CN102559269B - Method for combining coal gasification process and vapor turbine power generation process - Google Patents
Method for combining coal gasification process and vapor turbine power generation process Download PDFInfo
- Publication number
- CN102559269B CN102559269B CN201210050209.XA CN201210050209A CN102559269B CN 102559269 B CN102559269 B CN 102559269B CN 201210050209 A CN201210050209 A CN 201210050209A CN 102559269 B CN102559269 B CN 102559269B
- Authority
- CN
- China
- Prior art keywords
- water
- steam
- temperature
- synthetic gas
- coal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
Landscapes
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The invention discloses a method for combining a coal gasification process and a vapor turbine power generation process, which comprises: cooling high-temperature mixture discharged from a coal gasification furnace after reaction by using water, using high-temperature and high-pressure vapor generated in a Rankine circulation for generating power, removing water and slag from the mixture obtained after reaction to obtain synthetic gas, expanding the synthetic gas to reduce the pressure of the synthetic gas, cooling the normal-temperature cooling water, and allowing the cooled cooling water into a condensator in the Rankine circulation as a coolant for cooling exhaust gas. When the method is used, the power generation efficiency of the Rankine circulation is improved.
Description
The application is divisional application, and the application number of its original bill application is 201010258734.1, the applying date is on August 20th, 2010, denomination of invention is " coupling process of coal gasifying process and steam turbine generation technique ".
Technical field
The present invention relates to the Poly-generation field of coal, being specially with coal is the pneumoelectric coproduction field of raw material.
Background technology
Current, Coal Gasification Technology in China widespread use, but is confined to coal chemical technology substantially, to obtain tangible Chemicals.In order to improve energy efficiency, current development trend is combined with generation technology Coal Gasification Technology, namely carries out so-called pneumoelectric coproduction.Take coal as raw material, co-production synthesis gas, electricity and hot.Wherein synthetic gas can combustion power generation further, or is processed into Chemicals (as synthetic ammonia, methyl alcohol, dme, liquid fuel etc.) further.Chemical process and electrical production organically combine by such pneumoelectric joint process, achieve huge Social and economic benef@.
Current Coal (syngas) polygeneration technique, mainly rest on gasification product stream to import in each relatively independent follow-up system and carry out coproduction, such as the synthetic gas produced in coal gasification course is imported as fuel in power generation system, or this synthetic gas is imported in follow-up system for methanol synthesis for the synthesis of methyl alcohol etc.Wherein coal gasifying process and electrification technique as well as or methanol synthesizing process are relatively independent, and only contact by product flow stock between them, be relatively independent between each technique of energy.
Another kind of coal gas Electricity Federation production art is that integrated gasification combined cycle plants (is called for short IGCC, lower same), in this technique, the oxygen that coal after process and air separation unit come generates synthetic gas in vapourizing furnace, the sensible heat of synthetic gas carrys out heating water to produce steam by indirect heat exchange, and this steam can be used for driving steam turbine generation.Synthetic gas is after clean unit purification, and enter gas turbine combustion with generating, the heat of combustion tail gas reclaims and produces steam in waste heat boiler, and this steam also can be used for driving steam turbine generation.
Steam turbine generating uses the thermodynamic process based on Rankine circulation usually.Rankine circulation is a kind of steam-electric power circulation well known to those skilled in the art, and the schema of typical Rankine circulation as shown in Figure 2, is summarized as follows:
Water enters boiler by service pump adherence pressure, and be then heated into after steam through boiler and enter continuation heating in superheater, its temperature is raised further, and (it is continue raised temperature thus increase efficiency further that its effect mainly contains two: one; Two is become unsaturation steam (being called dry steam) from saturation steam (being called wetting vapour).The total heat sucked in this heating and superheating process is Q.Then, make dry steam external work done Ws of adiabatic expansion in engine (steamer or steam turbine), the steam (being called exhaust steam) after cooling of expanding enters condenser again and is condensed into water, releases heat.Water of condensation sends into boiler by service pump again, completes a circulation.
Desirable Rankine circulation also can describe with temperature-entropy diagram (T-S figure) as shown in Figure 3.The theoretical merit that steam is external done is equivalent to the area that in Fig. 3, curve 1 → 2 → 3 → 4 → 5 → 6 → 1 surrounds.Heat absorption (1 → 2 → 3 → 4) wherein in circulation and exothermic process (5 → 6) are isobaric process, and expansion (4 → 5) and the water of condensation boost process (6 → 1) of steam are isoentropic process.
About the detailed introduction of Rankine circulation, refer to " Modern Coal transforms the practical pandect with Coal Chemical Industry New Technologies ", chapter 9, the 6th section, steam integrated coal gasification combined cycle, Liao Hanxiang edits, 2004, and " integrated gasification combined cycle thermoelectric oil multi-production process technical characterstic and application ", Chen Chongliang, Yuan Longjun, coal engineering, 11 phases in 2008.
As seen from Figure 2, steam turbine generating mainly comprises steam turbine generation, and steam cools, and pump pressurization returns a few part.A desirable Rankine circulation, its thermo-efficiency depends on the temperature and pressure of endothermic process and exothermic process.The generating efficiency of steam turbine depends on net work Ws (the Ws=Δ H=H of circulation
5-H
4) with the ratio of Q initially being supplied heat and Fig. 2 by the external world.
The thermo-efficiency of whole Rankine circulation is:
η＝(H
4-H
5)/(H
4-H
1)
Wherein H
4, H
5, H
1the enthalpy entering the steam before turbine respectively shown in representative graph 2, the enthalpy of exhaust steam 5 and enter the enthalpy of high pressure water of boiler.This enthalpy is directly proportional to the temperature of steam or water substantially.
For the exothermic process carried out in steam turbines, the temperature reducing exhaust steam 5 can improve Rankine thermal efficiency of cycle, but the temperature of exhaust steam 5 can not unrestrictedly reduce, and this temperature limits by coolant temperature and condenser size.Such as, in usual steam turbine power generation process, the heat-eliminating medium of steam cooling segment often uses water coolant.The usual operating mode of water coolant is gauge pressure 0.52MPa, temperature 32 DEG C.Due to the restriction of water coolant medium, go out usually the controlling more than 32 DEG C of so-called exhaust steam 5 in the steam of turbine and Fig. 2.
For example, when using water and dry steam as Rankine circulatory mediator, the temperature entering the dry steam of steam turbine is 550 DEG C, pressure is 23MPa, and the temperature going out the exhaust steam 5 of steam turbine is 120.21 DEG C, pressure is 0.2Mpa, and in this case, thermo-efficiency is about 23% as calculated.
Obviously, above-mentioned Rankine circulation requires to provide a large amount of water coolants.
Visible, in above-mentioned IGCC technique, remain the energy utilizing the heat exchange of this product flow stock of synthetic gas and/or burning to produce and water is heated into steam, steam and then driving steam turbine generation are also relatively independent between coal gasifying process and Rankine circulation technology.Namely the generating efficiency of Rankine circulation is only subject to the impact of the temperature of produced steam, and coal gasifying process does not directly affect the generating efficiency of Rankine circulation.In other words, above the technique that gasification is combined with steam turbine generation only be make use of by the steam produced in coal gasification course, namely only by the steam of the generation in coal gasification course, coal gasifying process and steam turbine generation technique are contacted, the leeway that energy degree of integration and technique degree of integration are all still improved.
The present invention provides a kind of from process flow stock and energy point of view, the coupling process of the coal gasifying process that degree of integration is higher and steam turbine generation technique.
Summary of the invention
The invention provides the coupling process of a kind of novel coal gasifying process and steam turbine generation technique, it comprises the following steps:
A makes coal react with water and optional oxygenant generating gasification in vapourizing furnace, thus produces and comprise mixture after the reaction of synthetic gas;
Mixture after described reaction imports in interchanger and carries out indirect heat exchange with water by b, and water is generating steam by heating, and after described reaction, mixture is cooled obtains mixture after cooled reaction;
The steam generated in step b is introduced and is carried out expansion work in steam turbine and generate electricity by c, and this steam becomes exhaust steam because of expansion work, the temperature and pressure of wherein this exhaust steam and the vapor phase in step b reduce than all;
D dewaters slagging-off to obtain synthetic gas, then by this synthetic gas expansion step-down to mixture after the cooled reaction in step b;
Synthetic gas after the expansion step-down of e steps d carrys out water coolant, and makes the exhaust steam of the obtained water through cooling and step c carry out heat exchange, thus described exhaust steam is become liquid water;
F by from step e liquid water pressurization after send into step b interchanger in with described reaction after mixture carry out heat exchange, to regenerate described steam.
Accompanying drawing explanation
Fig. 1 is the indicative flowchart of a kind of thermoelectricity gas joint process of the prior art.
Fig. 2 is the indicative flowchart of Rankine circulation.
Fig. 3 is the temperature-entropy diagram (T-S figure) of Rankine circulation.
Fig. 4 is the indicative flowchart of method of the present invention.
Embodiment
In step a of the present invention, coal is reacted with water and optional oxygenant generating gasification in vapourizing furnace, thus produce and comprise mixture after the reaction of synthetic gas.Above-described coal comprises bituminous coal, hard coal, brown coal, mud coal, biomass or its mixture.The particle diameter of coal is less than 1920 microns, and preferable particle size is less than 100 microns.Wherein said water is be in water that is subcritical or supercritical state.Oxygenant can be oxygen, oxygen-rich air, air or hydrogen peroxide or their two or more mixture any.Optionally add oxygenant, if the oxygenant words added, then its add-on can be the 10-60% of ature of coal amount.Coal and water and optional oxygenant generating gasification are reacted, generate the multiple reaction product comprising synthetic gas, also generate lime-ash simultaneously, unreacted reactant (as unreacted coal, unreacted water and unreacted other oxygenant completely completely completely) etc. completely is also remained in reacted system, they mix outflow vapourizing furnace, the material flowing out vapourizing furnace are referred to as the rear mixture of reaction.A kind of specific embodiments of step a is that coal and water are mixed with coal water slurry, and water coal slurry concentration (butt coal massfraction) is generally 10-70%, preferred 20-50%.Stablizer and a certain proportion of catalyzer can also be added in process for preparation.The add-on of catalyzer can be the 2-20% of quality of pc.Catalyzer includes but not limited to the oxyhydroxide of basic metal or alkaline-earth metal, basic metal or alkaline earth salt or their mixture, such as K2O, Na
2o, CaO, MgO, NaOH, KOH, Ca (OH)
2, Mg (OH)
2, K
2cO
3and Na
2cO
3, or the mixture be made up of them.Send in vapourizing furnace by after such coal water slurry preheating pressurization, under the subcritical state that vapourizing furnace is in water or supercritical state, the subcritical state of wherein said water refers to that temperature pressure more than the atmospheric boiling point of water and below the critical temperature of water is make water remain liquid pressure, the supercritical state of described water refer to absolute pressure at more than 22.1MPa and temperature more than 374 DEG C.Coal reacts with water generating gasification in this vapourizing furnace, generates synthetic gas.Optionally can also pass into oxygenant such as oxygen, oxygen-rich air, air or hydrogen peroxide or their two or more mixture any in vapourizing furnace, then coal generates synthetic gas with water and oxidant reaction in this vapourizing furnace.It is worthy of note, this oxygenant is optional interpolation, and namely this oxygenant can add and also can not add.But preferably add oxygenant, because oxygenant provides except a part of synthetic gas except also reacting with coal, the more important thing is, because the gasification reaction that coal and subcritical water or supercritical water occur absorbs heat, coal and oxidant reaction are released heat and then can be used for maintaining the temperature in vapourizing furnace.If do not add oxygenant, then in order to maintain gasifier temperature, indirect heating equipment such as electric heating cover etc. is needed to heat to maintain the temperature of vapourizing furnace to vapourizing furnace.
In step b of the present invention, mixture after described reaction is imported in interchanger and carries out indirect heat exchange with water, water is generating steam by heating, and after described reaction, mixture is cooled obtains mixture after cooled reaction, the absolute pressure of wherein said steam is more than 15MPa, and temperature is more than 200 DEG C.The steam be within the scope of above temperature and pressure is called high temperature and high pressure steam herein.The actual temp of this steam and pressure specifically can be selected in above scope according to the needs of the processing condition of Rankine circulation, and such as in a preferred embodiment, absolute pressure can be 15MPa and temperature is 400 DEG C or higher.The water that wherein rear mixture carries out heat exchange with reaction is the pressurized water after pump pressurizes.Wherein said interchanger can be any suitable interchanger for indirect heat exchange, such as shell and tube heat exchanger, finned heat exchanger etc., and type and the concrete structure of these interchanger well known to a person skilled in the art, repeats no more here.Due to leave vapourizing furnace reaction after the temperature of mixture very high, therefore by reclaiming its sensible heat with water heat exchange, this liquid water can be transformed into high temperature and high pressure steam by this.In one embodiment, described high temperature and high pressure steam is that temperature is 374-700 DEG C and absolute pressure is the steam of 22.1-40MPa.In one embodiment, this high temperature and high pressure steam can for being suitable for any temperature and pressure of Rankine circulation.Obviously, this interchanger serves boiler in the Rankine circulation shown in Fig. 2 and the effect of superheater.
In step c of the present invention, introduced by the steam generated in step b and carry out expansion work in steam turbine and generate electricity, this steam becomes exhaust steam because of expansion work, wherein the temperature and pressure of this exhaust steam and the vapor phase in step b are than all reducing.In one embodiment, the temperature of this exhaust steam is about 25 DEG C-30 DEG C, and absolute pressure is 0.0032-0.0042MPa.It is worthy of note, exhaust steam is still in steam condition.
In steps d of the present invention, slagging-off is dewatered to obtain synthetic gas to mixture after the cooled reaction in step b, then by this synthetic gas expansion step-down, obtains low-temp low-pressure synthetic gas thus, wherein said low temperature is less than 2.6 DEG C, and low pressure is below 2MPa.Make synthetic gas carry out above-mentioned expansion pressure reduction by bloating plant, such bloating plant comprises pressure drop capillary tube, dropping valve, decompressor etc.More than make the method and apparatus of gas expansion step-down all well known to a person skilled in the art, do not repeat them here.Such expansion pressure reduction also causes synthetic gas temperature to reduce, such as, the temperature of synthetic gas can be down to about 0 DEG C.As more generally principle, the temperature of this synthetic gas can be down to the temperature lower than the exhaust steam of step c.
In step e of the present invention, carry out water coolant with the synthetic gas after the expansion step-down of steps d, and make the exhaust steam of the obtained water through cooling and step c carry out heat exchange, thus described exhaust steam is become liquid water.In this step e, first water coolant is carried out with the synthetic gas after expansion step-down, this can carry out in interchanger, reversible flow heat exchange also can and flow heat exchange, preferred countercurrent flow, cooled water can be the water under normal temperature, the preferably conventional in the prior art water coolant for cooling exhaust steam, its temperature is generally about 32 DEG C, and as previously mentioned, synthetic gas temperature after expansion step-down generally can be down to about 0 DEG C, therefore by heat exchange in interchanger, the temperature of this water can be reduced further, such as be reduced to 20 DEG C, the own temperature while of water-cooled is then slightly promoting by the synthetic gas after step-down that expands, then synthetic gas leave condenser enter follow-up separating unit or deliver to gas turbine combustion generating.Then make the exhaust steam of the obtained water through cooling and step c carry out heat exchange, thus described exhaust steam is become liquid water, this can carry out within the condenser.This condenser is an interchanger in essence.The exhaust steam of step c and the water through cooling can carry out indirect heat exchange or direct mixed heat transfer wherein, preferred indirect heat exchange.Exhaust steam is condensed into liquid water.In this step, due to employ than in common Rankine circulation for the water coolant that the temperature of cooling water cooling exhaust steam is lower, therefore can the temperature of the exhaust steam in step c be set lower, and then improve generating efficiency.
In step f of the present invention, by from step e liquid water pressurization after send into step b interchanger in with described reaction after mixture carry out heat exchange, to regenerate described steam.Be forced through pump to carry out, preferably this liquid water be heated to more than absolute pressure 15MPa.Regenerated high temperature and high pressure steam by mixture heating after the reaction of the high temperature from vapourizing furnace after this liquid water enters the interchanger of step b, this high temperature and high pressure steam is used for carrying out next round Rankine circulation.
Advantage of the present invention is as follows:
The coupling process of coal gasifying process of the present invention and steam turbine generation technique makes the energy efficiency of system be improved.First, the thermal source in Rankine circulation takes from the Exposure degree of the synthetic gas after gasification reaction, does not need external heat source, this eliminates conventional boiler and superheater.Secondly, adopt the cooled water of low-temp low-pressure synthetic gas after being inflated step-down using the water of 32 DEG C replacing general Rankine circulation conventional as the heat-eliminating medium of condenser, because this temperature through water coolant is lower than normally used temperature of cooling water 32 DEG C, therefore can the temperature of the exhaust steam going out steam turbine be set lower, this is equivalent to 5 in T-S figure and to move down at 6 two, therefore add the area that curve 1-2-3-4-5-6-1 surrounds, represent that the theoretical merit that steam externally does is larger, and then add generating efficiency.Again, follow-up sepn process is also helped after synthetic gas expansion step-down.
Embodiment
Method of the present invention is illustrated by following non-limiting example.
With reference to Fig. 4, the catalytic gasification occurred for bituminous coal and supercritical water.Coal grinds the coal dust made granularity and be less than 150 microns through pulverizing, with catalyst n a
2cO
3it is the coal water slurry of 40% that (consumption is 10% of quality of pc) and water are prepared into coal dust butt concentration.The process of preparation coal water slurry does not draw in the diagram.Coal water slurry is through pressurization, and preheating reaches 23MPa, and 550 DEG C enter vapourizing furnace, passes into oxygen in vapourizing furnace simultaneously.Part coal water slurry and the oxygen reaction added in vapourizing furnace, by temperature increase to 650 DEG C.In the supercritical state, coal and water react under the effect of catalyzer, generate the synthetic gas being rich in methane.The main component of synthetic gas is methane, carbon monoxide, carbonic acid gas, hydrogen etc.Go out vapourizing furnace product and comprise synthetic gas, supercritical water and the rear residue of reaction.This product and the 23MPa water heat exchange in First Heat Exchanger from force (forcing) pump, produce high temperature and high pressure steam, become exhaust steam after entering steam turbine expansion power generation, it is 0.0032MPa that this exhaust steam can be controlled in pressure, temperature is 25 DEG C, and exhaust steam enters condenser condenses and becomes liquid water.Synthetic gas after heat exchange enters clean unit, by synthetic gas and water, slag is separated, synthetic gas after separation cools the temperature to 0 DEG C through overexpansion step-down, then be the water quench to 20 DEG C of 32 DEG C in the second heat exchanger by the temperature in general Rankine circulation with it, this synthetic gas can enter subsequent separation process or enter follow-up gas turbine combustion generating afterwards, and the water through cooling is then used as the heat-eliminating medium of above-mentioned condenser, so that exhaust steam is condensed into water.The water carrying out condenser turns back in First Heat Exchanger Yu from mixture after the reaction of the high temperature of vapourizing furnace and carries out heat exchange, to regenerate high temperature and high pressure steam after pump pressurization.
Although describe method of the present invention in conjunction with specific embodiment, one skilled in the art will recognize that, various change can also be carried out to the present invention, and not deviate from the protection domain defined in appended claim.Such as, although Rankine circulation is using water and steam as working medium in the present invention, obviously, the present invention is also applicable to the Rankine circulation making working medium with other material such as carbonic acid gas, organic fluid such as isoparaffin etc.Those skilled in the art have the ability the concrete technology parameter regulated according to adopted specific works medium in the present invention, are implemented to make the present invention.
Claims (5)
1. a coupled system for coal gasifying process and steam turbine generation technique, comprising:
Vapourizing furnace, coal reacts mixture after the reaction producing and comprise synthetic gas with water or with water and oxygenant generating gasification in vapourizing furnace, and described water is be in water that is subcritical or supercritical state;
Force (forcing) pump;
First Heat Exchanger, after reaction, mixture produces high temperature and high pressure steam with water heat exchange in this interchanger of pressurizeing through force (forcing) pump;
Steam turbine, the high temperature and high pressure steam produced enters and carries out expansion work in this steam turbine and generate electricity, and this steam becomes exhaust steam;
Clean unit, to mixture after the cooled reaction in described interchanger dewater slagging-off after obtain synthetic gas;
Bloating plant, to this synthesis gas expansion step-down;
Second interchanger, in the second heat exchanger, carrys out water coolant with the synthesis gas after expansion step-down, and this synthetic gas enters follow-up gas turbine combustion generating afterwards; And
Condenser, exhaust steam and the water through cooling obtained carry out direct or indirect heat exchange, described exhaust steam liquefy water within the condenser.
2. coupled system according to claim 1, the synthetic gas leaving condenser enters follow-up separating unit or delivers to gas turbine combustion generating.
3. coupled system according to claim 1, described bloating plant comprises pressure drop capillary tube, dropping valve, decompressor.
4. coupled system according to claim 1, described First Heat Exchanger is the interchanger for indirect heat exchange.
5. coupled system according to claim 1, also comprises the indirect heating equipment maintaining gasifier temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210050209.XA CN102559269B (en) | 2010-08-20 | 2010-08-20 | Method for combining coal gasification process and vapor turbine power generation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210050209.XA CN102559269B (en) | 2010-08-20 | 2010-08-20 | Method for combining coal gasification process and vapor turbine power generation process |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102587341A Division CN102373092B (en) | 2010-08-20 | 2010-08-20 | Coupling method of coal gasification technology and steam turbine generating technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102559269A CN102559269A (en) | 2012-07-11 |
| CN102559269B true CN102559269B (en) | 2015-03-04 |
Family
ID=46405897
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210050209.XA Active CN102559269B (en) | 2010-08-20 | 2010-08-20 | Method for combining coal gasification process and vapor turbine power generation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102559269B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102518489B (en) * | 2012-01-06 | 2016-08-03 | 新奥科技发展有限公司 | Electricity-generating method, the device generated electricity for gasified production of energy products and heat |
| CN106701203A (en) * | 2017-01-13 | 2017-05-24 | 厦门大学 | Biomass gasification power generation waste heat recycling system based on organic Rankine cycle |
| CN107165688A (en) * | 2017-05-19 | 2017-09-15 | 北京迈未科技有限公司 | The device and method that a kind of utilization combustion gas and Steam Combined generate electricity |
| CN113316682B (en) * | 2018-11-07 | 2024-05-14 | 南非大学 | Waste plastic power generation process and system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1053898A (en) * | 1990-02-09 | 1991-08-21 | 三菱重工业株式会社 | High-temperature reductibility gas process for purification and gasifying combined generating apparatus |
| CN1102872A (en) * | 1993-07-06 | 1995-05-24 | 福斯特·惠勒发展公司 | Combined-cycle poser generation system using a coal-fired gasifier |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0598908A (en) * | 1991-10-09 | 1993-04-20 | Mitsubishi Heavy Ind Ltd | Power generating device utilizing combustion gas of combustion furnace |
| JPH06272516A (en) * | 1993-03-16 | 1994-09-27 | Mitsui Eng & Shipbuild Co Ltd | Hydrogen oxygen premixed combustion power generation |
-
2010
- 2010-08-20 CN CN201210050209.XA patent/CN102559269B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1053898A (en) * | 1990-02-09 | 1991-08-21 | 三菱重工业株式会社 | High-temperature reductibility gas process for purification and gasifying combined generating apparatus |
| CN1102872A (en) * | 1993-07-06 | 1995-05-24 | 福斯特·惠勒发展公司 | Combined-cycle poser generation system using a coal-fired gasifier |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102559269A (en) | 2012-07-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102518489B (en) | Electricity-generating method, the device generated electricity for gasified production of energy products and heat | |
| CN102373097B (en) | Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process | |
| US8715379B2 (en) | Advanced ASU and HRSG integration for improved integrated gasification combined cycle efficiency | |
| CN106414330B (en) | The technique for producing ammonia and its derivative, especially urea | |
| CA2267687C (en) | Turbine plant | |
| RU2534077C2 (en) | Method of combined production of synthesis-gas and electric energy | |
| Xin et al. | Thermodynamic analysis of a novel zero carbon emission coal-based polygeneration system incorporating methanol synthesis and Allam power cycle | |
| WO2011115739A1 (en) | System for heat integration with methanation system | |
| JP2008535768A (en) | Integrated gasification and ammonia production | |
| CA2715493C (en) | Methods and systems for integrated boiler feed water heating | |
| CN102559269B (en) | Method for combining coal gasification process and vapor turbine power generation process | |
| JPH1068329A (en) | Manufacture of synthesis gas and energy in combination | |
| EP2905433B1 (en) | Method and system for producing liquid fuel and generating electric power | |
| CN102373090B (en) | Coal gasification technology and steam turbine power generation technology coupled method | |
| CN102373091B (en) | Method for coupling coal gasification process and steam turbine power generation process | |
| CN102234547A (en) | Water gas shift reactor system for integrated gasification combined cycle power generation systems | |
| CA2734840C (en) | Co-production of synthesis gas and power | |
| CN102373099B (en) | Method for coupling coal gasification process and steam turbine power generation process | |
| CN102373096B (en) | Coupling method of coal gasification technology and steam turbine generating technology | |
| CN102373092B (en) | Coupling method of coal gasification technology and steam turbine generating technology | |
| CN102373098B (en) | Coupling method of coal gasification technology and steam turbine generating technology | |
| CN217127311U (en) | Device for synthesizing methanol by double-carbon hydrogenation | |
| Jin et al. | A Novel Multifunctional Energy System (MES) for CO 2 Removal With Zero Energy Penalty | |
| Jin et al. | A Novel Multi-Functional Energy System (MES) for CO2 Removal With Zero Energy Penalty | |
| WO2023167922A1 (en) | Electric power co-generation for chemical and physical processes with steam utilization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |