CN102373097A - Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process - Google Patents
Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process Download PDFInfo
- Publication number
- CN102373097A CN102373097A CN2010102587182A CN201010258718A CN102373097A CN 102373097 A CN102373097 A CN 102373097A CN 2010102587182 A CN2010102587182 A CN 2010102587182A CN 201010258718 A CN201010258718 A CN 201010258718A CN 102373097 A CN102373097 A CN 102373097A
- Authority
- CN
- China
- Prior art keywords
- water
- steam
- logistics
- mixture
- 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.)
- Granted
Links
Images
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
-
- 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
Landscapes
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The invention discloses a coupling method of a coal gasification process, a residual carbon oxidation process and a steam turbine power generation process. The technology comprises the steps of: cooling a high temperature reacted mixture departing from a coal gasifier so as to obtain high temperature and high pressure steam, which is then subjected to power generation in a Rankine cycle, separating the reacted mixture so as to obtain slurry-like residual carbon and syngas, leaving the slurry-like residual carbon to complete oxidation in subcritical or supercritical water with the presence of excess oxygen, thus obtaining a mixture of carbon dioxide and water, introducing the low temperature water obtained from decompressional expansion and gas-liquid separation of the mixture of carbon dioxide and water, as well as the low temperature syngas obtained from decompressional expansion of the syngas into a condenser of the Rankine cycle, or first using the low temperature water and the low temperature syngas to cool cooling water, then leading the cooling water the condenser of the Rankine cycle so as to serve as a cooling medium for exhaust steam cooling, thus improving the power generation efficiency of the Rankine cycle.
Description
Invention field
The present invention relates to the Poly-generation field of coal, being specially with the coal is the pneumoelectric coproduction field of raw material.
Background technology
Coal Gasification Technology is current cleaning, and the main approach that high-efficiency coal utilizes also is one of key link of current energy hi-tech development.The coal gasifying process of current comparative maturity comprises the strange gasifying process in Shandong, Shell gasifying process and GE (Texaco) gasifying process etc.From the consideration of gasification rate, the common feature of these gasifying process be gasification temperature usually more than 1000 ℃, it mainly is CO and H that synthetic gas is formed
2These gasifications are because the coal gasification temperature is very high, and efficiency of carbon conversion is also very high, does not have the carbon residue problem basically.
Produce the flow process of synthetic gas or methane for the catalytic gasification that with the coal water slurry is raw material; Since the catalytic gasification of coal lower temperature for example the supercritical temperature of water as carrying out under 650 ℃ at the most; Speed of reaction certainly will be lower than its corresponding Coal Gasification Technology under the high temperature more than 1000 ℃, reaction carry out the also corresponding reduction of degree, thereby the part coal is failed fully reaction; So in the product inevitably some carbon residue be unreacted coal completely; And this part carbon residue and water and lime-ash (being the mineral substance composition in the coal, generally not flammable) form mixture, and this mixture is commonly referred to as slurry-like residual carbon.How effectively to utilize this part slurry-like residual carbon, be an importance that improves the efficiency of catalytic coal gasifaction whole process flow.
For the processing of such slurry-like residual carbon, common treating processes is through pump slurry-like residual carbon to be delivered to the pressure filter press filtration to go out moisture wherein, utilizes external heat source that carbon residue is carried out drying afterwards, and dried carbon residue is sent to boiler and burns.The energy of such process need labor, and flow process is complicated.
Another kind of conventional treatment process is a landfill, but the landfill rule is not obviously effectively utilized these carbon residues, and is unfavorable for environment protection.
In addition, Coal Gasification Technology is in China's widespread use, but is confined to coal chemical technology basically, is main to obtain tangible Chemicals.In order to improve energy efficiency, current development trend is that Coal Gasification Technology and generation technology are combined, and promptly carries out so-called pneumoelectric coproduction, is raw material with the coal, co-production synthesis gas, electricity and hot.Wherein, synthetic gas is combustion power generation further, or further is processed into Chemicals (like synthetic ammonia, methyl alcohol, dme, liquid fuel etc.).Such pneumoelectric joint process organically combines chemical process and electrical production, has obtained huge social and economic benefit.
Current Coal (syngas) polygeneration technology; Mainly rest on carrying out coproduction in each relatively independent follow-up system of gasification product stream importing; For example be used for synthesizing methanol etc. with acting as a fuel in the synthetic gas importing power generation system that produces in the coal gasification course, perhaps this synthetic gas being imported in the follow-up system for methanol synthesis.Wherein, coal gasifying process and electrification technique as well as or methanol synthesizing process are relatively independent, only depend on the product flow thigh to get in touch between them, see between each technology it is relatively independent from the angle of energy.
Another kind of coal gas Electricity Federation prodn. art is that integrated gasification combined cycle plants (is called for short IGCC; Down together); In this technology; The oxygen that coal after the processing and air separation unit come generates synthetic gas in vapourizing furnace, the sensible heat of synthetic gas adds hot water to produce steam through indirect heat exchange, and this steam can be used for driving steam turbine generation.Synthetic gas gets into gas turbine combustion with generating after purifying through clean unit, and the heat of combustion tail gas reclaims and produce steam in waste heat boiler, and this steam also can be used for driving steam turbine generation.
The steam turbine generating is used based on Rankine round-robin thermodynamic process usually.The Rankine circulation is a kind of steam-electric power circulation well known to those skilled in the art, and typical R ankine round-robin schema is as shown in Figure 2, is summarized as follows:
Water gets into boiler by the service pump adherence pressure, after boiler is heated into steam, gets into then and continues heating in the suphtr, and its temperature is further raise, and (its effect mainly contained two: one, further increased efficient thereby continue elevated temperature; The 2nd, become unsaturation steam (being called dry steam) from saturation steam (being called wetting vapour).The total heat that in this heating and superheating process, sucks is Q.Then, make dry steam external work done Ws of adiabatic expansion in mover (steamer or turbine), the steam (being called exhaust steam) after the cooling of expanding gets into condensing surface again and is condensed into water, emits heat.Water of condensation is sent into boiler through service pump again, accomplishes a circulation.
Ideal Rankine circulation also can use temperature-entropy diagram as shown in Figure 3 (T-S figure) to describe.The external theoretical merit of doing of steam is equivalent to the area that curve 1 → 2 → 3 → 4 → 5 → 6 → 1 is surrounded among Fig. 3.Wherein heat absorption (1 → 2 → 3 → 4) and the exothermic process (5 → 6) in the circulation is isobaric process, and expansion of steam (4 → 5) and the water of condensation process (6 → 1) of boosting is an isoentropic process.
Introduce in detail about the Rankine round-robin, see also " the practical pandect of modern coal conversion and Coal Chemical Industry new technology novel process ", the 6th piece of chapter 9; The steam integrated coal gasification combined cycle, Liao Hanxiang chief editor, 2004; And " integrated gasification combined cycle thermoelectric oil multi-production process technical characterstic and application ", Chen Chongliang, Yuan Longjun; The coal engineering, 2008 11 phases.
Visible by Fig. 2, the steam turbine generating mainly comprises steam turbine generation, steam cooling, and several parts are returned in the pump pressurization.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 round-robin net work W
s(W
s=Δ H=H
5-H
4) be the ratio of the Q of Fig. 2 by the initial heat supplied in the external world.
Whole Rankine round-robin thermo-efficiency is:
η＝(H
4-H
5)/(H
4-H
1)
H wherein
4, H
5, H
1Represent the enthalpy of the preceding steam of entering turbine shown in Figure 2 respectively, the enthalpy of exhaust steam 5 and the enthalpy that gets into the high pressure water of boiler.This enthalpy is directly proportional with the temperature of steam or water basically.
For the exothermic process that in steam turbines, carries out, the temperature that reduces exhaust steam 5 can improve the Rankine thermal efficiency of cycle, but the temperature of exhaust steam 5 can not unrestrictedly reduce, and this temperature is limited by coolant temperature and condenser size.For example, in the steam turbine power generation process, the heat-eliminating medium of steam cooling part is often used water coolant usually.The common operating mode of water coolant is gauge pressure 0.52MPa, 32 ℃ of temperature.Because the restriction of water coolant medium, the steam that goes out turbine are being controlled at usually more than 32 ℃ of so-called exhaust steam 5 among Fig. 2.
For instance; Under the situation that makes water and dry steam as the Rankine circulatory mediator, the temperature that gets into the dry steam of steam turbine is 550 ℃, and pressure is 23MPa; And the temperature that goes out the exhaust steam 5 of steam turbine is 120.21 ℃; Pressure is 0.2Mpa, and in this case, thermo-efficiency is about 23% through calculating.
Obviously, above-mentioned Rankine circulation requires to provide a large amount of water coolants.
It is thus clear that; In above-mentioned IGCC technology; Remain and utilize the energy that heat exchange and/or burning produced of this product flow thigh of synthetic gas that water is heated into steam, steam and then driving steam turbine generation also are relatively independent between coal gasifying process and the Rankine circulation technology.Be the Influence of Temperature of the Rankine round-robin generating efficiency steam that only receives to be produced, coal gasifying process does not directly influence Rankine round-robin generating efficiency.In other words; More than the technology of gasification and steam turbine generation associating has only been utilized by the steam that produces in the coal gasification course; Promptly only by the steam of the generation in the coal gasification course coal gasifying process and steam turbine generation technology are got in touch, energy degree of integration and technology degree of integration all still have the leeway of raising.
The present invention then provides a kind of and has seen from process flow thigh and energy point of view, the coupling process of coal gasifying process that degree of integration is higher and slurry-like residual carbon total oxygen metallization processes and steam turbine generation technology.
Summary of the invention
In first aspect of the present invention, the invention provides the coupling process of a kind of coal gasifying process and carbon residue oxidizing process and steam turbine generation technology, may further comprise the steps:
A makes the generating gasification reaction in vapourizing furnace of coal and water and optional oxidizing agent, thereby produces mixture after the reaction that comprises synthetic gas and slurry-like residual carbon, and wherein said pulpous state carbon residue comprises water and carbon residue;
B imports said reaction back mixture in the interchanger and carries out indirect heat exchange with water, and water is heated and generates steam, and said reaction back mixture is cooled and obtains cooled reaction mixture afterwards;
C introduces the steam that generates among the step b and expands acting in the steam turbine and generate electricity, and this steam becomes exhaust steam because of the acting of expanding, and wherein the temperature and pressure of this exhaust steam has reduced than all with vapor phase among the step b;
D carries out gas/liquid-solid separation to the cooled reaction back mixture among the step b, obtains two bursts of logistics: (I) synthetic gas; (II) comprise the slurry-like residual carbon of water and carbon residue; Then,
E makes that above-mentioned logistics (I) and logistics (II) are parallel carries out following two sub-steps:
(e1) with logistics (I) expansion step-down, the synthetic gas after the step-down that obtains expanding;
(e2) logistics (II) is sent in the oxidation reactor, said slurry-like residual carbon and excessive oxygen are reacted, generate the mixture that logistics (III) promptly comprises carbonic acid gas and water; Logistics then (III) obtains atmospheric carbon dioxide and liquid water successively through foam overblow step-down and gas-liquid separation;
Then,
F will feed in the condensing surface to carry out indirect heat exchange with the exhaust steam from step c as heat-eliminating medium from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2) jointly, thus said exhaust steam become water of condensation;
G will from the interchanger of sending into step b after the pressurization of the water of condensation of step f with said reaction afterwards mixture carry out heat exchange, to produce said steam again.
In second aspect of the present invention, the invention provides the coupling process of a kind of coal gasifying process and carbon residue oxidizing process and steam turbine generation technology, may further comprise the steps:
A makes the generating gasification reaction in vapourizing furnace of coal and water and optional oxidizing agent, thereby produces mixture after the reaction that comprises synthetic gas and slurry-like residual carbon, and wherein said pulpous state carbon residue comprises water and carbon residue;
B imports said reaction back mixture in the interchanger and carries out indirect heat exchange with water, and water is heated and generates steam, and said reaction back mixture is cooled and obtains cooled reaction mixture afterwards;
C introduces the steam that generates among the step b and expands acting in the steam turbine and generate electricity, and this steam becomes exhaust steam because of the acting of expanding, and wherein the temperature and pressure of this exhaust steam has reduced than all with vapor phase among the step b;
D carries out gas/liquid-solid separation to the cooled reaction back mixture among the step b, obtains two bursts of logistics: (I) synthetic gas; (II) comprise the slurry-like residual carbon of water and carbon residue; Then,
E makes that above-mentioned logistics (I) and logistics (II) are parallel carries out following two sub-steps:
(e1) with logistics (I) expansion step-down, the synthetic gas after the step-down that obtains expanding;
(e2) logistics (II) is sent in the oxidation reactor, said slurry-like residual carbon and excessive oxygen are reacted, generate the mixture that logistics (III) promptly comprises carbonic acid gas and water; Logistics then (III) obtains atmospheric carbon dioxide and liquid water successively through foam overblow step-down and gas-liquid separation;
Then,
F will come successively as heat-eliminating medium or simultaneously water coolant cooled off from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2), obtain thus through the refrigerative water coolant; Feed in the condensing surface to carry out indirect heat exchange through the refrigerative water coolant said then, thus said exhaust steam is become water of condensation with exhaust steam from step c;
G will from the interchanger of sending into step b after the pressurization of the water of condensation of step f with said reaction afterwards mixture carry out heat exchange, to produce said steam again.
The accompanying drawing summary
Fig. 1 is the indicative flowchart of a kind of thermoelectric gas joint process of the prior art.
Fig. 2 is a Rankine round-robin indicative flowchart.
Fig. 3 is Rankine round-robin temperature-entropy diagram (T-S figure).
Fig. 4 is a kind of indicative flowchart of embodiment of the first aspect of method of the present invention.
Fig. 5 is a kind of indicative flowchart of embodiment of the second aspect of method of the present invention.
Detailed Description Of The Invention
In the step a of first aspect of the present invention, make the generating gasification reaction in vapourizing furnace of coal and water and optional oxidizing agent, thereby produce mixture after the reaction that comprises synthetic gas and slurry-like residual carbon, wherein said pulpous state carbon residue comprises water and carbon residue.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 can be in and anyly be suitable for making under the processing condition of gasification, preferably is under subcritical or the supercritical state.Oxygenant can be oxygen, oxygen-rich air, air or hydrogen peroxide or their any two kinds or more kinds of mixtures.Can randomly add oxygenant, if the oxygenant that adds words, then its add-on can be the 10-60% of ature of coal amount.Coal and water and the reaction of optional oxidizing agent generating gasification generate the multiple reaction product that comprises synthetic gas, also generate slurry-like residual carbon simultaneously.Slurry-like residual carbon is the mixture that comprises carbon residue, lime-ash and big water gaging, and usually, carbon residue content wherein is 10-30 weight %; Cinder content is 20-30 weight %; The content of water is 50-60 weight %, surplus is other solid matter, and said weight % is based on the gross weight of slurry-like residual carbon.Gaseous product and slurry-like residual carbon mix the outflow vapourizing furnace, and the material that flows out vapourizing furnace is referred to as reaction back mixture.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 ature of coal amount mark) is generally 10-70%, preferred 20-50%.Can also add stablizer and a certain proportion of catalyzer in the process for preparation.The add-on of catalyzer can be the 2-20% of quality of pc.Catalyzer comprises but is not limited to oxyhydroxide, basic metal or alkaline earth salt or their mixture, the for example K of oxide compound, basic metal or the earth alkali metal of basic metal or earth alkali metal
2O, Na
2O, CaO, MgO, NaOH, KOH, Ca (OH)
2, Mg (OH)
2, K
2CO
3And Na
2CO
3, or the mixture of forming by them.With sending in the vapourizing furnace after such coal water slurry preheating pressurization; Vapourizing furnace is under the subcritical state or supercritical state of water; The subcritical state of wherein said water is meant temperature more than the atmospheric boiling point of water and below the critical temperature at water and pressure is to make water remain liquid pressure, the supercritical state of said water be meant absolute pressure more than the 22.1MPa and temperature more than 374 ℃.Coal reacts with the water generating gasification in this vapourizing furnace, generates synthetic gas.Can also randomly in vapourizing furnace, feed oxygenant for example oxygen, oxygen-rich air, air or hydrogen peroxide or their any two kinds or more kinds of mixtures, then coal generates synthetic gas with water and oxidant reaction in this vapourizing furnace.It is worthy of note that this oxygenant is optional the interpolation, promptly this oxygenant can add also and can not add.But preferably add oxygenant; Because oxygenant is except also providing a part of synthetic gas with the coal reaction; The more important thing is that because the gasification reaction that coal and subcritical water or supercritical water take place absorbs heat, coal and oxidant reaction are emitted heat then can be used for keeping the temperature in the vapourizing furnace.If do not add oxygenant, then in order to keep gasifier temperature, need indirect heating equipment for example electrically heated cover etc. vapourizing furnace is heated to keep the temperature of vapourizing furnace.In the another kind of embodiment of step a of the present invention, said gasification can be called the gasifying process of pressurised fluidized bed gasification (is representative with the KRW gasifying process) or pressurized entrained-bed gasification (is representative with the Inferior of Texaco Gasification Technology) by those skilled in the art.The pressurised fluidized bed gasification of coal is meant the coal gasification of in the fluidized-bed gasification furnace that pressure is increased, being heated; The gasification of the pressurized entrained-bed of coal is meant the coal gasification of in the airflow bed gasification furnace that pressure is increased, being heated.About the definition and concrete configuration of fluidized-bed and air flow bed, be well known to a person skilled in the art, repeat no more here.20 middle of century; The various shortcoming that gasification exists to The normal pressure fluidized bed; Fluidized-bed gasification furnace develops to pressurization and raising gasification temperature direction, and has successfully developed multiple novel fluidized bed gasification technology, and HTW, U-gas, CFB and KRW vapourizing furnace are wherein typically arranged.Pressurised fluidized bed gasifying process is a s-generation Coal Gasification Technology, and suitable coal mainly contains the fine coal charging of the not too strong long-flame coal of brown coal, non-caking coal, weakly caking coal, cohesiveness, meager coal, lean coal and hard coal etc.The pressurized air flow bed gasification technology is one of direction of first developing both at home and abroad, is the technology the most ripe in the s-generation Coal Gasification Technology, that the commercialization device is maximum, and is the most representative with the pressurized air flow bed gasification technology that Texaco (Texaco) method wet method is reinforced.
The gasifying process of step a of the present invention can adopt above-mentioned any gasifying process.No matter adopt above-mentioned which kind of gasifying process, all will leave all materials of vapourizing furnace, comprise the coal gas that gasification produces, be referred to as reaction back mixture.
In the step b of first aspect of the present invention, said reaction back mixture imported in first interchanger carry out indirect heat exchange with water, water is heated and generates steam, and said reaction back mixture is cooled and obtains cooled reaction mixture afterwards.The water that wherein carries out heat exchange with reaction back mixture is the pressurized water after the pump pressurization.Wherein said first interchanger can be any suitable interchanger that is used for indirect heat exchange, for example shell and tube heat exchanger, finned heat exchanger etc., and the type of these interchanger is well known to a person skilled in the art with concrete structure, repeats no more here.Owing to the temperature of mixture after the reaction of leaving vapourizing furnace is very high, so reclaim its sensible heat through the water heat exchange, this can be transformed into steam with this liquid water, and the absolute pressure of wherein said steam is more than the 15MPa, and temperature is more than 200 ℃.The steam that will be among this paper in the above temperature and pressure scope is called high temperature and high pressure steam.The actual temp of this steam and pressure can specifically be selected in above scope according to the needs of Rankine round-robin processing condition, and for example in a preferred embodiment, absolute pressure can be 15MPa and temperature is 400 ℃ or higher.In another embodiment, said high temperature and high pressure steam is that temperature is that 374-700 ℃ and absolute pressure are the steam of 22.1-40MPa.In one embodiment, this high temperature and high pressure steam can be for being suitable for any temperature and pressure of Rankine round-robin.Obviously, this first interchanger has played boiler and the effect of suphtr in the Rankine circulation shown in Fig. 2.
In the step c of first aspect of the present invention, the steam that generates among the step b to be introduced expand acting in the steam turbine and generate electricity, this steam becomes exhaust steam because of the acting of expanding, and wherein the vapor phase among the temperature and pressure of this exhaust steam and the step b is than all having reduced.In one embodiment, the temperature of this exhaust steam is about 25 ℃-30 ℃, and absolute pressure is 0.0032-0.0042MPa.It is worthy of note that exhaust steam still is in steam condition.Then this exhaust steam is imported in the condensing surface.
In the steps d of first aspect of the present invention, the cooled reaction back mixture among the step b is carried out gas/liquid-solid separation, obtain two bursts of logistics: (I) synthetic gas; (II) comprise the slurry-like residual carbon of water and carbon residue.This sepn process can be carried out in well known to a person skilled in the art the gas/liquid-solid separator of any routine.After the separation, separator is left in two bursts of logistics respectively, goes to subsequent step separately.
In the step e of first aspect of the present invention, above-mentioned logistics (I) and logistics (II) are walked abreast carry out following two sub-steps:
(e1) with logistics (I) expansion step-down, the synthetic gas after the step-down that obtains expanding;
(e2) logistics (II) is sent in the oxidation reactor, said slurry-like residual carbon and excessive oxygen are reacted, generate the mixture that logistics (III) promptly comprises carbonic acid gas and water; Logistics then (III) obtains atmospheric carbon dioxide and liquid water successively through overcooling, expansion step-down and gas-liquid separation.In step e1, with this synthetic gas expansion step-down, obtain the low-temp low-pressure synthetic gas through bloating plant thus, wherein said low temperature is below 2.6 ℃, low pressure is below the 2MPa.Such bloating plant comprises step-down kapillary, dropping valve, decompressor etc.The method and apparatus of gas expansion step-down all well known to a person skilled in the art, repeat no more at this.Such expansion step-down process also causes the synthetic gas temperature to reduce, and for example can the temperature of synthetic gas be reduced to about 0 ℃.As more general principle, can the temperature of this synthetic gas be reduced to the temperature lower than the exhaust steam of step c.In step e2, said slurry-like residual carbon and excessive oxygen are reacted, generate the mixture that logistics (III) promptly comprises carbonic acid gas and water, and generate lime-ash.The amount that wherein said excessive oxygen is meant oxygen is more than making the just amount of the required oxygen of complete oxidation of carbon residue.This oxidizing reaction is generally carried out in oxidation reactor, and carries out in the preferred water under being in subcritical state or supercritical state.Slurry-like residual carbon is introduced in the oxidation reactor, in this oxidation reactor, fed excessive oxygen simultaneously.Oxygen can provide with modes such as purity oxygen or oxygen-rich air or normal air.In the presence of excessive oxygen, carbon residue is generated CO by complete oxidation basically
2, emit heat simultaneously and heat the water in the slurry-like residual carbon, thereby make the temperature of this oxidation reactor be increased to the subcritical state or the supercritical state of water, and under this state, make carbon residue and oxygen sustained reaction.Certainly, also can by other thermal source the temperature of this oxidation reactor be increased to the subcritical state or the supercritical state of water independently.Sub-fraction in the reaction institute liberated heat is used to remedy the thermosteresis that causes because of the reactor drum heat radiation; With the temperature of keeping reactor drum itself on the desired temperatures level; The then recyclable utilization of most of heat for example is used for the preheating water coal slurry, perhaps is used to produce steam and generates electricity.This heat recovery method is well known to a person skilled in the art.Said oxidation reactor can be tubular reactor or fluidized-bed reactor.Slurry-like residual carbon and oxygen also circulation are gone in the reactor drum, also can adverse current feed in the reactor drum.The charging mass flux ratio of slurry-like residual carbon and oxygen can be 1: 1.5 to 1: 3.Through above-mentioned complete oxidation technology, the carbon residue in the coal has also obtained almost 100% utilization.Make above-mentioned logistics (III) successively through foam overblow step-down and gas-liquid separation then, obtain atmospheric carbon dioxide and liquid water.Stream I II is after the foam overblow step-down, and temperature can be reduced to below 20 ℃.Before the expansion depressurization step, can also earlier logistics (III) be cooled off and purify.In the embodiment preferred of this step e2, can implement above-mentioned process of cooling through the water that enters into step a with logistics (III) preheating.In another embodiment preferred of this step e2, between said process of cooling and expansion step-down, also there is the process that logistics (III) is purified, this scavenging process is used for removing the dust that stream I II contains.Gas-liquid separation process among the step e2 also well known to a person skilled in the art, repeats no more.
In the step f of first aspect of the present invention; To feed in the condensing surface to carry out indirect heat exchange as heat-eliminating medium jointly from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2), thus said exhaust steam become water of condensation with exhaust steam from step c.This heat exchange step can be carried out in condensing surface.This condensing surface is interchanger, for example an interchanger of shell and tube heat exchanger or finned heat exchanger and any suitable type in essence.The exhaust steam of step c and said liquid water and can carry out indirect heat exchange therein from the synthetic gas after the expansion step-down of step e1.Exhaust steam is condensed into water of condensation, and the synthetic gas after the expansion step-down then temperature slightly promotes, and synthetic gas leaves the follow-up separating unit of condensing surface entering or delivers to the gas turbine combustion generating then.Water coolant with the exhaust steam heat exchange after also leave this condensing surface.It is worthy of note; Under the situation of using indirect heat exchange; Synthetic gas after said liquid water and the said expansion step-down is to get into this condensing surface respectively and leave this condensing surface respectively; Be the two pipeline of respectively walking each, do not come in contact each other or mix, but they have carried out heat exchange jointly in this condensing surface Yu from the exhaust steam of step c.And the synthetic gas after the water of condensation that exhaust steam cooling back forms and said liquid water and the said expansion step-down does not take place directly to contact yet.In this step f, condensing surface can be one or more, and when adopting a plurality of condensing surface, they can be one another in series or parallel connection or series-parallel connection.
In the step g of first aspect of the present invention, will from the interchanger of sending into step b after the pressurization of the water of condensation of step f with said reaction afterwards mixture carry out heat exchange, to produce said steam again.Pressurization is carried out through pump, preferably this liquid water is heated to more than the absolute pressure 15MPa.Reacted the back mixture heating up and regenerated high temperature and high pressure steam by the pyritous from vapourizing furnace behind the interchanger of this liquid water entering step b, this high temperature and high pressure steam is used to carry out next round Rankine circulation.
The each side of the step a of the second aspect of the present invention all step a with first aspect of the present invention is identical.
The each side of the step b of second aspect of the present invention is identical with the step b of first aspect of the present invention.
The each side of the step c of second aspect of the present invention is identical with the step c of first aspect of the present invention.
The each side of the steps d of second aspect of the present invention is identical with the steps d of first aspect of the present invention.
The each side of the step e of second aspect of the present invention is identical with the step e of first aspect of the present invention.
In the step f of second aspect of the present invention, will come successively as heat-eliminating medium or simultaneously water coolant will be cooled off from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2), obtain thus through the refrigerative water coolant; Feed in the condensing surface to carry out indirect heat exchange through the refrigerative water coolant said then, thus said exhaust steam is become water of condensation with exhaust steam from step c.Above-mentionedly use from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2) to come successively or simultaneously water coolant is carried out the refrigerative process to occur in the interchanger as heat-eliminating medium; Interchanger among this interchanger and the step b is not same interchanger; But it is the same with the interchanger among the step b; It can be any suitable interchanger, for example shell and tube heat exchanger or a finned heat exchanger etc. in this area.The water coolant that is cooled for example is conventional water coolant (for example about 32 ℃ of its temperature), and it leaves the water coolant of this interchanger, claims again through the refrigerative water coolant, and then temperature decreases, and for example is reduced to 20 ℃.To be somebody's turn to do then to import in the condensing surface Yu and carry out indirect heat exchange, thus said exhaust steam become water of condensation from the exhaust steam of step c through the refrigerative water coolant.This condensing surface also is interchanger, for example an interchanger of shell and tube heat exchanger or finned heat exchanger and any suitable type in essence.The exhaust steam of step c with can carry out indirect heat exchange therein through the refrigerative water coolant.Exhaust steam is condensed into water of condensation.
The each side of the step g of second aspect of the present invention is identical with the step g of first aspect of the present invention.
Embodiment
Illustrate method of the present invention through following non-limiting example.
Embodiment 1
With reference to Fig. 4, the catalytic gasification that takes place with bituminous coal and supercritical water is an example.Coal is processed granularity less than 150 microns coal dust, with catalyst n a through pulverize grinding
2CO
3It is 40% coal water slurry that (consumption be quality of pc 10%) and water are prepared into coal dust butt concentration.The process of preparation coal water slurry is not drawn in Fig. 4.Coal water slurry is through pressurization, and preheating reaches 23MPa, and 550 ℃ get into vapourizing furnace, aerating oxygen in vapourizing furnace simultaneously.The oxygen reaction of part coal water slurry and adding in vapourizing furnace is with temperature increase to 650 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the synthetic gas and the slurry-like residual carbon that are rich in methane.The staple of synthetic gas is a methane, carbon monoxide, carbonic acid gas, hydrogen etc.Mixture comprises synthetic gas and slurry-like residual carbon after going out the reaction of vapourizing furnace.This product with from 23MPa water heat exchange in interchanger of force (forcing) pump; Producing temperature and be 400 ℃ and absolute pressure is the high temperature and high pressure steam of 15MPa; This high temperature and high pressure steam becomes exhaust steam after getting into the steam turbine expansion power generation; It is 0.0032MPa that this exhaust steam can be controlled in pressure, and temperature is 25 ℃, and exhaust steam gets into condenser condenses Cheng Shui.Mixture entering separator carries out gas/liquid-solid separation after the reaction after the heat exchange; Synthetic gas after the separation cools the temperature to 0 ℃ through the foam overblow step-down; Be used as the heat-eliminating medium of above-mentioned condensing surface then; So that exhaust steam is condensed into water, this synthetic gas can get into the later separation unit or get into follow-up gas turbine combustion generating afterwards.Slurry-like residual carbon then is transported in the oxidation reactor.In this oxidation reactor, feed excessive oxygen, and the oxidizing reaction liberated heat of dependence carbon residue and oxygen all rises to the temperature and pressure in this oxidation reactor the subcritical state or the supercritical state of water.Oxidizing reaction continues to carry out, and obtains comprising CO after the reaction
2And H
2The fluid mixture of O and lime-ash, the heat that reaction is produced are used for the preheating water coal slurry or produce steam.Lime-ash is discharged oxidation reactor, as material of construction.And the said CO that comprises
2And H
2The mixture of O then is able to cooling through the preheating water coal slurry, purifying and dedusting then, and expanding is depressurized to about about 2 ℃, carries out gas-liquid separation then, obtains cryogenic liquid water and atmospheric carbon dioxide.Then this cryogenic liquid water also is passed in the said condensing surface, be used for said expansion step-down after synthetic gas come together exhaust steam is cooled to water of condensation.To after the pump pressurization, turn back in the interchanger with from this water of condensation then and carry out heat exchange, to produce high temperature and high pressure steam again from mixture after the pyritous reaction of vapourizing furnace.
Embodiment 2
With reference to Fig. 5, the catalytic gasification that takes place with bituminous coal and supercritical water is an example.Coal is processed granularity less than 150 microns coal dust, with catalyst n a through pulverize grinding
2CO
3It is 40% coal water slurry that (consumption be quality of pc 10%) and water are prepared into coal dust butt concentration.The process of preparation coal water slurry is not drawn in Fig. 5.Coal water slurry is through pressurization, and preheating reaches 23MPa, and 550 ℃ get into vapourizing furnace, aerating oxygen in vapourizing furnace simultaneously.The oxygen reaction of part coal water slurry and adding in vapourizing furnace is with temperature increase to 650 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the synthetic gas and the slurry-like residual carbon that are rich in methane.The staple of synthetic gas is a methane, carbon monoxide, carbonic acid gas, hydrogen etc.Mixture comprises synthetic gas and slurry-like residual carbon after going out the reaction of vapourizing furnace.This product with from 23MPa water heat exchange in interchanger of force (forcing) pump; Producing temperature and be 400 ℃ and absolute pressure is the high temperature and high pressure steam of 15MPa; This high temperature and high pressure steam becomes exhaust steam after getting into the steam turbine expansion power generation; It is 0.0032MPa that this exhaust steam can be controlled in pressure, and temperature is 25 ℃, and exhaust steam gets into condenser condenses Cheng Shui.Mixture entering separator carries out gas/liquid-solid separation after the reaction after the heat exchange; Synthetic gas after the separation cools the temperature to 0 ℃ through the foam overblow step-down; Be incorporated into certain interchanger (this interchanger is not an interchanger with the interchanger that usefulness generates said steam) then and as heat-eliminating medium water coolant cooled off, this synthetic gas can get into the later separation unit or get into follow-up gas turbine combustion generating afterwards.Slurry-like residual carbon then is transported in the oxidation reactor.In this oxidation reactor, feed excessive oxygen, and the oxidizing reaction liberated heat of dependence carbon residue and oxygen all rises to the temperature and pressure in this oxidation reactor the subcritical state or the supercritical state of water.Oxidizing reaction continues to carry out, and obtains comprising CO after the reaction
2And H
2The fluid mixture of O and lime-ash, the heat that reaction is produced are used for the preheating water coal slurry or produce steam.Lime-ash is discharged oxidation reactor, as material of construction.And the said CO that comprises
2And H
2The mixture of O then is able to cooling through the preheating water coal slurry, purifying and dedusting then, and expanding is depressurized to about about 2 ℃, carries out gas-liquid separation then, obtains cryogenic liquid water and atmospheric carbon dioxide.Then this cryogenic liquid water also is passed in said certain interchanger, be used for said expansion step-down after synthetic gas come together water coolant is cooled off.To be sent in the condensing surface carrying out heat exchange through the refrigerative water coolant then, and exhaust steam will be cooled to water of condensation with exhaust steam.This water of condensation turns back to after the pump pressurization in the interchanger with from mixture after the pyritous reaction of vapourizing furnace and carries out heat exchange then, to produce high temperature and high pressure steam again.
Advantage of the present invention is following:
The coupling process of coal gasifying process of the present invention and slurry-like residual carbon total oxygen metallization processes and steam turbine generation technology makes the energy efficiency of system be improved.At first, the thermal source in the Rankine circulation takes from that the sensible heat of mixture reclaims after the reaction behind the gasification reaction, does not need external heat source.Secondly; In condensing surface, then adopted the low-temp low-pressure synthetic gas after the expansion step-down and come common condensation exhaust steam from the water at low temperature after the expansion step-down of stream I II; Perhaps earlier with the low-temp low-pressure synthetic gas after the expansion step-down and from coming water coolant from the water at low temperature after the expansion step-down of stream I II; Make then through refrigerative water and go the condensation exhaust steam, made full use of synthetic gas and said water at low temperature after the expansion step-down cold energy.No matter take above which kind of scheme; Because the temperature of heat-eliminating medium all is lower than the temperature of conventional water coolant; So all can set the temperature of the exhaust steam that steam turbine lower, this be equivalent to 5 among the T-S figure and 6 two are moved down, so increased the area that curve 1-2-3-4-5-6-1 is surrounded; The theoretical merit that expression steam is externally done is bigger, and then has increased generating efficiency.Once more, also help follow-up sepn process after the synthetic gas expansion step-down.At last, the total oxygenization of slurry-like residual carbon makes carbon residue obtain almost 100% utilization, has reduced the discharging of solid waste.
Although described the method for this aspect in conjunction with concrete embodiment, one skilled in the art will recognize that, can also carry out various variations to the present invention, and not deviate from defined protection domain in the appended claim.For example, though among the present invention Rankine circulation with water and steam as working medium, obviously, the present invention also be applicable to other material for example carbonic acid gas, organic fluid for example the Rankine that makes the work medium such as isoparaffin circulate.Those skilled in the art have the ability to regulate the concrete processing parameter among the present invention according to the concrete working medium that is adopted, so that the present invention is able to implement.And those skilled in the art obviously also can replace with the coal among the present invention biomass and/or organic waste.Biomass are got its ordinary meaning, promptly directly come from the material of organism, for example stalk, vegetation, algae, vegetables oil, animal tallow, cereal, grain hulls or nut shell etc.Organic waste then for example is: the mud of municipal wastes, human waste's (black/buck), sewage sludge, Biohazard Waste, the mud that contains waste, petroleum refining and petroleum chemicals waste, paper pulp and the paper mill of organic trade waste, electronic component manufacturing, sewage work's process biochemical treatment, or the like.Therefore, the present invention will comprise that also with biomass and/or organic waste be the gasifying process that carries out of raw material and coupling process by the total oxygen metallization processes and the steam turbine generation technology of the carbon residue that produces behind biomass and/or the organic waste material for gasification.
Claims (10)
1. the coupling process of a coal gasifying process and carbon residue oxidizing process and steam turbine generation technology may further comprise the steps:
A makes the generating gasification reaction in vapourizing furnace of coal and water and optional oxidizing agent, thereby produces mixture after the reaction that comprises synthetic gas and slurry-like residual carbon, and wherein said pulpous state carbon residue comprises water and carbon residue;
B imports said reaction back mixture in the interchanger and carries out indirect heat exchange with water, and water is heated and generates steam, and said reaction back mixture is cooled and obtains cooled reaction mixture afterwards;
C introduces the steam that generates among the step b and expands acting in the steam turbine and generate electricity, and this steam becomes exhaust steam because of the acting of expanding, and wherein the temperature and pressure of this exhaust steam has reduced than all with vapor phase among the step b;
D carries out gas/liquid-solid separation to the cooled reaction back mixture among the step b, obtains two bursts of logistics: (I) synthetic gas; (II) comprise the slurry-like residual carbon of water and carbon residue; Then,
E makes that above-mentioned logistics (I) and logistics (II) are parallel carries out following two sub-steps:
(e1) with logistics (I) expansion step-down, the synthetic gas after the step-down that obtains expanding;
(e2) logistics (II) is sent in the oxidation reactor, said slurry-like residual carbon and excessive oxygen are reacted, generate the mixture that logistics (III) promptly comprises carbonic acid gas and water; Logistics then (III) obtains atmospheric carbon dioxide and liquid water successively through foam overblow step-down and gas-liquid separation;
Then,
F will feed in the condensing surface to carry out indirect heat exchange with the exhaust steam from step c as heat-eliminating medium from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2) jointly, thus said exhaust steam become water of condensation;
G will from the interchanger of sending into step b after the pressurization of the water of condensation of step f with said reaction afterwards mixture carry out heat exchange, to produce said steam again.
2. the coupling process of a coal gasifying process and carbon residue oxidizing process and steam turbine generation technology may further comprise the steps:
A makes the generating gasification reaction in vapourizing furnace of coal and water and optional oxidizing agent, thereby produces mixture after the reaction that comprises synthetic gas and slurry-like residual carbon, and wherein said pulpous state carbon residue comprises water and carbon residue;
B imports said reaction back mixture in the interchanger and carries out indirect heat exchange with water, and water is heated and generates steam, and said reaction back mixture is cooled and obtains cooled reaction mixture afterwards;
C introduces the steam that generates among the step b and expands acting in the steam turbine and generate electricity, and this steam becomes exhaust steam because of the acting of expanding, and wherein the temperature and pressure of this exhaust steam has reduced than all with vapor phase among the step b;
D carries out gas/liquid-solid separation to the cooled reaction back mixture among the step b, obtains two bursts of logistics: (I) synthetic gas; (II) comprise the slurry-like residual carbon of water and carbon residue; Then,
E makes that above-mentioned logistics (I) and logistics (II) are parallel carries out following two sub-steps:
(e1) with logistics (I) expansion step-down, the synthetic gas after the step-down that obtains expanding;
(e2) logistics (II) is sent in the oxidation reactor, said slurry-like residual carbon and excessive oxygen are reacted, generate the mixture that logistics (III) promptly comprises carbonic acid gas and water; Logistics then (III) obtains atmospheric carbon dioxide and liquid water successively through foam overblow step-down and gas-liquid separation;
Then,
F will come successively as heat-eliminating medium or simultaneously water coolant cooled off from the synthetic gas after the expansion step-down of step (e1) with from the liquid water of step (e2), obtain thus through the refrigerative water coolant; Feed in the condensing surface to carry out indirect heat exchange through the refrigerative water coolant said then, thus said exhaust steam is become water of condensation with exhaust steam from step c;
G will from the interchanger of sending into step b after the pressurization of the water of condensation of step f with said reaction afterwards mixture carry out heat exchange, to produce said steam again.
3. claim 1 or 2 method, wherein oxygenant described in the step a is oxygen, oxygen-rich air, air or hydrogen peroxide or any two kinds or more kinds of mixtures in them.
4. claim 1 or 2 method; Wherein gasification reaction carries out in the presence of catalyzer described in the step a, and said catalyzer is selected from salt or their mixture of oxyhydroxide, basic metal or earth alkali metal of oxide compound, basic metal or the earth alkali metal of basic metal or earth alkali metal.
5. claim 1 or 2 method wherein replace water among step b with as Rankine round-robin working medium with other working medium that is selected from carbonic acid gas or isoparaffin.
6. claim 1 or 2 method; Wherein the said water among the step a is in the supercritical state or the subcritical state of water; And being reflected among the step e2 is in the water of supercritical state or subcritical state and carries out; Wherein subcritical state is meant temperature more than the atmospheric boiling point of water and below the critical temperature at water and pressure is to make water remain liquid pressure, the supercritical state of said water be meant absolute pressure more than the 22.1MPa and temperature more than 374 ℃.
7. claim 1 or 2 method, wherein the temperature of steam described in the step b is more than 200 ℃, more than the absolute pressure 15MPa of said steam.
8. wherein also there are the process that logistics (III) is cooled off and purified in claim 1 or 2 method before the expansion step-down in step (e2).
9. the method for claim 8, the process of cooling of wherein coming implementation step (e2) through the water that enters into step a with logistics (III) preheating.
10. each method in the aforementioned claim wherein replaces said coal to gasify with biomass and/or organic waste.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102587182A CN102373097B (en) | 2010-08-20 | 2010-08-20 | Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102587182A CN102373097B (en) | 2010-08-20 | 2010-08-20 | Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102373097A true CN102373097A (en) | 2012-03-14 |
| CN102373097B CN102373097B (en) | 2013-12-11 |
Family
ID=45792331
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102587182A Active CN102373097B (en) | 2010-08-20 | 2010-08-20 | Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102373097B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103555371A (en) * | 2013-11-15 | 2014-02-05 | 华东理工大学 | Method for improving gasification efficiency of slurry feed gasification device |
| CN105152509A (en) * | 2015-09-10 | 2015-12-16 | 新奥科技发展有限公司 | Supercritical reactor, supercritical reaction system and supercritical treatment method of sludge |
| CN105505465A (en) * | 2015-11-19 | 2016-04-20 | 万伟 | Method for using carbon-containing raw material to produce synthesis gas |
| CN105971679A (en) * | 2016-07-13 | 2016-09-28 | 西安热工研究院有限公司 | Supercritical water gasification and supercritical carbon dioxide Brayton cycle joint production system |
| CN106147865A (en) * | 2016-07-19 | 2016-11-23 | 西安交通大学 | The method and apparatus of continuous supercritical water double tube reactor gasification organic matter |
| CN111201307A (en) * | 2017-06-14 | 2020-05-26 | 多元伙伴公司 | Aftertreatment arrangement and method for the aftertreatment of gases at least downstream of a fluidized bed gasification process, and logic unit and use |
| CN113048465A (en) * | 2021-03-26 | 2021-06-29 | 中国科学院工程热物理研究所 | Coal-fired power generation system and method for coal gasification with supercritical water |
| CN116590053A (en) * | 2023-07-17 | 2023-08-15 | 太原理工大学 | Method and device for producing hydrogen by efficiently gasifying coal |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0129167A2 (en) * | 1983-06-10 | 1984-12-27 | Hitachi, Ltd. | Coal gasification composite power generating plant |
| 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 |
| JPH09194855A (en) * | 1996-01-12 | 1997-07-29 | Hitachi Ltd | Power generation plant by combination of gasification and improved heat exchange and method for operating it |
-
2010
- 2010-08-20 CN CN2010102587182A patent/CN102373097B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0129167A2 (en) * | 1983-06-10 | 1984-12-27 | Hitachi, Ltd. | Coal gasification composite power generating plant |
| 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 |
| JPH09194855A (en) * | 1996-01-12 | 1997-07-29 | Hitachi Ltd | Power generation plant by combination of gasification and improved heat exchange and method for operating it |
Non-Patent Citations (2)
| Title |
|---|
| 冷雪峰等: "煤气化及其多联产系统技术的发展现状", 《上海电力学院学报》 * |
| 陈秋雄等: "天然气管网压力能利用与水合物联合调峰研究", 《煤气与热力》 * |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103555371A (en) * | 2013-11-15 | 2014-02-05 | 华东理工大学 | Method for improving gasification efficiency of slurry feed gasification device |
| CN105152509B (en) * | 2015-09-10 | 2017-11-14 | 新奥科技发展有限公司 | The supercritical processing methods of supercritical reaction device, supercritical reaction system and sludge |
| CN105152509A (en) * | 2015-09-10 | 2015-12-16 | 新奥科技发展有限公司 | Supercritical reactor, supercritical reaction system and supercritical treatment method of sludge |
| CN105505465A (en) * | 2015-11-19 | 2016-04-20 | 万伟 | Method for using carbon-containing raw material to produce synthesis gas |
| CN105505465B (en) * | 2015-11-19 | 2018-04-17 | 万伟 | A kind of method using carbon raw material production synthesis gas |
| CN105971679A (en) * | 2016-07-13 | 2016-09-28 | 西安热工研究院有限公司 | Supercritical water gasification and supercritical carbon dioxide Brayton cycle joint production system |
| CN105971679B (en) * | 2016-07-13 | 2017-09-12 | 西安热工研究院有限公司 | Supercritical water gasification and supercritical carbon dioxide Brayton cycle Joint Production system |
| CN106147865A (en) * | 2016-07-19 | 2016-11-23 | 西安交通大学 | The method and apparatus of continuous supercritical water double tube reactor gasification organic matter |
| CN106147865B (en) * | 2016-07-19 | 2019-10-01 | 陕西中核交大超洁能源技术有限公司 | The method and apparatus of continuous supercritical water double tube reactor gasification organic matter |
| CN111201307A (en) * | 2017-06-14 | 2020-05-26 | 多元伙伴公司 | Aftertreatment arrangement and method for the aftertreatment of gases at least downstream of a fluidized bed gasification process, and logic unit and use |
| CN113048465A (en) * | 2021-03-26 | 2021-06-29 | 中国科学院工程热物理研究所 | Coal-fired power generation system and method for coal gasification with supercritical water |
| CN113048465B (en) * | 2021-03-26 | 2022-08-12 | 中国科学院工程热物理研究所 | Coal-fired power generation system and method for coal gasification with supercritical water |
| CN116590053A (en) * | 2023-07-17 | 2023-08-15 | 太原理工大学 | Method and device for producing hydrogen by efficiently gasifying coal |
| CN116590053B (en) * | 2023-07-17 | 2023-09-08 | 太原理工大学 | Method and device for producing hydrogen by efficiently gasifying coal |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102373097B (en) | 2013-12-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102373097B (en) | Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process | |
| CN102518489B (en) | Electricity-generating method, the device generated electricity for gasified production of energy products and heat | |
| KR101739494B1 (en) | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation | |
| KR101767287B1 (en) | System for heat integration with methanation system | |
| Darmawan et al. | Black liquor-based hydrogen and power co-production: Combination of supercritical water gasification and syngas chemical looping | |
| CN106414330B (en) | The technique for producing ammonia and its derivative, especially urea | |
| CN101432571A (en) | Process for superheated steam | |
| CN102079685A (en) | Coal gasification process for methane preparation by two stage gasification stove | |
| CN100503790C (en) | Method of producing chemical product by double fuel reforming chemical system | |
| Prakash et al. | Proposal and design of a new biomass based syngas production system integrated with combined heat and power generation | |
| US20090300976A1 (en) | Hybrid energy conversion system and processes | |
| Wei et al. | Process simulation and economic analysis of calcium looping gasification for coal to synthetic natural gas | |
| CN102559269B (en) | Method for combining coal gasification process and vapor turbine power generation process | |
| 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 | |
| Ajiwibowo et al. | Co-production of hydrogen and power from black liquor via supercritical water gasification, chemical looping and power generation | |
| 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 | |
| Larson et al. | Production of hydrogen and methanol via biomass gasification | |
| CN105505465B (en) | A kind of method using carbon raw material production synthesis gas | |
| CN102373098B (en) | Coupling method of coal gasification technology and steam turbine generating technology | |
| CN218909867U (en) | Carbon-containing fuel CO 2 In-situ trapping hydrogen production poly-generation system | |
| CN217127311U (en) | Device for synthesizing methanol by double-carbon hydrogenation | |
| CN211111887U (en) | Thermal power plant pyrolysis of coal gas hydrogen manufacturing system |
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 |