239000000428 dust Substances 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 10
- 238000005507 spraying Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 2
- 230000010354 integration Effects 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000006227 byproduct Substances 0.000 abstract description 2
- 239000011269 tar Substances 0.000 description 33
- 239000002994 raw material Substances 0.000 description 15
- 239000002918 waste heat Substances 0.000 description 14
- 239000002956 ash Substances 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 13
- 239000002028 Biomass Substances 0.000 description 11
- 239000003921 oil Substances 0.000 description 7
- 238000003860 storage Methods 0.000 description 6
- 238000003763 carbonization Methods 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000002802 bituminous coal Substances 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000004480 active ingredient Substances 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- 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
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
-
- 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
-
- 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
- C10J3/50—Fuel charging devices
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0966—Hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
Abstract
A pyrolysis-gasification integrated device and process comprises a pyrolysis furnace gasifier which is communicated, wherein a semicoke distributor with a transverse tube for condensation is arranged between the pyrolysis furnace and the gasifier; the top end of the pyrolysis furnace is provided with a feed inlet, and one side of the feed inlet is provided with a pyrolysis furnace gas outlet; the gas outlet of the pyrolysis furnace is connected with the cyclone separator; the top outlet of the cyclone separator is connected with the distillation tower through an indirect constant cooler; the gasification furnace is provided with a gasification gas outlet which is connected with the desulfurization device; the gasification furnace is provided with a gasification nozzle communicated with the inside of the gasification furnace. The invention realizes the functions of pyrolysis at the upper part and gasification at the lower part in one furnace body. The pyrolysis furnace and the gasification furnace can be fed simultaneously, and under the high-temperature and high-pressure operation condition, the pyrolysis and gasification efficiency is improved, the unit gas production capacity of the equipment is greatly enhanced, and the quality of coal gas and gasification gas is improved. The invention adopts high-temperature pressurizing operation conditions, and has high heat efficiency; the granularity of the fed pulverized coal is small, the gasification reaction is fully carried out, and the byproducts are few.
Description
Technical Field
The invention relates to a pyrolysis-gasification integrated device and a pyrolysis-gasification integrated process, and belongs to the technical field of coal gasification.
Background
The energy occurrence state of 'oil deficiency, gas deficiency and relative coal enrichment' in China determines that coal has an irreplaceable position in the economic development of China. The development of coal chemical industry, in particular to coal pyrolysis and coal gasification technology, is a foundation for deep processing and utilization of coal, has the characteristics of high efficiency, environmental protection and the like, and is widely focused on the research of the coal pyrolysis and coal gasification technology in China.
Along with the continuous and deep research on the coal pyrolysis and coal gasification technologies, technologies of pyrolysis coking, gasification, liquefaction and the like of coal are widely reported according to the composition and structural characteristics of the coal, but the technologies of pyrolysis and gasification of coal by taking inferior coal as raw material have the disadvantages of long process flow, multiple devices, high energy consumption, complex operation and the like, and the reserves of low-rank coal in China are large.
In the existing coal pyrolysis technology, the carbonization of ash-fused pulverized coal can increase the combustion amount of generated semicoke, and the equipment size of a combustion unit is required to be larger, so that the equipment investment is increased; the pulverized coal pyrolysis technology which takes high-temperature water gas as a fluidization medium and a heat carrier of pyrolysis raw materials has higher requirements on the material of a gas compressor and stable long-period operation under a high-severity environment, and severely restricts the development of the technology; the pyrolysis technology using the circulating fluidized bed combustion as the basis and the high-temperature circulating ash as the heat carrier has the problems of high dust content of pyrolysis gas, easy pipeline blockage, difficult utilization of dust-containing tar and the like, and the high-temperature circulating ash as the heat carrier has low ash heat value, low density and low heat transfer efficiency. The coal gasification technology mainly comprises a coal water slurry gasification technology and a pulverized coal gasification technology, wherein the pulverized coal gasification technology is widely applied, a gasification furnace is mostly a chilling operation flow, high-temperature sensible heat generated in the production process is difficult to effectively utilize, waste of heat energy is caused, and carbon content of fly ash carried by coal gas generated in the production process is high, so that energy is wasted.
The invention provides a pulverized coal carbonization device and a pulverized coal carbonization method, which are provided by Chinese patent No. CN 108893130A, the invention has no smoke emission, and the generated gas of coke gasification can further synthesize methanol and light oil products, but the products have tar and gas which are difficult to use, and the quality of the generated oil products is difficult to control and the yield is not high.
The invention discloses a coal pyrolysis gasification poly-generation device and a process based on a circulating fluidized bed, which aim to solve the problems that a pipeline and dust tar are blocked by pyrolysis dust coal gas by taking a moving bed gasifier as a purifying device of pyrolysis dust coal gas, but a moving bed pyrolyzer and a gasification furnace adopted by the process cannot realize rapid pyrolysis of coal, the quality of tar is difficult to effectively control, and the pyrolysis gasification efficiency is low.
The invention provides a pyrolysis gasification device and a pyrolysis gasification process, which are provided by Chinese patent CN 104789245A, wherein three main reactors of an up-bed oxidation burner, a down-bed fast pyrolyzer and a bubbling bed gasifier are connected through high-temperature circulating semicoke, so that the organic coupling of the reaction process is realized, but the defects of low heat transfer efficiency, small treatment capacity, complex process and the like still exist.
The invention provides a coal and biomass mixed gas making system and a gas making method thereof, wherein the coal gasification and biomass pyrolysis are realized in the same furnace body, particularly coal gasification is realized in a gasification reaction zone at the lower part of the furnace body, biomass pyrolysis is realized in a pyrolysis zone at the upper part of the furnace body, the device greatly simplifies the process flow, avoids low heat transfer efficiency caused by high-temperature ash and pyrolysis coke, and is beneficial to the pyrolysis and gasification process of reactants, but the gas reaction furnace has lower operating temperature/pressure and smaller production capacity, and the pipeline design of the pyrolysis zone at the upper part of the reaction furnace is easily blocked due to the influence of the property of biomass raw materials, so that the stability of the system is poor.
Disclosure of Invention
In order to solve the problems existing in the prior art, the invention aims to provide a pyrolysis-gasification integrated device and a pyrolysis-gasification integrated process.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
The pyrolysis-gasification integrated device comprises a pyrolysis furnace gasifier which is communicated with each other, and a semicoke distributor with a transverse pipe for condensation is arranged between the pyrolysis furnace and the gasifier;
the top end of the pyrolysis furnace is provided with a feed inlet, and one side of the feed inlet is provided with a pyrolysis furnace gas outlet; the gas outlet of the pyrolysis furnace is connected with the cyclone separator; the top outlet of the cyclone separator is connected with the distillation tower through an indirect constant cooler;
The gasification furnace is provided with a gasification gas outlet which is connected with the desulfurization device;
The gasification furnace is provided with a gasification nozzle communicated with the inside of the gasification furnace.
The invention is further improved in that the semicoke distributor with the horizontal pipe condensation is connected with the refractory brick lining, and comprises the horizontal pipes which are uniformly distributed; the transverse pipes are triangular prism structures with upper tips and lower widths, are distributed in a manner of being uniformly distributed in a crisscross manner, and form square holes; the interior of the transverse tube is provided with a condensing tube.
The invention is further improved in that the outlet at the bottom end of the cyclone separator is connected with the gasification nozzle; the inner wall of the gasification furnace is provided with a refractory brick lining, and a water cooling wall is arranged inside the refractory brick lining.
The invention is further improved in that the water cooling wall inside the refractory brick lining is communicated with the condensing pipe inside the transverse pipe.
The invention is further improved in that a rotary distributor is arranged in the pyrolysis furnace, and a feed inlet is communicated with the rotary distributor.
The invention is further improved in that the indirect constant cooler comprises a first indirect constant Leng Qi and a second indirect constant Leng Qi, and spray devices are arranged at the top parts of the inside of the first indirect constant Leng Qi and the inside of the second indirect constant cooler;
the upper outlet of the side wall of the distillation tower is connected with the inlets of the tops of the first indirect constant Leng Qi and the second indirect constant cooler.
The invention is further improved in that the outlet at the top end and the outlet at the bottom end of the distillation column are connected with a tar collecting tank; the tar collecting tank comprises a light tar collecting tank and a heavy tar collecting tank from top to bottom;
The bottom end of the gasification furnace is provided with a circulating cooling device, a slag discharging device is arranged in the circulating cooling device, the slag discharging device is positioned at the outlet of the bottom of the gasification furnace, and the bottom of the circulating cooling device is provided with an ash and slag groove;
the number of the gasification nozzles is four, and the gasification nozzles are uniformly distributed along the circumferential direction of the gasification furnace.
An integrated pyrolysis-gasification process comprising the steps of:
(1) The gasification process is carried out:
Mixing pulverized coal with a gasifying agent, and then introducing the mixture into a gasifier for gasification to obtain high-temperature gasification gas and slag which mainly comprise carbon monoxide and hydrogen; slag generated in the gasification process enters a circulating cooling device to quench slag, and the temperature in a gasification furnace is 1100-1500 ℃; part of high-temperature gasification gas generated in the gasification process upwards enters a pyrolysis furnace to participate in the pyrolysis process, and the other part of the high-temperature gasification gas enters a desulfurization device through a gasification gas outlet to carry out desulfurization purification to obtain gasification gas;
(2) And (3) carrying out a pyrolysis process:
Adding pulverized coal into a pyrolysis furnace, and pyrolyzing the pulverized coal in the pyrolysis furnace under the heating action of high-temperature gasification gas generated in the gasification process in a gasification furnace to generate pyrolysis furnace gas and pyrolysis semicoke; in the pyrolysis process, the temperature in the pyrolysis furnace is 500-800 ℃; the pyrolysis semicoke enters a gasification furnace to participate in the gasification process through a semicoke distributor with a transverse pipe for condensation, so that pyrolysis and gasification integration is realized;
The pyrolysis furnace gas enters a cyclone separator for dust removal and purification, then enters an indirect constant cooler for cooling and condensation through an outlet of the cyclone separator, and then is distilled through a distillation tower to obtain medium tar.
The invention is further improved in that the indirect constant cooler comprises a first indirect constant Leng Qi and a second indirect constant Leng Qi, and spray devices are arranged at the top parts of the inside of the first indirect constant Leng Qi and the inside of the second indirect constant cooler; and the spraying devices in the first indirect constant Leng Qi and the second indirect constant cooler flush tar condensed by the gas in the pyrolysis furnace, and then distill to obtain light tar and heavy tar.
The invention is further improved in that the temperature of the first indirect constant cooler is 30-50 ℃, and the temperature of the second indirect constant cooler is 10-20 ℃;
The pyrolysis temperature of the pyrolysis furnace is 500-800 ℃, the gasification temperature of the gasification furnace is 1100-1500 ℃, and the pressure in the pyrolysis furnace and the gasification furnace is 2-4MPa;
The gasifying agent comprises steam and oxygen, and the molar ratio of the steam to the oxygen is 100 (1-10).
Compared with the prior art, the invention has the following beneficial effects:
1. The invention realizes the functions of pyrolysis at the upper part and gasification at the lower part in one furnace body. The pyrolysis furnace and the gasification furnace can be fed simultaneously, and under the high-temperature and high-pressure operation condition, the pyrolysis and gasification efficiency is improved, the unit gas production capacity of the equipment is greatly enhanced, and the quality of coal gas and gasification gas is improved.
2. The raw material has wide selectivity. The invention can effectively transform any coal species, can treat various coals such as anthracite, petroleum coke, bituminous coal, lignite and the like, and the raw materials used by the invention are not limited to the coals, and can also use oil, biomass and mixtures thereof including the coals.
3. High energy utilization rate and good environmental benefit. The invention adopts high-temperature pressurizing operation conditions, and has high heat efficiency; the granularity of the fed pulverized coal is small, the gasification reaction is fully carried out, and the byproducts are few.
Drawings
The drawings are only used for matching with the content of the specification, and do not limit the invention, so the invention has no technical essential meaning, and any structural modification, proportion relation or size adjustment falls within the scope covered by the technical content disclosed by the invention under the condition that the efficacy generated by the invention is not affected.
FIG. 1 is a schematic view of a pyrolysis-gasification integrated apparatus according to the present invention;
FIG. 2 is a top view of a semicoke distributor with cross tube condensation;
FIG. 3 is a schematic diagram of a cross tube distribution structure;
FIG. 4 is a schematic cross-sectional view of a cross-tube;
In the figure, a feed inlet is formed in the bottom of the cylinder; 2-a rotating distributor; 3-a semicoke distributor with a horizontal tube for condensation; 4-water cooling walls; 5-gasification gas outlet; 6-refractory brick lining; 7-a gasification nozzle; 8-a circulating cooling device; 9-a slag discharging device; 10-ash slag groove; 11-a pyrolysis furnace gas outlet; 12-cyclone separator; 13-a spraying device; 14-a first indirect constant Leng Qi; 15-a second indirect constant Leng Qi; 16-a distillation column; 17-a tar collection tank; 18-a first waste heat boiler; 19-a second waste heat boiler; 20-a desulfurizing device; 21-a gasification gas storage tank; 22-transverse tube; 23-condensing tubes; 24-pyrolysis furnace; 25-gasification furnace.
Detailed Description
The present invention will be further described with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent.
The terms such as "upper", "lower", "top", "bottom", and the like are used in this specification for ease of description only. And not as limitations on the scope of what may be practiced or of what may be other than the specific details, and which may be other than the specific details.
Referring to fig. 1 and 2, a pyrolysis-gasification integrated apparatus of the present invention includes: a pyrolysis furnace 24, a gasification furnace 25 and a feed inlet 1; a rotary distributor 2; a semicoke distributor 3 with a horizontal tube for condensation; a water cooling wall 4; a gasification gas outlet 5; a refractory brick lining 6; a gasification nozzle 7; a circulation cooling device 8; a slag discharging device 9; a slag bath 10; a pyrolysis furnace gas outlet 11; a cyclone separator 12; a spraying device 13; first indirect constant Leng Qi; second indirect constant Leng Qi; a distillation column 16; a tar collection tank 17; a first waste heat boiler 18; a second waste heat boiler 19; a desulfurizing device 20; a gasification gas storage tank 21; a cross tube 22 and a condenser tube 23.
Specifically, referring to fig. 1, the pyrolysis-gasification integrated device comprises a pyrolysis furnace 24, a gasification furnace 25, a circulation cooling device 8 and an ash tank 10 from top to bottom; a semicoke distributor 3 with a horizontal pipe for condensation is arranged between the pyrolysis furnace 24 and the gasification furnace 25; the circulating cooling device 8 is arranged at the bottom of the gasification furnace 25 and is communicated with the gasification furnace 25, a slag discharging device 9 is arranged between the circulating cooling device 8 and the gasification furnace 25, and the slag groove 10 is arranged at the bottom of the circulating cooling device 8.
The top end of the pyrolysis furnace 24 is provided with a feed inlet 1, and one side of the feed inlet 1 is provided with a pyrolysis furnace gas outlet 11; a rotary distributor 2 is arranged in the pyrolysis furnace 24, and a feed inlet 1 is communicated with the rotary distributor 2; the pyrolysis furnace gas outlet 11 is connected with a cyclone separator 12; the top outlet of the cyclone separator 12 is connected with the bottom inlet of the first indirect constant cooler 14, and the top outlet of the first indirect constant cooler 14 is connected with the bottom inlet of the second indirect constant Leng Qi; the outlets of the bottom ends of the first indirect constant cooler 14 and the second indirect constant cooler 15 are connected with the inlet of the distillation tower 16; the top of the inside of the first indirect constant cooler 14 and the second indirect constant Leng Qi are respectively provided with a spraying device 13, and the outlet of the upper part of the side wall of the distillation tower 16 is connected with the inlet of the top of the first indirect constant cooler 14 and the second indirect constant Leng Qi; the top and bottom outlets of distillation column 16 are connected to tar collection tank 17. The tar collection tank 17 includes a light tar collection tank and a heavy tar collection tank from top to bottom.
The upper part of the side wall of the gasification furnace 25 is provided with a gasification gas outlet 5, the lower part of the side wall of the gasification furnace 25 is provided with a gasification nozzle 7, the bottom end of the gasification furnace 25 is provided with a circulating cooling device 8, a slag discharging device 9 is positioned at the outlet of the bottom of the gasification furnace 25, and the bottom of the circulating cooling device 8 is provided with an ash and slag groove 10; the gasification gas outlet 5 is sequentially connected with the first waste heat boiler 18 and the second waste heat boiler 19 in series, specifically, the gasification gas outlet 5 is connected with the bottom inlet of the first waste heat boiler 18, the top outlet of the first waste heat boiler 18 is connected with the bottom inlet of the second waste heat boiler 19, the top outlet of the second waste heat boiler 19 is connected with the bottom inlet of the desulfurization device 20, and the top outlet of the desulfurization device 20 is connected with the inlet of the gasification gas storage tank 21; the raw materials and gasifying agent enter a gasification furnace 25 through a gasification nozzle 7, and the outlet at the bottom end of a cyclone separator 12 is connected with the gasification nozzle 7; the inner wall of the gasification furnace 25 is provided with a refractory brick lining 6, and a water cooling wall 4 is arranged in the refractory brick lining 6.
The gasification nozzles 7 are four nozzles uniformly distributed along the circumferential direction of the gasification furnace 25.
Referring to fig. 2, a semicoke distributor 3 with horizontal tube condensation is connected with a refractory brick lining 6, and the semicoke distributor 3 with horizontal tube condensation comprises a plurality of horizontal tubes 22 which are uniformly distributed; referring to fig. 3 and 4, the transverse tube 22 has a triangular prism structure, the interior of the transverse tube 22 is provided with a plurality of condensing tubes 23, and the condensing tubes 23 are uniformly distributed in a crisscross manner to form square holes.
The material of the transverse tube 22 is the same as that of the refractory brick lining 6.
Referring to fig. 1 and 2, the water wall 4 inside the firebrick lining 6 is in communication with a condenser tube 23 inside the cross tube 22.
The pyrolysis-gasification integrated process provided by the invention comprises the following steps of:
(1) Treating the raw materials
After the raw material coal is dried, crushing, grinding and screening are carried out to obtain coal powder with the particle size smaller than and larger than 75 mu m, which are respectively called coal powder-1 and coal powder-2.
(2) Gasification process
The pulverized coal-1 and the gasifying agent are mixed and then enter the gasifier 25 through the gasifying nozzle 7, the pulverized coal-1 and the gasifying agent are subjected to the high-temperature radiation action of the refractory brick lining 6 in the gasifier 25 and rapidly undergo a series of complex physical and chemical processes such as preheating, carbonization, cracking combustion of volatile matters, gasification of carbon and the like, and high-temperature gasified gas and slag mainly comprising carbon monoxide and hydrogen are obtained; in the gasification process, the temperature in the gasification furnace 25 is maintained at 1100-1500 ℃ by controlling the addition amount of raw materials and gasifying agent, the cooling efficiency of the water-cooled wall 4 and the like. Slag generated in the gasification process enters a circulating cooling device 8 through a slag discharging device 9 to quench slag, and the cooled slag is discharged into an ash slag groove 10. Part of high-temperature gasification gas generated in the gasification process enters the pyrolysis furnace 24 upwards to participate in the pyrolysis process, and the other part of the high-temperature gasification gas enters the first waste heat boiler 18 and the second waste heat boiler 19 in sequence through the gasification gas outlet 5 to be cooled, so that heat is recovered; the cooled high-temperature gasified gas enters a desulfurization device 20 for desulfurization and purification, and the purified gasified gas enters a gasified gas storage tank 21 for collection and storage.
(3) Pyrolysis process
The pulverized coal-2 is uniformly added into a pyrolysis furnace 24 through a feed inlet 1 and a rotary distributor 2, and the pulverized coal-2 is heated in the pyrolysis furnace 24 by high-temperature gasification gas generated in a gasification process in a gasification furnace 25 to be pyrolyzed, so as to generate pyrolysis furnace gas and pyrolysis semicoke; in the pyrolysis process, the temperature of the pyrolysis furnace 24 is maintained at 500-800 ℃ by controlling the addition amount of the pulverized coal-2 and the gasification process. Pyrolysis semicoke generated in the pyrolysis process downwards enters the gasification furnace 25 through the semicoke distributor 3 with the transverse pipe condensation to participate in the gasification process, so that pyrolysis and gasification integrated operation is realized.
The pyrolysis furnace gas generated in the pyrolysis process enters a cyclone separator 12 through a pyrolysis furnace gas outlet 11 to remove dust, high-temperature ash and the pyrolysis furnace gas after dust removal are generated, the obtained high-temperature ash downwards passes through a bottom outlet of the cyclone separator 12, coal dust-2 and gasifying agent enter a gasification furnace 25 through a nozzle 7, the pyrolysis furnace gas after dust removal sequentially enters a first indirect constant cooler 14 and a second indirect constant cooler 15 through a top outlet of the cyclone separator 12 to cool and condense, tar obtained after condensation enters a distillation tower 16 through the first indirect constant cooler 14 and the second indirect constant Leng Qi to distill, medium tar obtained by distillation washes tar condensed by the pyrolysis furnace gas through a spraying device 13 at the upper part in the first indirect constant cooler 14 and the second indirect constant cooler 15 through an upper outlet of the distillation tower 16, and light tar and heavy tar obtained by distillation are respectively collected in a tar collecting tank and a heavy tar collecting tank through an upper outlet and a lower outlet of the distillation tower 16.
Through the steps, the pyrolysis and gasification reaction of the coal are realized, and tar and gasification gas are obtained. According to actual needs, the technological process of the device can be adjusted, for example, the gasification gas outlet can be selectively closed, and only tar is produced;
The temperature of the first indirect intercooler 14 is controlled to be 30-50 deg.c, and the temperature of the second indirect intercooler 15 is controlled to be 10-20 deg.c.
In the operation process of the pyrolysis-gasification integrated device, the pyrolysis temperature of the pyrolysis furnace 24 is controlled to be 500-800 ℃, the gasification temperature of the gasification furnace 25 is controlled to be 1100-1500 ℃, and the furnace body pressure is controlled to be 2-4MPa.
The raw materials in the pyrolysis-gasification integrated process are illustrated by taking coal as an example, but the raw materials are not limited to the coal, and can be coal, oil, biomass or a mixture of two of the coal, the oil and the biomass; the coal is not limited, the oil can be heavy coal tar, and the biomass can be agricultural and forestry waste and household garbage;
The gasifying agent comprises water vapor and oxygen, is a common gasifying agent in the field, and can be adjusted by a person skilled in the art according to the actual condition of field operation; the molar ratio of the vapor to the oxygen of the gasifying agent is controlled to be 100 (1-10).
To illustrate the effect of the present invention, the following examples use low metamorphic bituminous coal and biomass as raw materials for the pyrolysis-gasification integrated process.
Example 1
A. crushing, grinding and screening the low-metamorphic bituminous coal to obtain coal dust with the particle size smaller than and larger than 75 mu m respectively, which are called coal dust-1 and coal dust-2 respectively;
b. the pulverized coal-1 and gasifying agent are taken as raw materials of the gasifier 25 and enter the gasifier 25 of the pyrolysis-gasification integrated furnace through the gasification nozzle 7, the pulverized coal-1 and the gasifying agent are subjected to the high-temperature radiation action of the refractory brick lining 6 in the gasifier 25 and rapidly undergo a series of complex physical and chemical processes such as preheating, carbonization, cracking combustion of volatile matters, gasification of carbon and the like, and high-temperature gasified gas and slag mainly comprising carbon monoxide and hydrogen are obtained; the temperature of the gasification furnace 25 is controlled between 1100 ℃ and 1500 ℃;
c. B, allowing slag generated in the gasifier 25 to enter a circulating cooling device 8 downwards through a slag discharging device 9 to quench slag, and allowing the slag to be trapped in water after quenching and solidification by the circulating cooling device 8 and fall into an ash slag groove 10 for timed discharge;
d. Part of the high-temperature gasification gas generated in the gasification furnace 25 in the step b enters the pyrolysis furnace 24 upwards to participate in the pyrolysis reaction; part of the gasified gas enters the first waste heat boiler 18 and the second waste heat boiler 19 through the gasified gas outlet 5 to recycle heat, the cooled gasified gas enters the desulfurization device 20 to be desulfurized, and the desulfurized gasified gas enters the gasified gas storage tank 21 to be collected and stored;
e. The pulverized coal-2 is added into a pyrolysis furnace 24 through a feed inlet 1 via a rotary distributor 2, and high-temperature gasification gas entering the pyrolysis furnace 24 is used as a heat carrier to heat the pulverized coal-2 for pyrolysis, so that pyrolysis furnace gas and pyrolysis semicoke are generated; the temperature of the pyrolysis furnace 24 is controlled to be 500-800 ℃;
f. The pyrolysis semicoke generated in the step e enters a gasification furnace 25 downwards through a semicoke distributor 3 with a transverse pipe for condensation to participate in gasification reaction;
g. The pyrolysis furnace gas generated in the step e enters a cyclone separator 12 through a pyrolysis furnace gas outlet 11 to remove dust, high-temperature ash obtained by separation, pulverized coal-1 and gasifying agent enter a gasification furnace 25, the pyrolysis furnace gas after dust removal is cooled and condensed through a first indirect constant cooler 14 and a second indirect constant Leng Qi to generate tar, the obtained tar enters a distillation tower 16 to be distilled, medium fractions are washed through a spray device 13 at the upper part of the first indirect constant cooler 14 and the second indirect constant cooler 15 through an outlet at the upper part of the distillation tower 16 to condense the pyrolysis furnace gas, and light tar and heavy tar are respectively collected in a light tar collecting tank and a heavy tar collecting tank through an outlet at the top end and the bottom end of the distillation tower 16;
f. the pressure in the furnace body of the pyrolysis-gasification integrated furnace is controlled to be 2-4MPa.
In the step, the effective components of the gasification gas from the gasification furnace 25, namely CO and H 2, are more than 90%, and the methane content is low.
Example 2
In this example, low-metamorphic bituminous coal and biomass are used as raw materials, the raw materials added into the pyrolysis furnace 24 are changed into ground and sieved biomass on the basis of example 1, and the pressure and temperature inside the furnace body are kept unchanged. The specific operation steps of this example are the same as those of example 1.
In the embodiment 2, the active ingredients of the gasification gas from the gasification furnace 25 include CO, H 2 and CH 4, wherein the volume content of CH 4 is about 8%.
The embodiments of the present invention are merely described in terms of preferred embodiments of the present invention, and are not intended to limit the spirit and scope of the present invention, but various modifications or improvements of the technical solutions of the present invention should be made by those skilled in the art without departing from the design concept of the present invention.
Claims (5)
1. The pyrolysis-gasification integrated device is characterized by comprising a pyrolysis furnace (24) and a gasification furnace (25) which are communicated, wherein a semicoke distributor (3) with a transverse pipe for condensation is arranged between the pyrolysis furnace (24) and the gasification furnace (25);
A feed inlet (1) is formed in the top end of the pyrolysis furnace (24), and a pyrolysis furnace gas outlet (11) is formed in one side of the feed inlet (1); the pyrolysis furnace gas outlet (11) is connected with the cyclone separator (12); the top outlet of the cyclone separator (12) is connected with a distillation tower (16) through an indirect constant cooler;
The gasification furnace (25) is provided with a gasification gas outlet (5), and the gasification gas outlet (5) is connected with the desulfurization device (20);
The gasification furnace (25) is provided with a gasification nozzle (7) communicated with the inside of the gasification furnace (25);
The semicoke distributor (3) with the horizontal pipe condensation is connected with the refractory brick lining (6), and the semicoke distributor (3) with the horizontal pipe condensation comprises horizontal pipes (22) which are uniformly distributed; the transverse pipes (22) are triangular prism structures with upper tips and lower widths, are distributed in a manner of being uniformly distributed in a crisscross manner, and square holes are formed among the transverse pipes (22); a condenser tube (23) is arranged in the transverse tube (22);
The outlet at the bottom end of the cyclone separator (12) is connected with the gasification nozzle (7); the inner wall of the gasification furnace (25) is provided with a refractory brick lining (6), and a water cooling wall (4) is arranged inside the refractory brick lining (6);
The water cooling wall (4) in the refractory brick lining (6) is communicated with the condensing pipe (23) in the transverse pipe (22);
the top end outlet and the bottom end outlet of the distillation tower (16) are connected with a tar collecting tank (17); the tar collecting tank (17) comprises a light tar collecting tank and a heavy tar collecting tank from top to bottom;
The bottom end of the gasification furnace (25) is provided with a circulating cooling device (8), a slag discharging device (9) is arranged in the circulating cooling device (8), the slag discharging device (9) is positioned at the outlet of the bottom of the gasification furnace (25), and an ash and slag groove (10) is arranged at the bottom of the circulating cooling device (8);
the number of the gasification nozzles (7) is four, and the gasification nozzles are uniformly distributed along the circumferential direction of the gasification furnace (25);
The indirect constant cooler comprises a first indirect constant Leng Qi (14) and a second indirect constant Leng Qi (15), and spraying devices (13) are arranged at the top parts inside the first indirect constant Leng Qi (14) and the second indirect constant Leng Qi (15);
The upper outlet of the side wall of the distillation column (16) is connected with the inlets at the top of the first indirect constant Leng Qi (14) and the second indirect constant Leng Qi (15).
2. The pyrolysis-gasification integrated device according to claim 1, wherein a rotary distributor (2) is arranged in the pyrolysis furnace (24), and the feed inlet (1) is communicated with the rotary distributor (2).
3. A pyrolysis-gasification integrated process based on the apparatus of claim 1, comprising the steps of:
(1) The gasification process is carried out:
Mixing pulverized coal and a gasifying agent, and then introducing the mixture into a gasifier (25) for gasification to obtain high-temperature gasification gas and slag mainly comprising carbon monoxide and hydrogen; slag generated in the gasification process enters a circulating cooling device (8) to be quenched, and the temperature in a gasification furnace (25) is 1100-1500 ℃; part of high-temperature gasification gas generated in the gasification process upwards enters a pyrolysis furnace (24) to participate in the pyrolysis process, and the other part enters a desulfurization device (20) through a gasification gas outlet (5) to carry out desulfurization purification to obtain gasification gas;
(2) And (3) carrying out a pyrolysis process:
Adding pulverized coal into a pyrolysis furnace (24), wherein the pulverized coal is pyrolyzed in the pyrolysis furnace (24) under the heating action of high-temperature gasification gas generated in the gasification process in a gasification furnace (25) to generate pyrolysis furnace gas and pyrolysis semicoke; in the pyrolysis process, the temperature in the pyrolysis furnace (24) is 500-800 ℃; the pyrolysis semicoke enters a gasification furnace (25) to participate in the gasification process through a semicoke distributor (3) with a transverse pipe for condensation, so that pyrolysis and gasification integration is realized;
The pyrolysis furnace gas enters a cyclone separator (12) for dust removal and purification, then enters an indirect constant cooler for cooling and condensation through an outlet of the cyclone separator (12), and then is distilled through a distillation tower (16) to obtain medium tar.
4. A pyrolysis-gasification integrated process according to claim 3, wherein the indirect cooler comprises a first indirect constant Leng Qi (14) and a second indirect constant Leng Qi (15), and the top inside the first indirect constant Leng Qi (14) and the second indirect constant Leng Qi (15) are both provided with a spraying device (13); the spraying devices (13) in the first indirect constant Leng Qi (14) and the second indirect constant Leng Qi (15) flush tar condensed by coal gas in the pyrolysis furnace (24), and then distill to obtain light tar and heavy tar.
5. A pyrolysis-gasification integrated process according to claim 3, wherein the temperature of the first indirect constant Leng Qi (14) is 30-50 ℃ and the temperature of the second indirect constant Leng Qi (15) is 10-20 ℃;
The pyrolysis temperature of the pyrolysis furnace (24) is 500-800 ℃, the gasification temperature of the gasification furnace (25) is 1100-1500 ℃, and the pressure in the pyrolysis furnace and the gasification furnace (25) is 2-4MPa;
The gasifying agent comprises steam and oxygen, and the molar ratio of the steam to the oxygen is 100 (1-10).
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| CN114686269A (en) * | 2020-12-27 | 2022-07-01 | 新疆宜化化工有限公司 | Circulating fluidized bed coal gasifier for preventing furnace bottom coke slag and quartz sand from solidifying to form plate-shaped body |
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