CN104987891B - A kind of alternative fuel based on coal hydrocarbon component classification gasification/chemical products production system - Google Patents
A kind of alternative fuel based on coal hydrocarbon component classification gasification/chemical products production system Download PDFInfo
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- 238000002309 gasification Methods 0.000 title claims abstract description 123
- 239000003245 coal Substances 0.000 title claims abstract description 107
- 239000000126 substance Substances 0.000 title claims abstract description 75
- 239000000446 fuel Substances 0.000 title claims abstract description 62
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 56
- 239000004215 Carbon black (E152) Substances 0.000 title abstract description 22
- 229930195733 hydrocarbon Natural products 0.000 title abstract description 22
- 150000002430 hydrocarbons Chemical class 0.000 title abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 112
- 239000000571 coke Substances 0.000 claims abstract description 107
- 239000001257 hydrogen Substances 0.000 claims abstract description 43
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 43
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000007906 compression Methods 0.000 claims abstract description 15
- 238000010248 power generation Methods 0.000 claims abstract description 8
- 238000003786 synthesis reaction Methods 0.000 claims description 44
- 238000000034 method Methods 0.000 claims description 38
- 238000000926 separation method Methods 0.000 claims description 38
- 238000002360 preparation method Methods 0.000 claims description 25
- 150000002431 hydrogen Chemical class 0.000 claims description 19
- 230000008569 process Effects 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 18
- 230000015572 biosynthetic process Effects 0.000 claims description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 14
- 229910052799 carbon Inorganic materials 0.000 claims description 14
- 238000011084 recovery Methods 0.000 claims description 14
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 12
- 239000002918 waste heat Substances 0.000 claims description 11
- 230000006835 compression Effects 0.000 claims description 10
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 8
- 239000002802 bituminous coal Substances 0.000 claims description 8
- 238000012824 chemical production Methods 0.000 claims description 8
- 239000003546 flue gas Substances 0.000 claims description 8
- 239000003077 lignite Substances 0.000 claims description 8
- 230000010354 integration Effects 0.000 claims description 5
- 239000003034 coal gas Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 3
- 239000003830 anthracite Substances 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 239000002028 Biomass Substances 0.000 claims description 2
- 239000012495 reaction gas Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000004480 active ingredient Substances 0.000 abstract 1
- 238000001311 chemical methods and process Methods 0.000 abstract 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 48
- 239000000047 product Substances 0.000 description 39
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 20
- 238000002485 combustion reaction Methods 0.000 description 14
- 239000001569 carbon dioxide Substances 0.000 description 10
- 229910002091 carbon monoxide Inorganic materials 0.000 description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- 238000002156 mixing Methods 0.000 description 4
- 238000003763 carbonization Methods 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000010000 carbonizing Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000005773 Enders reaction Methods 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000002864 coal component Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Industrial Gases (AREA)
Abstract
The invention discloses a kind of alternative fuel/chemical products production system, coal hydrocarbon component classification gasification and traditional chemical process, including gasification island and chemical industry island are coupled, chemical industry island converter unit and CO is utilized2The CO that separative element is produced2, to the island coke gasification that gasifies, so that Water gas shift/WGS and CO needed for having eliminated Primordial Qi island2Separative element, reduces energy consumption and equipment investment；After hydrogen-rich coke-stove gas, richness CO gasification gases, the hydrogen obtained from gasification island is mixed by a certain percentage, suitable H is obtained2/ CO than the new gas of synthetic reaction, meet the requirement of alternative fuel/chemical products production, realize component counterpart, the cascade utilization of active ingredient；The steam that gasification island coke-stove gas, gasification gas Exposure degree are obtained is used for chemical industry island steam turbine power generation, and an electric power part for chemical industry island richness production is used for the CO needed for island that gasifies2Compression, realize gasification island and chemical industry island energy utilization it is efficiently integrated.
Description
Technical Field
The invention belongs to the field of energy power and coal chemical industry, relates to efficient and clean utilization of coal, and particularly relates to a system for producing alternative fuels/chemical products based on staged gasification of hydrocarbon components of coal.
Background
The existing production process of alternative fuels/chemical products is mostly based on the traditional coal gasification technology, such as Shell coal gasification, GE coal gasification and the like. Whereas the conventional coal gasification process (as shown in FIG. 1) is O2Or O2The mixture with steam is a gasifying agent, which consumes a large amount of pure oxygen, and the oxygen preparation causes a large amount of power consumption (generally speaking, the power consumption of an air separation unit accounts for about 60-70% of the total power consumption of a coal chemical plant) and additional equipment investment. To match the power consumption of the whole plant, conventional chemical plants are typically equipped with small, inefficient self-contained power plants, further reducing the energy conversion efficiency of the whole plant.
Moreover, the conventional coal gasification technology based on the existing production process of alternative fuels/chemical products can only obtain carbon-rich synthesis gas, the gasified gas product is single, and a water gas shift unit is required to be equipped to convert most of CO into H2Can meet the requirement of the production of alternative fuels/chemical products on the high H of the synthesis gas2The requirement of the/CO ratio, which results in a loss of chemical energy of the synthesis gas.
Meanwhile, the traditional alternative fuel production process has strict requirements on the coal type, which depends on the coal gasification mode adopted by the system. The residual resource amount of coal in China is about 1.54 trillion tons, and the coal is divided into lignite, bituminous coal and anthracite. The lurgi furnace can adopt brown coal and partial bituminous coal (long flame coal, non-caking coal, weakly caking coal and gas coal), and the available resource amount is 5934.5 hundred million tons, which accounts for 58 percent of the total resource amount. The Texaco furnace can adopt most of bituminous coal, the available resource amount is 6728.8 hundred million tons, and the available resource amount accounts for 66 percent of the total resource amount. The Sheer furnace can adopt lignite and almost all bituminous coal, the resource amount is 9242 hundred million tons, and the resource amount accounts for 91 percent of the total resource amount. The Ender furnace can adopt brown coal and a small part of bituminous coal (long flame coal and non-caking coal), and the available resource amount is 4479.6 hundred million tons, which accounts for 44 percent of the total resource amount.
Aiming at the problems of large air separation power consumption, low efficiency of a self-contained power plant and gasification product H in the traditional alternative fuel/chemical product production process2The method is based on the principle of 'component matching and grading conversion' of fuel, and comprises the steps of carbonizing coal, producing carbon monoxide, and transforming to produce hydrogen, firstly carbonizing and purifying the coal to obtain crude coke, then reacting the crude coke with carbon dioxide to generate carbon monoxide, finally generating hydrogen and carbon dioxide through a transformation reaction, and supplying the carbon dioxide to a coke carbon monoxide carbonization unit. The gasification method for the staged conversion of the hydrocarbon component of the coal, which is proposed by the Chinese patent CN201210592802.7, can greatly reduce the irreversibility of the gasification process of the coal and obviously improve the gasification efficiency of the coal, but can obtain the coal prepared by the methodHow to efficiently prepare and utilize the synthetic gas with different carbon-hydrogen ratios obtained by mixing the hydrogen, the carbon monoxide and the coke oven gas does not provide a feasible operation path. The invention provides an alternative fuel/chemical product production system for 'coal hydrocarbon component graded gasification' based on the thought of 'component matching and graded conversion', and the components between a gasification island and a chemical island are effectively coupled with energy, so that the defect of low energy conversion efficiency of the traditional alternative fuel/chemical product is overcome.
Disclosure of Invention
In order to overcome the defects and shortcomings of the prior art, the invention aims to provide a production system of alternative fuels/chemical products, wherein the production system is divided into a gasification island and a chemical island, and components and energy between the gasification island and the chemical island are fully and effectively coupled based on the concept of 'coal hydrocarbon component graded gasification'.
The technical scheme adopted by the invention for realizing the technical purpose is as follows:
a production system of alternative fuel/chemical products comprises a gasification island and a chemical island, wherein the gasification island comprises a burner, a coke preparation unit and a coke gasification unit, hot coal and preheated high-temperature air are combusted in the burner to generate high-temperature flue gas, then the high-temperature flue gas is fed into the coke preparation unit and the coke gasification unit, the coke preparation unit prepares the gasified coal into coke, the coke is fed into the coke gasification unit, hydrogen-rich coke oven gas prepared by the coke preparation unit and CO-rich gasified gas prepared by the coke gasification unit are fed into the chemical island, and the production system is characterized in that,
the chemical island comprises a water gas shift unit and CO2A separation unit and an alternative fuel production/chemical synthesis unit, wherein,
-the CO-rich gasified gas produced by the coke gasification unit in the gasification island is divided into two paths after heat recovery by a waste heat boiler, one path is introduced into the water gas shift unitReacting with water vapor to generate CO2Mixture of gas and hydrogen, after which the mixture is passed over said CO2Separation unit for separation into CO2Gas and hydrogen, and the other path of CO-rich gasified gas and the CO2The hydrogen separated by the separation unit and the hydrogen-rich coke oven gas prepared by the coke preparation unit and subjected to heat recovery by another waste heat boiler are mixed in proportion to form H2The synthesis reaction new gas of the CO is introduced into the alternative fuel production/chemical synthesis unit to produce alternative fuel/chemical products;
- -said CO2CO separated by a separation unit2The gas is divided into two paths, one path is through CO2The compressed coke is introduced into the coke gasification unit in the gasification island, and the other path is directly emptied or passes through CO2After being purified by the purification unit, the carbon is trapped by compressing the carbon by the compression unit;
the steam recovered by the alternative fuel production/chemical synthesis unit and the steam recovered by each waste heat boiler are merged and then introduced into a steam turbine and power generation equipment unit for power generation, and part of the obtained power is used for driving the CO2A compressor.
Further, the substitute fuel production/chemical synthesis unit is a methanation synthesis unit, the methanation synthesis unit comprises a plurality of stages of methanation reactors, wherein unreacted gas discharged from a first stage of methanation reactor is mostly compressed and then recycled to enter the first stage of methanation reactor, and the rest of the unreacted gas is cooled and then is introduced into a next stage of methanation reactor.
Further, the hydrogen-rich coke oven gas prepared by the coke preparation unit is subjected to heat recovery and cooling, then is introduced into a desulfurization unit to remove sulfur, and is compressed, and then is mixed with the CO-rich gasified gas and the CO2The hydrogen separated by the separation unit is converged to synthesize the new reaction gas.
Preferably, the CO is2CO of a separation unit2The separation mode includes various CO2Separation methods, including but not limited to Selexol, PSA, MEA, etc; removing CO required for coke gasification2，CO2Excess CO obtained in the separation unit2Carbon capture can be performed either after evacuation or compression.
Preferably, the gasified coal types include various types of lignite, bituminous coal and anthracite, the heat supply coal is all types of coal, and the coke is all coke, including but not limited to metallurgical coke.
Preferably, the chemical synthesis comprises a plurality of chemical synthesis processes, including a plurality of chemical synthesis processes of methane, hydrogen, methanol, dimethyl ether, synthetic oil and the like. The synthesis of each chemical product involves a variety of production processes and is not limited to a particular process. The output products are various chemical products and alternative fuels, including but not limited to methane, hydrogen, methanol, dimethyl ether, synthetic oil, etc.
The gasification island adopts a 'coal hydrocarbon component grading gasification' method. The gasified coal is firstly subjected to coke preparation and coke oven gas production processes to obtain products such as crude coke, coke oven gas, tar and the like, and the required heat is provided by heat generated by combustion of heat supply coal and high-temperature air in an external combustion type combustor. And secondly, carrying out a process of preparing CO by gasifying coke, reacting the high-temperature crude coke obtained in the coke preparation process with carbon dioxide to produce high-purity CO, wherein the heat required in the process is also provided by the heat generated by burning the heat supply coal and high-temperature air. And then, performing a CO conversion hydrogen production process, performing a conversion reaction on part of carbon monoxide produced in the process of preparing CO by gasifying the coke and water vapor to generate carbon dioxide and hydrogen, separating by using a separation device to obtain carbon dioxide and pure hydrogen, returning part of the separated carbon dioxide to the device for preparing CO by gasifying the coke to continuously react with the coke, and emptying the rest part of the carbon dioxide or performing carbon capture and utilization.
The hydrogen-rich coke oven gas and the CO-rich gasified gas obtained through the three steps are obtainedAnd H2Mixing the three gas products according to a certain proportion to obtain the product with wide range of H2The new gas of the chemical synthesis reaction with the ratio of/CO is introduced into a chemical synthesis unit to prepare the alternative fuel/chemical product.
The alternative fuel/chemical product production system of the invention has the following remarkable characteristics:
(1) firstly, the invention organically combines a transformation unit in the 'coal hydrocarbon component grading gasification' method with a modulation unit in chemical synthesis, and CO generated by the modulation unit in chemical synthesis2Is provided to a char gasification unit. In the production process of alternative fuels/chemical products, a water gas shift unit is required to convert part of CO in synthesis gas into CO by reacting with steam2And H2Separation of CO2After make H2The ratio of/CO meets the synthesis requirement. In the gasification method adopted by the invention, CO is needed2The coke is gasified as a gasifying agent. Therefore, CO generated by chemical islands2The method is used for gasification of the gasification island coke, and can eliminate a water gas shift unit in a coal hydrocarbon component grading gasification method, thereby reducing the system energy consumption and equipment investment.
(2) Secondly, the invention realizes the component-to-port gradient utilization between the effective components of the gasification island and the chemical island by 'coal hydrocarbon component graded gasification'. The wide range of H is obtained by adjusting different proportions of three gas products (hydrogen-rich coke oven gas, CO-rich gas and hydrogen) of the gasification island2The synthesis reaction of CO is new gas, thereby meeting the production requirements of different alternative fuels/chemical products.
(3) Thirdly, compared with the traditional chemical production system, the invention is based on the method of 'coal hydrocarbon component graded gasification'. Compared with the traditional gasification method in which all reactions are carried out simultaneously in the gasification process, the coal gasification method based on the invention classifies different reactions, and based on the principle of 'component matching and graded conversion' of fuel, coal gasification is divided into three steps of coke preparation, hydrogen-rich coke oven gas production, coke gasification for preparing CO and CO conversion for producing hydrogen, and the components can be used for producing hydrogenDirected conversion with simultaneous production of H-rich2Coke oven gas, CO-rich gasification gas, and H2Three gaseous products, rather than the syngas that is typically only rich in CO as in conventional gasification. The coal gasification method based on the invention does not need oxygen to participate in the reaction, and can eliminate an air separation device. Meanwhile, the coal gasification method based on the invention has the advantages that the heat required by the units for preparing the coke, producing the hydrogen-rich coke oven gas and preparing the CO through the gasification of the coke is provided by the external combustion type combustion equipment, and the external combustion type combustion equipment can combust various fuels such as low-rank coal, biomass and the like without being limited by the type of the gasified coal.
(4) Finally, the invention realizes the energy integration and the high-efficiency utilization of the gasification island and the chemical island from two angles. One is as follows: recovering the electricity generated by the steam from the chemical island, for driving the gasifying agent CO needed by the chemical island2Compression of (2). CO separation from chemical units2The desorption pressure is low, and coke-CO is often introduced after recompression2A gasification unit. The invention uses the power generation of the steam recovery of the chemical unit to drive CO2The compressor realizes the effective integration of the energy of the gasification island and the chemical unit. The second step is as follows: and a waste heat boiler is arranged to recover the sensible heat of the high-temperature synthesis gas of the gasification island and is used for generating power by a chemical island steam turbine, so that the co-production of electric power is realized while alternative fuels/chemical products are produced.
The invention provides a production system of alternative fuels/chemical products based on 'coal hydrocarbon component staged gasification', and equipment using the method mainly comprises an external combustion unit, a heat transfer unit, a coke and coke oven gas preparation unit, a coke gasification CO preparation unit, a conversion hydrogen production unit, a chemical synthesis unit, a waste heat recovery unit and the like.
According to the system, the coke preparation unit adopts a coarse coking process of external combustion of coal, and the used fuel is divided into gasified coal and heat supply coal. The gasified coal can use all kinds of soft coal and lignite, and the heat supply coal can use all kinds of coal and other low-grade fuels.
Compared with the traditional method, the invention is based on the 'coal hydrocarbon component grading gasification' process, does not need oxygen, and saves an air separation unit for oxygen production compared with the traditional coal gasification process.
Compared with the traditional method, the invention generally does not need to arrange a self-prepared power plant, and the steam recovered from the whole plant can be used for generating power by a steam turbine, so that the power requirement of the whole plant can be met.
In the invention, the temperature of the coking unit is reduced to 600-1000 ℃ which is about 200 ℃ lower than that of the traditional coking unit, and the carbonized products are crude coke, coke oven gas, tar and the like. The gasification temperature of the coke is 900-1000 ℃, and compared with the traditional gasification endothermic reaction of high-temperature (above 1300 ℃), the irreversibility of the reaction can be greatly reduced.
In the invention, the raw materials are divided into gasified coal, heat supply coal and other fuels, the gasified coal is used for generating synthesis gas, and the heat supply coal and the other fuels are used for providing reaction heat required by heat absorption of the carbonization unit and the gasification unit.
In said invention, the carbon dioxide required by the carbon monoxide production unit is converted and CO2And (4) separating the obtained product.
In the invention, the coke preparation unit can also be a heating furnace, a soaking furnace or a calcining furnace in the metallurgical industry.
The invention has the beneficial effects that: compared with the traditional alternative fuel/chemical product production method, the new process based on 'coal hydrocarbon component staged gasification' can improve the cold coal gas efficiency of coal gasification to 83-89%, so that more coal energy is converted into chemical energy of synthesis gas, the feed gas components for chemical synthesis are improved, and more alternative fuels and chemical products are synthesized; CO produced by chemical islands2For substitution of gasifying agents for O2The organic coupling between the components of the gasification island and the chemical island is realized, the air separation can be cancelled, and the electric quantity consumption is saved, so that the low-efficiency self-contained power plant is cancelled, the power coal of the self-contained power plant is saved, and the energy conversion efficiency is further improved; the high-temperature steam recovered by the gasification island is used for generating power by a chemical island steam turbine unit,the method realizes higher system integration degree and improves the energy utilization efficiency of the system.
Drawings
FIG. 1 is a schematic diagram of a conventional alternative fuel/chemical production system;
FIG. 2 is a schematic view of an alternative fuel/chemical production system of the present invention;
FIG. 3 is a schematic diagram of a process flow for an exemplary embodiment of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings and examples.
As shown in the attached figure 2, in the alternative fuel/chemical product production system, the gasified coal 10 passes through the coke preparation unit 3 to obtain hydrogen-rich coke oven gas 11 and coke 13, and the coke 13 and CO2The gas 16 is reacted in the char gasification unit 4 to produce a CO-rich gasification gas 14. The heat required by the coke preparation unit 3 and the coke gasification unit 4 is supplied by high temperature flue gas 24 discharged by combustion of the heating coal 23 of the heating unit through the heat transfer chambers 5, 6. The air 20 exchanges heat with the combustion flue gas in the preheater 1 to form high-temperature air 22, and then the high-temperature air is introduced into the heat supply coal combustion unit 2 to react with heat supply coal 23 to produce high-temperature flue gas 24.
The CO-rich gasification gas 14 is divided into two streams after sensible heat recovery by the waste heat boiler 30, and one stream enters the water gas shift and CO shift2A separation unit 7 reacting with the steam 15 and passing through the CO2After separation, CO is formed2Gas 16 and hydrogen 17. The hydrogen 17, the hydrogen-rich coke oven gas 11 and the other CO-rich gasified gas 14 are mixed to form proper H2the/CO synthesis reaction fresh gas 18 is introduced into the chemical synthesis unit 9 to produce the alternative fuel/chemical product 19. From the water gas shift andCO2CO obtained in separation unit 72The gas is compressed by a compressor 8 and passed to a char gasification unit 4. Excess CO2The gas 34 is either evacuated or purified by a purification unit 35 and then compressed by a compression unit to perform carbon capture (a system with capture). The purification unit 35 may be based on captured CO2Terminal application mode and to CO2The requirement of purity, etc.
The steam 26 recovered from the chemical synthesis unit 9 and the steam 27, 28 recovered from the waste heat boilers 30, 31 are passed to the steam turbine and power plant unit 25 to generate power, and the resulting partial power 32 is used to drive CO2A compressor 8.
The reaction temperature of the coke preparation unit 3 is 600-1100 ℃, the reaction temperature of the carbon monoxide preparation unit is 800-1100 ℃, the main product is CO, and the temperature of the shift reaction in the hydrogen production process is about 200-500 ℃. CO 22Separation methods include Selexol, PSA, MEA, etc.
The invention is further illustrated with reference to the following figures and examples.
Comparative example:
fig. 3 is a typical process flow of an alternative fuel/chemical production system based on staged gasification of the hydrocarbon components of coal. The process flow is used to produce alternative fuel natural gas. The gasified coal 10 passes through a coke making unit to obtain coke oven gas 11 and coke 13, and the coke 13 and CO2The gas 16 reacts to produce a CO-rich gasification gas 14. The heat required by the coke making unit and the coke gasification unit is provided by the fuel coal combustion of the heat supply unit. The coke oven gas 11 is subjected to heat recovery and cooling, enters a desulfurization unit to remove sulfur content, and is compressed to about 23 bar. The CO-rich gasified gas 14 enters a water gas conversion unit after heat recovery. The CO in the gasification gas 14 reacts with the steam in the shift unit to form CO2And H2And the gas after the shift reaction enters a decarburization unit after heat recovery and condensation. In the decarbonization unit, the CO is removed2One part is used for gasifying coke, and the rest is emptied or compressed for carbon capture (belt)CO2A trapped system). CO-rich gasified gas and decarbonized H-rich gas2Mixing the synthetic gas with the purified coke oven gas to obtain H2the/CO is about 3.0, and the reaction fresh gas enters a methanation synthesis unit after being preheated to 300 ℃ to prepare a natural gas product. To control the methanation reactor temperature (the methanation reactor temperature should not exceed 700 ℃ C. to ensure catalyst activity and prevent severe carbon deposition), a portion (about 75%) of the unreacted gas from the first stage reactor is compressed and recycled to the first stage reactor. And introducing high-temperature steam prepared by heat recovery of the high-temperature coke oven gas and heat recovery of the methanation unit into a steam turbine unit for power generation.
Wherein the operating conditions of the combustion unit are: the pressure in the furnace is micro-positive pressure, the temperature of the flue gas discharged from the furnace is 1400-1700 ℃, and the adjustment is moderate according to the heat exchange period. The combustion exhaust gas temperature is 140 ℃. The temperature of the coke making unit and the coke gasification unit is 1000 ℃, the carbon conversion rate of the coke gasification unit is 0.99, and the heat exchange loss in the carbonization process and the carbon monoxide production unit process is about 14%. The operating temperature of the water gas shift unit is 250 ℃, the methanation unit is an adiabatic reactor, the operating temperature of the reactor is 200-700 ℃ in consideration of the characteristics of the catalyst, and the temperature of the first-stage methanation reactor is controlled to be 700 ℃. The pressure of the steam heat recovery was set at 120bar/30bar/8bar and the temperature was 535 ℃/430 ℃/290 ℃.
The parameters of the main streams of the production process are shown in table 1 and the properties are shown in table 2, based on 1kg of feed coal input. The raw material coal includes gasified coal and heat-supplying coal of the gasification unit. The power coal refers to coal consumed by self-contained power plants. In order to ensure the reasonability of comparison, the traditional coal methanation unit and the cascade gasification methanation unit have the same operation parameters, the unreacted gas circulation multiplying power of the synthesis unit is the same, and the minimum temperature difference of each heat exchanger of the methanation unit is basically the same. To the carbon dioxide with CO2The capture process adopts 10 stages of interstage cooling compression to compress CO2Compression was carried out to 100 bar.
Table 1 examples main logistic parameters
TABLE 2 System Performance Table
Raw coal comprises gasified coal and heat-supplying coal.
CO is introduced2Compression was carried out to 100 bar. The new system has 20% carbon capture rate, and the traditional system has about 66% carbon capture rate.
As can be seen from Table 2, the efficiency of natural gas production (SNG lower heating value/lower heating value of raw coal) for the new system based on "staged gasification of the hydrocarbon components of coal" is as high as 65.8%, approximately 8.5 percentage points higher than for the conventional system. The new system not only has high natural gas production efficiency, but also can generate about 1.7% more power than the traditional system. If the system implements CO2Capture, requiring consumption of large amounts of CO2Work of compression, for entrained CO2For the new system of capture, about 1.1% of the power is used for CO2Compressing; and for the band CO2In the conventional system for trapping, the by-product power cannot satisfy the requirement of CO2Compression, insufficient power needs to be provided by the self-contained power plant, resulting in a drop in natural gas production efficiency of the conventional system to 53.3%. Table 3 lists the system certain laws and balances.
For the traditional coal gasification system, the air separation unit and the gasification island oxygen compressor have the largest power consumption, which accounts for about 55-64% of the power consumption of the whole plant; if carrying CO2Capture of CO2The compression work is about 30%. Compared with the traditional gasification, the coal gas making system for 'coal hydrocarbon component staged gasification' cancels an air separation and oxygen compression unit, so the power consumption of the whole plant is higher than that of the traditional gasificationThe coal gas system is about 28.0-50.0% lower. The power consumed by the improved system before gas conversion compression is obviously reduced, so the total power output of the system is increased.
TABLE 3 System Performance Table
The invention provides a coal hydrocarbon component grading gasification-based alternative fuel/chemical product production system which has the following characteristics: 1. using chemical island conversion units and CO2Separation of CO produced by the unit2Gas is used for gasifying the gasification island coke, thereby eliminating water gas shift and CO of the gasification island2The separation unit reduces energy consumption and investment; 2. mixing the hydrogen-rich coke oven gas, the CO-rich gasified gas and the hydrogen obtained from the gasification island according to a certain proportion to obtain proper H2The synthesis reaction fresh gas with the ratio of/CO meets the production requirement of alternative fuels/chemical products, and realizes the component-to-mouth cascade utilization of effective components; 3. high-temperature steam obtained by recovering sensible heat of coke oven gas and gasified gas is used for power generation of a chemical island steam turbine, and one part of electric power generated by the chemical island is used for a gasification agent CO2The energy utilization and high-efficiency integration of the gasification island and the chemical island are realized. The invention realizes the coupling between the staged gasification of the hydrocarbon components of the coal and the production of the traditional alternative fuel/chemical products by the three means.
Meanwhile, the invention adopts a 'coal hydrocarbon component grading gasification' method, compared with the traditional process, the gasification method is characterized in that: 1. the coal gasification unit adopts a coke making unit, a coke gasification unit and CO2The preparation unit has three parts, realizes the directional gasification of coal components and can respectively obtain the coal rich in H2Coke oven gas rich in H2And a CO-rich gasified gas, thereby enabling production of a gas having a wide range of H2The chemical synthesis reaction of CO is carried out to obtain new gas; 2. with CO2The air separation unit is cancelled for gasifying agent, thereby greatly reducing the power consumption of the whole plantAnd the investment can be reduced; 3. the temperature of the shift reaction is about 200-400 ℃, so that the irreversible loss of the reaction is reduced; 4. the fuel is divided into heat supply coal and gasified coal, the gasified coal can use lignite and bituminous coal, the heat supply coal has no requirement on coal types, and therefore the whole gasification process can use all coal types.
In conclusion, the alternative fuel/chemical product production system based on coal hydrocarbon component staged gasification has the advantages that the energy conversion efficiency is greatly improved, an air separation device is omitted, the investment cost is greatly reduced, and all coal types are suitable, so that the system is very practical and promising.
The above description is only exemplary of the present invention and should not be taken as limiting the invention, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. A production system of alternative fuel/chemical products comprises a gasification island and a chemical island, wherein the gasification island comprises a burner, a coke preparation unit and a coke gasification unit, hot coal and preheated high-temperature air are combusted in the burner to generate high-temperature flue gas, then the high-temperature flue gas is fed into the coke preparation unit and the coke gasification unit, the coke preparation unit prepares the gasified coal into coke, the coke is fed into the coke gasification unit, hydrogen-rich coke oven gas prepared by the coke preparation unit and CO-rich gasified gas prepared by the coke gasification unit are fed into the chemical island, and the production system is characterized in that,
the chemical island comprises a water gas shift unit and CO2A separation unit and an alternative fuel production/chemical synthesis unit, wherein,
the CO-rich gasified coal gas prepared by the coke gasification unit in the gasification island is divided into two paths after heat recovery by a waste heat boiler, and one path is introduced into the water gas shift unit to react with water vapor to generate CO2Mixture of gas and hydrogen, then said CO2The mixed gas of gas and hydrogen is passed through the described CO2Separation unit for separation into CO2Gas and hydrogen, and the other path of CO-rich gasified gas and the CO2The hydrogen separated by the separation unit and the hydrogen-rich coke oven gas prepared by the coke preparation unit and subjected to heat recovery by another waste heat boiler are mixed in proportion to form H2The synthesis reaction new gas of the CO is introduced into the alternative fuel production/chemical synthesis unit to produce alternative fuel/chemical products;
- -said CO2CO separated by a separation unit2The gas is divided into two paths, one path is through CO2The compressed coke is introduced into the coke gasification unit in the gasification island, and the other path is directly emptied or passes through CO2After being purified by the purification unit, the carbon is trapped by compressing the carbon by the compression unit;
the steam recovered by the alternative fuel production/chemical synthesis unit and the steam recovered by each waste heat boiler in the gasification island are converged and then introduced into a steam turbine and power generation equipment unit for power generation, and part of the obtained power is used for driving the CO2The compressor realizes energy integration between the gasification island and the chemical island; the waste heat boilers arranged in the gasification island are used for recovering the sensible heat of the high-temperature synthesis gas of the gasification island and generating power by a chemical island steam turbine, so that the co-production of electric power is realized while alternative fuels/chemical products are produced;
wherein,
the reaction temperature of the coke preparation unit is 600-1100 ℃, the reaction temperature of the coke gasification unit is 800-1100 ℃, and the temperature of the shift reaction in the hydrogen production process by the water gas shift unit is 200-500 ℃.
2. The alternative fuel/chemical product production system according to claim 1, wherein the alternative fuel/chemical product production unit is a methanation synthesis unit, the methanation synthesis unit includes a plurality of stages of methanation reactors, wherein a majority of unreacted gas discharged from a first stage methanation reactor is compressed and then recirculated into the first stage methanation reactor, and the rest of unreacted gas is cooled and then introduced into a next stage methanation reactor.
3. The alternative fuel/chemical production system of claim 2, wherein the hydrogen-rich coke oven gas produced by the coke making unit is heat recovered and cooled, then passed to a desulfurization unit to remove sulfur, and compressed, and then mixed with the CO-rich gasification gas and the CO2The hydrogen separated by the separation unit is converged to synthesize the new reaction gas.
4. The alternative fuel/chemical production system of claim 1 wherein said CO2CO of a separation unit2The separation mode includes various CO2Separation methods, including but not limited to Selexol, PSA, MEA methods; removing CO required for coke gasification2，CO2Excess CO obtained in the separation unit2Evacuation or compression followed by carbon capture.
5. The alternative fuel/chemical production system of claim 1 wherein said gasified coal types include various types of lignite, bituminous coal, anthracite, said heat-supplying coal is all types of coal, and said coke is all types of coke, including but not limited to metallurgical coke.
6. The alternative fuel/chemical product production system of claim 1 wherein said chemical synthesis comprises a plurality of chemical synthesis processes, including methane, hydrogen, methanol, dimethyl ether, synthetic oil chemical synthesis processes; the synthesis of each chemical product comprises a plurality of production processes, and is not limited to a certain process; the output products are various chemical products and alternative fuels, including but not limited to methane, hydrogen, methanol, dimethyl ether, synthetic oil.
7. The alternative fuel/chemical production system of claim 1 wherein the energy input to the burner is a plurality of fuels including but not limited to coal and biomass.
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