CN102212396B - Coal gasification Fischer-Tropsch synthetic system and method with CO2 capturing function for generating fuel along with electricity - Google Patents
Coal gasification Fischer-Tropsch synthetic system and method with CO2 capturing function for generating fuel along with electricity Download PDFInfo
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- CN102212396B CN102212396B CN201110112911XA CN201110112911A CN102212396B CN 102212396 B CN102212396 B CN 102212396B CN 201110112911X A CN201110112911X A CN 201110112911XA CN 201110112911 A CN201110112911 A CN 201110112911A CN 102212396 B CN102212396 B CN 102212396B
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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]
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Abstract
The invention relates to a coal gasification Fischer-Tropsch synthetic system and method with a CO2 capturing function for generating fuel along with electricity and belongs to the technical fields of energy and environment. The system contains an air separation unit (1), a pure-oxygen pressurization airflow bed coal gasification and preliminary purification unit (2), a synthesis gas desulfurization and decarburization purification unit (3), a single-pass Fischer-Tropsch synthetic unit (4) using a Fe-based catalyst, a power generation unit (5) of a pressurization gas boiler adopting a O2/CO2 combustion technology and an ultra-supercritical steam turbine and a CO2 compression unit (6). Compared with the single-product system, the cogeneration system has the characteristics that the process flow is simple, the chemical/electricity ratio is flexible to adjust and CO2 can be captured. The system is especially suitable for the modification of the existing coal gasification Fischer-Tropsch synthetic system and the reduction of CO2 emission.
Description
Technical field
The present invention relates to a kind ofly can capture CO
2Gasification Fischer-Tropsch synthol/cogeneration system and method, belong to the fields such as energy and environment technology.
Background technology
China's hydrocarbon resources relatively lacks and coal resources are relatively abundant, the a large amount of dependence on import of crude oil, current crude oil year, import volume was above 2.0 hundred million tons, the import interdependency surpasses 50%, it mainly is used to the liquid fuels such as refining diesel oil, gasoline as can be known from the crude oil in China consumption structure, accounts for 60% of oil consumption total amount.If the crude oil import amount continues development according to nearly 10 years average growth rate, crude oil in China consumption and import interdependency will constantly increase, and the security threat that the power supply strategy is subject to also will further aggravate.In addition, the Life cycle disposal of pollutants that produces of directly burning of the liquid fuels such as these diesel oil that refine based on crude oil, gasoline also is difficult to satisfy increasingly strict environmental requirement.
Along with people to CO
2How going deep into of emission problem understanding realizes reducing discharging CO from coal-based energy resource system
2Become the focus of research.Capture in a large number at present CO
2Coal-based energy resource system and method be suggested, existing result of study shows and captures CO
2The difference of position and flow process, on impacts such as the heating power of system and economic performances obviously.From smoke evacuation, capture CO with coal power station
2Compare, adopting transformationreation to be translated into main component to synthesis gas from coal gasification is CO
2And H
2Synthetic gas, adopt then that physical cleaning or chemical purification technique are separated, concentrated and compression CO from conversion gas
2, be a kind of by the CO of extensive concern
2Trapping technique.The green coal electric energy system that " FutureGen " energy resource system that proposes such as USDOE and China Huaneng Group group propose etc.Yet above this class technological system separation of C O
2After the synthetic gas main component that obtains be hydrogen, adopt extensive hydrogen turbine generation technology still immature to it.
O
2/ CO
2Combustion technology also is one and can be used for capturing CO
2Technology.Its principal feature is to utilize CO
2Replace airborne N
2, can obtain highly purified CO behind the smoke evacuation process condensation separation liquid water
2Gas can mainly contain station boiler and IGCC etc. in applicable field.With capture CO before the employing burning
2Technology compare, this technology range of application is wider, not only can be used for existing power station and reduces discharging CO
2, but also can be used for newly building a power station.With capture CO after the employing burning
2Compare, this technology has less energy-consumption and the low-cost CO of capture
2Advantage.Compare with the air-breathing mode, adopt O
2/ CO
2Combustion technology not only is convenient to capture CO
2, the utilization ratio of raising fuel, SO
x, NO
xAlso decrease with disposals of pollutants such as heavy metals.This technology is relatively ripe, the practical operating experiences of more existing Demonstration Stations.And employing supercharging O
2/ CO
2Combustion technology can also be by improving CO in the outlet flue gas
2Concentration and pressure, reduce flue gas purifying technique equipment size and CO
2Compression power consumption.Yet, being subject to current commercial technology horizontal constraints, the IGCC system exists specific investment high, the deficiencies such as technical process complexity, simple consideration captures CO
2Will further affect its application.
The chemical industry that is coupled after the gasification of coal synthesizes the co-generation system with dynamic power, than advantages such as flexible adjustments, has caused people's concern with its total energy utilising efficiency height, simplification chemical unit flow process and change electricity.And development oil fuel substitute is an approach the stablize environmental issue that China's liquid fuel security provisions and solution petroleum base liquid fuel bring.Investigators have proposed the scheme of multiple chemicals coproduction electricity at present, such as methyl alcohol/cogeneration system scheme, and dme/cogeneration system scheme, and F-T synthol/cogeneration system scheme etc.Wherein, take synthetic gas as raw material, the liquid fuel that utilizes the F-T synthetic technology to obtain is with the obvious advantage.Its characteristics are: the sulphur in the F-T combined diesel oil, nitrogen and arsenic equal size are all lower, and the quality product of F-T synthol is better than petroleum products; 16 alkane values of F-T combined diesel oil reach 70, can be used as the allotment that branded oil is used for other oil products, can deliver to the user under the condition that does not change existing Infrastructure.And develop other fuel substitutes, and solve except needs the problems such as startup that engine reformation, combustion processes run into, operation and control, also need to solve the problems such as construction of storage, transportation and the supply system of fuel substitute.And compare with DCL/Direct coal liquefaction liquefaction technology, the ICL for Indirect Coal Liquefaction technology has that Technology is relatively ripe, and coal subject range is wide, and efficiency of carbon conversion is high, require relatively low and the advantage such as oil quality is high to reactor operating condition.
This shows, utilize the coproduction concept, research and establishment band CO
2The gasification F-T synthol that captures/cogeneration system scheme for stablizing China's fuel security provisions, improves its environmental-protecting performance, and development of coal clean and effective comprehensive utilization technique is significant.
Summary of the invention
The technical problem that (one) will solve
The object of the invention is to propose a cover and can simplify the technical process of chemical industry synthesis unit, coproduction chemicals and two kinds of products of electricity, can capture CO simultaneously
2, the major parts unit adopts the supercharging O based on current commercial technology
2/ CO
2Coal combustion gasification F-T synthesizes/cogeneration system, is specially adapted to transform complicated, high, the CO of energy consumption of existing synthesis technique flow process
2The independent gasification F-T synthesis system for the synthesis of liquid fuel that discharge capacity is large.
(2) technical scheme
Band CO of the present invention
2The system and method for the gasification Fischer-Tropsch synthol coproduction electricity that captures is characterized in that comprising following unit process: air gas separation unit, gasification and rough purification unit, synthetic gas desulfurization decarburization clean unit, F-T synthesis unit, dynamic power unit and CO
2Compressed element;
Wherein, air gas separation unit feed(raw material)inlet and air are connected, and air gas separation unit byproduct nitrogen outlet and atmosphere are connected, and air gas separation unit product oxygen outlet is divided into two branch roads; Wherein a branch road links to each other with the oxygen intake of gasification and rough purification unit, and another branch road links to each other with the vaporized chemical oxygen intake of dynamic power unit; Gasification and rough purification unit also have coal and water inlet, and the crude synthesis gas outlet of gasification and rough purification unit links to each other with the crude synthesis gas entrance of synthetic gas desulfurization decarburization clean unit; The clean syngas outlet of synthetic gas desulfurization decarburization clean unit links to each other with the new gas entrance of F-T synthesis unit, and synthetic gas desulfurization decarburization clean unit also has sulphur outlet and CO
2Outlet; The tail gas outlet of F-T synthesis unit links to each other with the fuel inlet of dynamic power unit, and the F-T synthesis unit also has the synthetic oil outlet; The exhanst gas outlet of dynamic power unit and CO
2The compressed element entrance links to each other;
Above-mentioned F-T synthesis unit is made of preheater, F-T synthesis reactor, gas-liquid separation device and the hydrogenation device for improving quality that links to each other with the gas-liquid separation device liquid-phase outlet successively, has the synthetic oil outlet on the hydrogenation device for improving quality; Above-mentioned preheater is positioned at F-T synthesis reactor outlet position, to utilize F-T synthesis reactor outlet logistics sensible heat new synthetic gas is carried out preheating;
Above-mentioned dynamic power unit comprises: the supercharging gas fired-boiler that fuel inlet links to each other with F-T synthesis unit gas-liquid separation device gaseous phase outlet, the exhanst gas outlet of supercharging gas fired-boiler is divided into two branch roads, obtains high pressure high purity gas phase CO after wherein a branch road separates liquid water through condenser
2, another branch road links to each other with the cold air entrance of mixing of supercharging gas fired-boiler through recycle compressor, and the supercharging gas fired-boiler also has oxygen intake; The live steam outlet of supercharging gas fired-boiler links to each other with supercritical turbine, condenser, water circulating pump successively, and the water inlet with the supercharging gas fired-boiler links to each other again.
The method of the synthol coproduction electricity of system of the present invention is characterized in that comprising following process:
The first step, air are separated into nitrogen and oxygen at air gas separation unit;
Second step, oxygen and coal, water are made crude synthesis gas in gasification and rough purification unit, and the crude synthesis gas main component is CO, H
2, H
2O, H
2S and CO
2, the crude synthesis gas sensible heat is used for adding the working-medium water of dynamic power system unit;
The 3rd step, crude synthesis gas are made into clean synthetic gas at synthetic gas desulfurization decarburization clean unit, and discharge byproduct S and a small amount of CO
2, clean synthetic gas main component is CO and H
2
The 4th step, clean synthetic gas are made synthetic oil and are discharged tail gas at the F-T synthesis unit; This step detailed process is as follows:
Clean synthetic gas from synthetic gas desulfurization decarburization clean unit reacts through entering the F-T synthesis reactor behind the preheater, and F-T synthesis reactor outlet logistics enters gas-liquid separation device after being preheated the device cooling;
The F-T synthesis reactor is the catalyst based slurry reactor of a kind of Fe of employing, and synthetic gas is converted into the hydrocarbon mixture that contains different carbonatomss therein;
Gas-liquid separation is carried out in the cooling logistics of preheater outlet in gas-liquid separation device, the gas-liquid separation device outlet can obtain liquid product and gas-phase product, gas-phase product acts as a fuel and links to each other with dynamic power unit gas fired-boiler fuel gas entrance, and the main component of gas-phase product is lower carbon number hydrocarbons, CO, H
2And CO
2
Above liquid product is sent into the hydrogenation device for improving quality and is made liquid fuel oil; The 5th step, tail gas are as the fuel of dynamic power unit (5), at O
2/ CO
2Produce flue gas under the condition; This step detailed process is as follows:
F-T synthesis unit gas-liquid separation device outlet gas-phase product is in the supercharging gas fired-boiler, at O
2/ CO
2Combustion-supporting and mix under the cool condition, perfect combustion and to generate main component be CO
2And H
2The flue gas of O, exhanst gas outlet are divided into two branch roads, and recirculated water is become ultra supercritical steam by flue gas heating in the supercharging gas fired-boiler;
Wherein the flue gas of a branch road obtains highly purified gaseous state CO after condenser separates liquid water
2, the flue gas of another branch road is used for mixing of supercharging gas fired-boiler after the recycle compressor supercharging cold.
Entering supercritical turbine from supercharging gas fired-boiler ultra supercritical steam out is converted into heat energy mechanical energy and further is converted into electric energy;
Condenser, the weary gas of supercritical turbine outlet is condensed into liquid water, links to each other with supercharging gas fired-boiler recirculated water entrance through water circulating pump through condenser;
The 6th step, flue gas are at CO
2Compressed element is made into the highly purified liquid phase CO of high pressure
2
Description of drawings
Fig. 1 captures CO
2Gasification Fischer-Tropsch synthol/cogeneration system process flow sheet
Fig. 2 is the process flow sheet of new system Fischer-Tropsch synthesis unit
Fig. 3 is the process flow sheet of new system dynamic generator unit
Fig. 4 is conventional Fischer-Tropsch synthesis unit process flow sheet
Fig. 5 is conventional IGCC system process figure
Fig. 6 is conventional gasification Fischer-Tropsch synthesis system process flow sheet
Number in the figure title: 1. air gas separation unit, 2. coal gasification unit, 3. synthetic gas desulfurization decarburization unit, 4. Fischer-Tropsch synthesis unit, 5. dynamic power unit, 6. CO
2Compressed element, 7. Fischer-Tropsch synthesis device, 8. preheater, 9. gas-liquid separation device, 10. CO
2The absorption tower, 11. rich or poor liquid heat exchangers, 12. CO
2Regenerator column, 13. hydrogenation device for improving quality, 14. interchanger, 15. autothermal reforming reaction devices, 16. the recycled offgas compressor, 17. supercharging gas fired-boilers, 18. steam turbine, 19. generators, 20. condenser, 21. water circulating pumps, 22. condensers, 23. recycle compressors.
Embodiment
The present invention relates to a kind of capture CO
2Gasification Fischer-Tropsch synthol/cogeneration system.The system that the present invention proposes mainly is in conjunction with the CO that adopts the catalyst based F-T building-up process of Fe
2Densification.Consist of one mainly by air gas separation unit, gasification and rough purification unit, synthetic gas desulfurization decarburization clean unit, the co-generation system scheme of F-T synthesis unit and dynamic power cell formation.Feed coal, water and produce the crude synthesis gas that obtains High Temperature High Pressure in the vapourizing furnace generating gasification reaction of coal gasification unit from the oxygen of air gas separation unit, the main component of crude synthesis gas is CO, CO
2, H
2, H
2O and H
2S.
Different from heat exchange form in the radiation recuperator of conventional coal gasification unit or the convection recuperator, cold-side fluid is the water coolant that is in ultra supercritical pressure in this co-generation system gasification unit crude synthesis gas interchanger, and the interior cold-side fluid employing of conventional coal gasification unit crude synthesis gas interchanger is high pressure water.Under the condition that does not change original crude synthesis gas interchanger heat interchanging area, the coal gasification unit of this co-generation system and rough purification unit outlet synthetic gas can be cooled to lower temperature; The high pressure low temperature crude synthesis gas that obtains from gasification and rough purification unit enters synthetic gas desulfurization decarburization clean unit, wherein H in the crude synthesis gas
2S and CO
2Separated step by step and be converted into S and CO
2, the clean synthetic gas that obtains through this unit is admitted to the F-T synthesis unit as unstripped gas.Clean synthetic gas the F-T synthesis unit by adopt Fe catalyst based once by the syrup state bed Fischer Tropsch synthetic technology.Mainly be that the catalyst based slurry attitude bed F-T of Fe is synthetic can to adapt to H in view of adopting
2The synthetic gas that/CO is lower, this process is once high by the synthetic gas transformation efficiency than fixed-bed reactor etc.And under the higher condition of synthetic gas transformation efficiency, the catalyst based effect by hydrosphere transformation adjustment synthesis gas composition of Fe is so that the F-T synthesis tail gas has CO
2Content is high, combustibles (H
2, CO, C
4-Deng lower carbon number hydrocarbons) characteristics such as the low and calorific value of content is low.Because above this F-T building-up process is when producing liquid fuel, its adjustment to synthesis gas composition is conducive to reduce the capture CO of unit
2Corresponding oxygen consumption, thus the internal system power consumption reduced.
In the dynamic power unit, once by Fischer-Tropsch process exhaust directly as the fuel (supercharging gas fired-boiler working pressure is suitable with F-T synthesis tail gas pressure) of supercharging gas fired-boiler, under the pure oxygen combustion-supporting condition from air gas separation unit, fully burning generation main component is CO
2And H
2The high temperature and high pressure flue gas of O.The flue gas that supercharging gas fired-boiler economizer is discharged is divided into two branch roads: a branch road loops back gas fired-boiler and is used for the control combustion temperature; After another branch road is condensed and separates liquid water, can obtain highly purified pressure CO
2(main component is three atomic gas to the high-temperature flue gas that the burning of supercharging gas fired-boiler produces, than N
2Have higher radiation heat transfer coefficient) heating water, the high temperature and high pressure steam of production promotes supercritical turbine and realizes generating.Because effective constituent (H in the F-T synthesis tail gas
2, CO and CH
4Deng lower carbon number hydrocarbons) content is low, adopts the supercharging gas fired-boiler by using supercharging O
2/ CO
2The amount of oxygen that combustion technology need to consume is few; F-T synthesis tail gas calorific value is low, and CO
2Content is higher, is used for the cold CO that mixes of control entrance flue gas temperature
2Internal circulating load is few, corresponding circulating flue gas compressor low in energy consumption; And supercharging O
2/ CO
2Products of combustion is mainly triatomic molecule (CO
2And H
2O), it can improve radiation heat transfer coefficient in the boiler, reduces the layout of heating surface.Consider F-T synthesis tail gas pressure high (suitable with F-T synthesis reactor working pressure), adopt supercharging O
2/ CO
2Combustion technology can separation obtain pressure CO from the gas fired-boiler smoke evacuation
2Thereby, can reduce CO
2The compression power consumption of capture process.Therefore, the supercharging gas fired-boiler that adopts of this dynamic power unit and ultra supercritical steam parameter can improve the supercharging gas fired-boiler fire with utilization ratio, reduce CO
2Compression power consumption.Pressure CO
2At CO
2Compressed element is by compression and cooling effect with the multistage centrifugal compressor of inter cooler, makes to be convenient to the liquid phase CO that transports and bury
2
In a word, compare with the per unit area yield scheme of identical output (IGCC+ shown in Figure 5 shown in Figure 6 independent F-T synthetic), this co-generation system and method have technical process simple, change/electricity than flexible adjustment, can capture CO
2Characteristics, be specially adapted to transform existing gasification Fischer-Tropsch synthesis system, and realize capturing CO
2, and this system also has advantage aspect the Technology ripening degree, and more obvious than the performance advantage under the condition at Gao Huadian.
Claims (2)
1. be with CO for one kind
2The gasification Fischer-Tropsch synthol coproduction electric system that captures, it is characterized in that: this system comprises: air gas separation unit (1), gasification and rough purification unit (2), synthetic gas desulfurization decarburization clean unit (3), F-T synthesis unit (4), dynamic power unit (5) and CO
2Compressed element (6);
Wherein, air gas separation unit (1) feed(raw material)inlet and air are connected, and the byproduct nitrogen outlet of air gas separation unit (1) and atmosphere are connected, and the product oxygen outlet of air gas separation unit (1) is divided into two branch roads; Wherein a branch road links to each other with the oxygen intake of gasification and rough purification unit (2), and another branch road links to each other with the vaporized chemical oxygen intake of dynamic power unit (5); Gasification and rough purification unit (2) also have coal and water inlet, and the crude synthesis gas outlet of gasification and rough purification unit (2) links to each other with the crude synthesis gas entrance of synthetic gas desulfurization decarburization clean unit (3); The clean syngas outlet of synthetic gas desulfurization decarburization clean unit (3) links to each other with the new gas entrance of F-T synthesis unit (4), and synthetic gas desulfurization decarburization clean unit (3) also has sulphur outlet and CO
2Outlet; The tail gas outlet of F-T synthesis unit (4) links to each other with the fuel inlet of dynamic power unit (5), and F-T synthesis unit (4) also has the synthetic oil outlet; Exhanst gas outlet and the CO of dynamic power unit (5)
2The entrance of compressed element (6) links to each other;
Above-mentioned F-T synthesis unit is made of preheater (8), F-T synthesis reactor (7), gas-liquid separation device (9) and the hydrogenation device for improving quality (13) that links to each other with the gas-liquid separation device liquid-phase outlet successively, has the synthetic oil outlet on the hydrogenation device for improving quality (13); Above-mentioned preheater (8) is positioned at F-T synthesis reactor (7) outlet position, to utilize F-T synthesis reactor (7) outlet logistics sensible heat new synthetic gas is carried out preheating;
Above-mentioned dynamic power unit (5) comprises the supercharging gas fired-boiler (17) that fuel inlet links to each other with F-T synthesis unit (4) gas-liquid separation device gaseous phase outlet, the exhanst gas outlet of supercharging gas fired-boiler (17) is divided into two branch roads, obtains high pressure high purity gas phase CO after wherein a branch road separates liquid water through condenser (22)
2, another branch road links to each other with the cold air entrance of mixing of supercharging gas fired-boiler (17) through recycle compressor (23), and supercharging gas fired-boiler (17) also has oxygen intake; The live steam outlet of supercharging gas fired-boiler (17) links to each other with supercritical turbine (18), condenser (20), water circulating pump (21) successively, and the water inlet with supercharging gas fired-boiler (17) links to each other again.
2. utilize the method for the synthol coproduction electricity of the described system of claim 1, it is characterized in that comprising following process:
The first step, air are separated into nitrogen and oxygen at air gas separation unit (1);
Second step, oxygen and coal, water are made crude synthesis gas in gasification and rough purification unit (2), and the crude synthesis gas main component is CO, H
2, H
2O, H
2S and CO
2, the crude synthesis gas sensible heat is used for adding the working-medium water of dynamic power system unit (5);
The 3rd step, crude synthesis gas are made into clean synthetic gas at synthetic gas desulfurization decarburization clean unit (3), and discharge byproduct S and a small amount of CO
2, clean synthetic gas main component is CO and H
2
The 4th step, clean synthetic gas are made synthetic oil and are discharged tail gas at F-T synthesis unit (4); This step detailed process is as follows:
Enter F-T synthesis reactor (7) reaction behind the clean synthetic gas process preheater (8) from synthetic gas desulfurization decarburization clean unit, and F-T synthesis reactor (7) outlet logistics enters gas-liquid separation device (9) after being preheated device (8) cooling;
F-T synthesis reactor (7) is the catalyst based slurry reactor of a kind of Fe of employing, and synthetic gas is converted into the hydrocarbon mixture that contains different carbonatomss therein;
The cooling logistics of preheater (8) outlet is carried out gas-liquid separation in gas-liquid separation device (9), gas-liquid separation device (9) outlet can obtain liquid product and gas-phase product, gas-phase product acts as a fuel and links to each other with dynamic power unit supercharging gas fired-boiler (17) fuel gas entrance, and the main component of gas-phase product is lower carbon number hydrocarbons, CO, H
2And CO
2
Above liquid product is sent into hydrogenation device for improving quality (13) and is made liquid fuel oil; The 5th step, tail gas are as the fuel of dynamic power unit (5), at O
2/ CO
2Produce flue gas under the condition; This step detailed process is as follows:
F-T synthesis unit gas-liquid separation device outlet gas-phase product is in the supercharging gas fired-boiler, at O
2/ CO
2Combustion-supporting and mix under the cool condition, perfect combustion and to generate main component be CO
2And H
2The flue gas of O, exhanst gas outlet are divided into two branch roads, and recirculated water is become ultra supercritical steam by flue gas heating in the supercharging gas fired-boiler;
Wherein the flue gas of a branch road obtains highly purified gaseous state CO after condenser (22) separates liquid water
2
The flue gas of another branch road is used for mixing of supercharging gas fired-boiler after recycle compressor (23) supercharging cold;
Entering supercritical turbine (18) from supercharging gas fired-boiler (17) ultra supercritical steam out is converted into heat energy mechanical energy and further is converted into electric energy;
Condenser (20), the weary gas of supercritical turbine (18) outlet is condensed into liquid water, links to each other with supercharging gas fired-boiler recirculated water entrance through water circulating pump (21) through condenser (20);
The 6th step, flue gas are at CO
2Compressed element (6) is made into the highly purified liquid phase CO of high pressure
2
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| CN105820842B (en) * | 2016-05-19 | 2018-10-09 | 中国科学院工程热物理研究所 | A kind of coal gasification supercritical CO2Cycle generating system |
| CN108977241B (en) * | 2018-08-07 | 2023-06-02 | 中国华能集团有限公司 | With CO 2 Trapped coal-fired power generation system and method |
| CN108979770B (en) * | 2018-08-27 | 2023-07-11 | 中国华能集团有限公司 | Integrated coal gasification combined cycle power generation system and method using supercritical carbon dioxide as working medium |
| CN110159370B (en) * | 2019-05-15 | 2023-12-26 | 上海发电设备成套设计研究院有限责任公司 | Coal-fired power generation system with carbon capturing device and method |
| CN111412022B (en) * | 2020-03-24 | 2021-02-09 | 西安交通大学 | Coal supercritical water gasification power generation system for controlling available energy loss and working method |
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| JPH11257094A (en) * | 1998-03-16 | 1999-09-21 | Electric Power Dev Co Ltd | Coal gasification power generation system |
| JP2004229374A (en) * | 2003-01-21 | 2004-08-12 | Hokkaido Univ | Method for mhd single high efficient power generation and system |
| CN101381627A (en) * | 2008-09-27 | 2009-03-11 | 余载强 | Side-push gas producer |
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2011
- 2011-05-04 CN CN201110112911XA patent/CN102212396B/en not_active Expired - Fee Related
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