CN102518489A - Power generation method, and device for gasified production of energy products and thermal power generation - Google Patents
Power generation method, and device for gasified production of energy products and thermal power generation Download PDFInfo
- Publication number
- CN102518489A CN102518489A CN2012100025334A CN201210002533A CN102518489A CN 102518489 A CN102518489 A CN 102518489A CN 2012100025334 A CN2012100025334 A CN 2012100025334A CN 201210002533 A CN201210002533 A CN 201210002533A CN 102518489 A CN102518489 A CN 102518489A
- Authority
- CN
- China
- Prior art keywords
- gas
- heat exchanger
- water
- exhaust steam
- condenser
- 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
Landscapes
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The invention provides a power generation method, comprising a step of condensing exhausted steam generated in the power generation process, wherein a heat exchange operation is directly or indirectly carried out between the exhausted steam and gas obtained after expanded depressurization. The invention further provides a device for gasified production of energy sources and thermal power generation. The device comprises an expansion depressurization device and a condenser, wherein the expansion depressurization device comprises an expansion depressurization inlet for receiving gas to be subjected to an expanded depressurization operation, and an expansion depressurization outlet for discharging the gas subjected to the expanded depressurization operation; and the condenser comprises a first heat exchange channel in which a cooling medium with the refrigerating capacity of the gas subjected to the expanded depressurization operation enters, and a second heat exchange channel in which the heat exchange operation is carried out between the exhausted steam generated in the power generation process and the cooling medium. According to the method and the device disclosed by the invention, the refrigerating capacity generated by the gas subjected to the expanded depressurization operation is used, so that the temperature of the exhausted steam is reduced below an environmental temperature, therefore the pressure energy of the gas is sufficiently used, and the power generation efficiency of turbine power generation equipment is improved.
Description
Technical field
The present invention relates to a kind of electricity-generating method and the device of be used to gasify production energy products and heat generating.
Background technique
IGCC (integrated gasification combined cycle plants) technology has realized gasification is combined with the gas and steam turbine combined generating system, is a kind of clean coal power generation technology.The oxygen that coal after the processing and air separation unit come generates mixed gas in gasification oven; The sensible heat of mixed gas produces steam through reclaiming; Mixed gas purifies back, combustion driven gas turbine power generation through clean unit; The heat energy of the flue gas that gas turbine is discharged reclaims, heats generation steam through exhaust heat boiler, the generating of steam driven steam turbine.In IGCC technology; Utilize this product stream thigh of mixed gas at first through gas turbine Brayton circulating generation; The fume afterheat of heat exchange and/or discharge of gas turbine is heated into steam with water, steam and then drive the steam turbine turbine power generation through Rankine circulation.The coupling or the synergy of relatively independent between coal gasifying process and Brayton circulation and the Rankine circulation technology, lack of depth; Be the Influence of Temperature of the Rankine circuit generating efficiency steam that only receives to be produced, coal gasifying process does not directly influence Rankine circuit generating efficiency.In other words, more than the technology of gasification and steam turbine generation associating has only been utilized by the steam thermal energy that produces in the coal gasification course, promptly only coal gasifying process and steam turbine generation method are got in touch by the steam of the generation in the coal gasification course.If the product of gasification not exclusively is used to the produce power of burning; But production energy products; Like methane, hydrogen and carbon monoxide etc., then the step optimization utilization of gasification and gas and steam turbine combined generating system energy and the degree of coupling between cell process all need further to improve.
In addition, the steam turbine generating is used based on Rankine circuit thermodynamic process usually.A desirable Rankine circulation, its thermal efficiency (generating efficiency) depends on the temperature and pressure of endothermic process and exothermic process.For the exothermic process that in steam turbine, carries out, the temperature that reduces exhaust steam can improve Rankine thermal efficiency of cycle (generating efficiency), but the temperature of exhaust steam 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 cooling medium of steam cooling part is often used cooling water usually.Because the restriction of cooling water medium, the steam that goes out turbine engine is that the temperature of exhaust steam is controlled at more than the ambient temperature usually.For example, the common operating mode of cooling water is gauge pressure 0.52MPa, 32 ℃ of temperature, thus limited being controlled at usually more than 32 ℃ of exhaust steam.(introduce in detail about the Rankine circuit, see also " the practical pandect of modern coal conversion and Coal Chemical Industry new technology new 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).
Desirable Rankine circulation also can use tephigram as shown in Figure 7 (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. 7.Wherein heat absorption (1 → 2 → 3 → 4) and the exothermic process (5 → 6) in the circulation is isopiestic process, and expansion of steam (4 → 5) and the condensed water process (6 → 1) of boosting is an isentropic process.
In addition; In the material direct generation of electricity such as the material of high water content such as brown coal, mud coal, mud and rubbish or the gasification, contain a large amount of steam in flue gas or the product gas, because the latent heat of water evaporation is very big; Cause great amount of heat to be walked, obviously reduce generating and gasification efficiency by the flue gas or the product band of gas.
Supercritical technology and generation technology coupling are arranged in the existing supercritical technology, and main mode is to utilize the heat energy of product to carry out turbine power generation through the steam that heat exchange produces, but can utilize the pressure of product gas.
The generation technology that combines with coal chemical technology, only the steam by the generation in the coal gasification course is got in touch coal gasifying process and steam turbine generation method.
Existing steam turbine generation technology exhaust steam temperature is controlled at more than the ambient temperature, has limited generating efficiency.
In addition, the material direct generation of electricity of high water content, great amount of heat is taken away by water vapor and flue gas, obviously reduces generating efficiency.
Existing technology is not applied to the high pressure energy of the product that supercritical water oxidation/gasification technology produces.The energy of system fails to be fully used.
Summary of the invention
To the problem that exists in the correlation technique; The object of the present invention is to provide a kind of electricity-generating method and the device of be used to gasify production energy products and heat generating; To utilize cold through the gas generation of expansion step-down; The temperature of exhaust steam is reduced to below the ambient temperature; Both made full use of gas pressure can, again the temperature increase through reducing exhaust steam in the Rankine circulation generating efficiency of turbine power generation equipment, thereby the lifting that has realized producing the energy products and the whole efficiency of energy utilization of the device of heat generating.
On the one hand, the present invention provides a kind of electricity-generating method, comprises the step that condensation is carried out in exhaust steam that when generating produced, in this step, makes said exhaust steam carry out heat exchange with gas through the overexpansion step-down directly or indirectly.
Preferably, said heat exchange is carried out in condenser, said condenser with by described water after the gas cooling of overexpansion step-down as cooling medium, said exhaust steam is directly carried out heat exchange with said cooling medium in said condenser.
Preferably, heat exchange is carried out in condenser, said condenser directly with described gas through the overexpansion step-down as cooling medium, said exhaust steam is directly carried out heat exchange with said cooling medium in said condenser.
Preferably; Heat exchange is carried out in condenser; Said condenser comprises first portion and second portion; The cooling medium of said first portion is a water, and the cooling medium of said second portion is described gas through the overexpansion step-down, and the cooling medium in said exhaust steam and said first and second parts directly carries out heat exchange.
Preferably, this method also comprises: raw material is sent in the reactor surpassed/subcritical gasification reaction or oxidation reaction formation reaction mixture; Wherein, described gas through the overexpansion step-down is the gas of from reaction mixture, separating to be expanded obtain after the step-down.
Preferably, this method also comprises: said reaction mixture is imported in second heat exchanger carry out heat exchange with generating working medium; Generate electricity in the generating working medium importing turbine engine with the said reaction mixture of absorption institute heat content; And to utilize described gas generation energy products through the overexpansion step-down, said energy products be methane or hydrogen or carbon monoxide or electricity or their combination in any.
Preferably, this method is lower than ambient temperature through the temperature of the gas of overexpansion step-down, and this ambient temperature is meant 28-32 ℃.
Preferably, this method raw material is coal, living beings, mud or waste water, contains gasifying agent or oxygenant in the said reactor, and said gasifying agent or oxygenant are oxygen, steam, oxygen-enriched air, airborne at least a.
Preferably, generating working medium is water or carbon dioxide or isoparaffin.
Temperature conditions when preferably, ultra/subcritical gasification reaction or oxidation reaction take place in said reactor raw material is that 350-750 ℃, pressure condition are 15-40MPa.
Preferably, the pressure that has 0.1-7MPa through the gas of overexpansion step-down.
Preferably, the gas through the overexpansion step-down has-25～20 ℃ temperature.
Preferably, the gas that comprises of reaction mixture be raw material ultra/gas that gas that subcritical gasification reaction produces or raw material oxidation reaction produce.
On the other hand, the present invention also provide a kind of be used to gasify produce the device of energy products and heat generating, comprising: the expansion dropping equipment has the expansion step-down inlet that receives the step-down gas of waiting to expand, and discharges the expansion step-down outlet through the gas of overexpansion step-down; And condenser, have first heat exchanger channels that supplies to be loaded with the cooling medium from the cold of said gas through the overexpansion step-down and get into, and the exhaust steam that supplies generating to produce get into wherein with said first heat exchanger channels in second heat exchanger channels of cooling medium heat exchange.
Preferably, the gas through the overexpansion step-down gets into said first heat exchanger channels as said cooling medium.
Preferably; Apparatus of the present invention also comprise first heat exchanger; Gas through the overexpansion step-down gets into a heat exchanger channels in first heat exchanger, and carries out heat exchange with cooling water in another heat exchanger channels of first heat exchanger, wherein; With said cooling water behind the gas converting heat of overexpansion step-down, be discharged to first heat exchanger channels of said condenser as cooling medium from described another heat exchanger channels.
Preferably; Condenser comprises first portion and second portion; Said first and second heat exchanger channels are located in the said first portion, and said second portion has exhaust steam entering one of them heat exchanger channels and the confession of confession after the heat release of said first portion and gets into another heat exchanger channels wherein in order to the water that cools off exhaust steam in this heat exchanger channels.
Preferably, apparatus of the present invention also comprise: use the reactor that reacts therein for raw material, have the relief opening of the reaction mixture discharge that supplies the reaction generation; Supply reaction mixture and generating working medium second heat exchanger of heat exchange each other, have is communicated with said relief opening in order to the heat transferring medium inlet that receives reaction mixture and will export from the generating working medium of the generating working medium discharge after the reaction mixture heat absorption; Utilize the turbine engine of the generating working medium generating after absorbing heat; Have is communicated with generating working medium outlet in order to the import that receives the generating working medium after the heat absorption, and the exhaust steam that supplies generating the to produce exhaust steam outlet of discharging, said exhaust steam outlet enters the mouth with the exhaust steam of said condenser and is communicated with.
Preferably, apparatus of the present invention also comprise and are connected segregating unit that gas separation in the reaction mixture is come out between said second heat exchanger and the said expansion dropping equipment.
Preferably, apparatus of the present invention also comprise gas turbine, and said gas turbine has fuel gas inlet, and said condenser has the outlet that the expansion step-down gas behind confession and the said exhaust steam heat-shift is discharged, and this outlet is communicated with said fuel gas inlet.
Preferably; Apparatus of the present invention also comprise gas turbine; Said gas turbine has fuel gas inlet, and said first heat exchanger has the outlet that the expansion step-down gas after the cooling water heat exchange in another heat exchanger channels is discharged described in confession and this first heat exchanger, and this outlet is communicated with said fuel gas inlet.
Preferably, apparatus of the present invention also comprise compression pump, have pump intake and pump discharge; Wherein, Said second heat exchanger has the inlet that supplies generating working medium to flow into, and this inlet is communicated with the pump discharge of said compression pump, wherein; Said condenser has the outlet that the saturation water that generates after the exhaust steam condensation is discharged, and this outlet is communicated with the pump intake of said compression pump.
Preferably; Apparatus of the present invention also comprise: the device that utilizes gas generation energy products after the expansion step-down be absorbed behind the cold; Has the inlet that gas gets into after the said expansion step-down that supplies to be absorbed behind the cold; Wherein, said condenser has the outlet that the expansion step-down gas behind confession and the said exhaust steam heat-shift is discharged, and this outlet is communicated with the said inlet of the device of said production energy products.
Preferably; Apparatus of the present invention also comprise: the device that utilizes gas generation energy products after the expansion step-down be absorbed behind the cold; Has the inlet that gas gets into after the said expansion step-down that supplies to be absorbed behind the cold; Wherein, said first heat exchanger has the outlet that the expansion step-down gas after the cooling water heat exchange in said another heat exchanger channels in confession and this first heat exchanger is discharged, and this outlet is communicated with the said inlet of the device of said production energy products.
Among the present invention; The heat exchanger that is adopted can be any suitable heat exchanger that is used for indirect heat exchange, for example tubular heat exchanger, finned heat exchanger etc., and the type of these heat exchangers is well known to a person skilled in the art with concrete structure; Condenser essence also is heat exchanger, repeats no more here.The expansion gear that is adopted comprises step-down capillary tube, dropping valve, decompressor etc., and the method and apparatus of gas expansion step-down all well known to a person skilled in the art, repeats no more at this.
Method and apparatus of the present invention has following beneficial effect: make the exhaust steam of from turbine engine, discharging carry out heat exchange with gas through the overexpansion step-down directly or indirectly; Utilize and to produce the cooling medium lower (for example-25～20 ℃ gas) after the expansion step-down through the overexpansion step-down than ambient temperature (28-32 ℃); With exhaust steam cooling, condensation, the pressure that had both made full use of generating working medium can generate electricity; Improved the generating efficiency of turbine power generation equipment; Produce more clean electric power; Being fit to of can making full use of also that gasification equal energy source production technology produced wait to expand the step-down acting gas pressure can, this energy also can be used for generating, thereby improves the energy utilization efficiency of whole process system.
In more detail; The present invention is because to the step-down of expanding from the gas in the reaction mixture that generates after ultra/subcritical gasification reaction or the oxidation reaction; Gas temperature after the expansion step-down can be reduced to below the ambient temperature (for example 0 ℃); Utilize the gas after the expansion step-down that condensation is carried out in exhaust steam then; Therefore utilize gas after the overexpansion step-down, can produce the cooling medium lower (for example-25～20 ℃ gas) through the overexpansion step-down than ambient temperature; The cooling water (generally using 32 ℃ of water as cooling medium) of cooling steam when replacing the steam turbine turbine power generation that common Rankine circulation drives just can be lowered the temperature to the more exhaust steam of low temperature (for example 5～10 ℃), condensation, and the temperature of exhaust steam just can be provided with lowlyer (for example is lower than common ambient temperature; Like 18～27 ℃ of room temperatures), just can improve the generating efficiency of turbine power generation equipment.Than existing technology; The cooling water that the present invention adopts the cooling medium lower than ambient temperature that produce through the overexpansion step-down (gas through the overexpansion step-down for example-25～20 ℃ is preferably 0～20 ℃) to come directly to substitute or part substitutes common ambient temperature to exhaust steam lower the temperature, condensation, or indirect utilization is through the cold of the gas of overexpansion step-down (for example; Cooling water through to ambient temperature cools off; Again with this cooling water to exhaust steam lower the temperature, condensation), just can with the temperature of exhaust steam be provided with lower, not only can improve the generating efficiency of turbine power generation equipment; And; The expansion step-down process acting that can also utilize ultra/subcritical gasification reaction or oxidation reaction to produce living gas is generated electricity, and has further increased generated energy, has improved whole process system energy utilization efficiency.
Further utilized the above-mentioned gas cooling exhaust steam after the expansion step-down, in existing technology, only utilized the water quench exhaust steam, the present invention correspondingly just can reduce the consumption consumption of cooling water, thereby saves cooling water.
Moreover; Isolated gas the reaction mixture that generates during from ultra/subcritical gasification reaction or oxidation reaction; Handle owing to carried out the expansion step-down, in the heat exchange of process with exhaust steam, temperature and pressure is relatively gentleer; Therefore be convenient to follow-up processing, for example be convenient to carry out separating treatment to produce energy products or to get into follow-up gas turbine combustion generating.
Description of drawings
Fig. 1 is the embodiment's 1,4,5,6 of electricity-generating method of the present invention indicative flowchart;
Fig. 2 is the indicative flowchart of the embodiment 2-3 of electricity-generating method of the present invention;
Fig. 3 is the embodiment's 7 of electricity-generating method of the present invention indicative flowchart;
Fig. 4 is the embodiment's 8 of electricity-generating method of the present invention indicative flowchart;
Fig. 5 is the embodiment's 9 of electricity-generating method of the present invention indicative flowchart;
Fig. 6 is the embodiment's 10 of electricity-generating method of the present invention indicative flowchart;
Fig. 7 is Rankine circuit tephigram (T-S figure).
Embodiment
The present invention provides a kind of electricity-generating method; It comprises the step that condensation is carried out in exhaust steam that when generating produced: make exhaust steam carry out heat exchange with gas through the overexpansion step-down directly or indirectly; In other words; In this step, exhaust steam absorbs in condenser through the contained cold of the gas of overexpansion step-down with by cooling, condensation.Preferably, condenser with by described water after the gas cooling of overexpansion step-down as cooling medium; Perhaps condenser directly with described gas through the overexpansion step-down as cooling medium; Perhaps condenser comprises first portion and second portion, and the cooling medium of first portion is a water, and the cooling medium of second portion is described gas through the overexpansion step-down.
Further, electricity-generating method of the present invention also comprises will the expand step of step-down gas of following generation: raw material is sent in the reactor surpassed/subcritical gasification reaction or oxidation reaction formation reaction mixture; Wherein, described gas through the overexpansion step-down is the gas of from reaction mixture, separating to be expanded obtain after the step-down.In order to generate electricity, aforesaid reaction mixture to be imported in second heat exchanger carry out heat exchange with generating working medium; Generate electricity in the generating working medium importing turbine engine with absorption reaction mixture institute heat content then.The gas that wherein expands after the step-down can also be used to produce energy products after discharging its cold.
Below referring to accompanying drawing, electricity-generating method of the present invention is described in detail.
[embodiment 1]
Referring to Fig. 1, be water with the generating working medium, the catalytic gasification that bituminous coal and supercritical water take place is an example.Coal is processed granularity less than 150 microns coal dust, with catalyst n a through pulverize grinding
2CO
3It is 40% water coal slurry that (consumption be quality of pc 10%) and water are prepared into coal dust butt concentration.Water coal slurry is through pressurization, and preheating reaches 23MPa, and 550 ℃ get into (reactor is a gasification oven among this embodiment), aerating oxygen (gasifying agent is an oxygen among this embodiment) in gasification oven simultaneously in the reactor.The oxygen reaction of part water coal slurry and adding in gasification oven is with temperature increase to 650 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the mixed gas that is rich in methane.The main component of mixed gas is a methane, carbon monoxide, carbon dioxide, hydrogen etc.Comprise mixed gas, supercritical water and reaction back residue from gasification oven through the reacted pyroreaction mixture of supercritical gasification (that is, go out the reaction of gasification oven after mixture) product.This product with from 23MPa water heat exchange in second heat exchanger of compression 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 turbine engine (being steam turbine among this embodiment) expansion power generation; It is 0.00087MPa that this exhaust steam can be controlled in pressure, and temperature is 5 ℃, and exhaust steam gets into condenser condenses Cheng Shui.The mixed gas of from reaction mixture, separating after the heat exchange gets into clean unit, and with mixed gas and water, slag separates; Mixed gas after the separation is through the overexpansion step-down; Pressure is reduced to 5.68MPa, and temperature is reduced to 0 ℃, is used as the cooling medium of above-mentioned condenser then; Exhaust steam is carried out heat exchange to be condensed into liquid water with cooling medium in condenser, this mixed gas can get into the later separation unit or get into follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 36.30% in this case.From the water of condenser after the pump pressurization, turn back in second heat exchanger with from gasification oven behind gasification reaction the pyroreaction mixture carry out heat exchange, to produce high temperature and high pressure steam again.
[embodiment 2]
With reference to Fig. 2, being generating working medium with water also, is example with the supercritical water gasification of bituminous coal.Bituminous coal process wet grinding machine grinds and processes concentration is 50% water coal slurry, delivers in the gasification oven (reactor is a gasification oven among this embodiment) through the pump pressurization then.Aerating oxygen or air are as gasifying agent in gasification oven simultaneously, and the operating temperature of gasification oven is about 750 ℃, and operation pressure is 27.0MPa.Coal and above-mentioned gasifying agent at high temperature react, and generate the coal gas that is rich in carbon monoxide, hydrogen, carbon dioxide, methane.Mixture comprises coal gas and tar and unreacted gasifying agent etc. completely after going out the reaction of gasification oven.Make this reaction back mixture and 23MPa water heat exchange in second heat exchanger from compression pump; And to make pressurized water become temperature be that 400 ℃ and absolute pressure are 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 0.0025MPa that this exhaust steam can be controlled in pressure, and temperature is 21.08 ℃, and exhaust steam gets into condenser condenses and becomes liquid water.Mixture gets into segregating unit after the reaction after the heat exchange; With coal gas and water; Slag separates, and the pressure after the overexpansion step-down of the coal gas after the separation is reduced to 5.00MPa, and temperature is reduced to-2.82 ℃; In first heat exchanger, using it then is 32 ℃ water quench to 18 ℃ with temperature; This coal gas can get into subsequent separation process or get into follow-up gas turbine combustion generating afterwards, and the cooled cooling water of the coal gas after the expansion step-down then is used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water.Generating efficiency is through being calculated as 35.53% in this case.After the pump pressurization, turn back in second heat exchanger and carry out heat exchange from the water of condenser, to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 3]
Referring to Fig. 2, with water generating working medium, the catalytic gasification that takes place with brown coal and supercritical water is example.Coal is prepared into granularity less than 150 microns water coal slurry through wet mill, and water coal slurry concentration is 35%, contains catalyzer K in the water coal slurry
2CO
3(consumption be quality of pc 3%).Water coal slurry is through pressurization, and preheating reaches 35MPa, and 450 ℃ get into gasification oven (reactor is a gasification oven among this embodiment), aerating oxygen in gasification oven simultaneously.The oxygen reaction of part water coal slurry and adding in gasification oven is with temperature increase to 570 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the mixed gas that is rich in methane.The main component of mixed gas is a methane, carbon monoxide, carbon dioxide, hydrogen etc.Go out the gasification oven product and comprise mixed gas, supercritical water and reaction back residue.This product with from 23MPa water heat exchange in second heat exchanger of compression pump; Produce high temperature and high pressure steam, become exhaust steam behind the entering steam turbine expansion power generation, it is 0.0024MPa that this exhaust steam can be controlled in pressure; Temperature is 20.34 ℃, and exhaust steam gets into condenser condenses and becomes liquid water.Mixed gas after the heat exchange gets into clean unit; With mixed gas and water; Slag separates, and the mixed gas after the separation is reduced to 4.76MPa through overexpansion step-down pressure, and temperature is reduced to-4.73 ℃; In first heat exchanger, using it then is 28 ℃ water quench to 16 ℃ with temperature; This mixed gas can get into subsequent separation process or get into follow-up gas turbine combustion generating afterwards, and the cooled cooling water of the mixed gas after the expansion step-down then is used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water.Generating efficiency is through being calculated as 35.65% in this case.After the pump pressurization, turn back in second heat exchanger and carry out heat exchange from the water of condenser (saturation water that is condensed into by exhaust steam), to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 4]
Referring to Fig. 1, be generating working medium with water, be example with the complete oxidation of high-concentration waste water.With concentration is that 7% high-concentration waste water tentatively filters.With being delivered to gasification oven after the waste water pressurization, aerating oxygen and steam are as gasifying agent in gasification oven simultaneously, and the operating temperature of gasification oven is about 450 ℃, and operation pressure is 15MPa.Carbonaceous material in the waste water and above-mentioned gasifying agent at high temperature react, and generate carbon dioxide and water.Mixture comprises gaseous product, solid residue and unreacted gasifying agent etc. completely after going out the reaction of gasification oven.Make this reaction back mixture and 23MPa water heat exchange in heat exchanger from compression pump; And make pressurized water become high temperature and high pressure steam; 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 25.16 ℃, and exhaust steam gets into condenser condenses and becomes liquid water.Mixture gets into segregating unit after the reaction after the heat exchange; With product and water, slag separates, and the pressure after the overexpansion step-down of the gas after the separation is reduced to 6.11MPa; Temperature is reduced to 2.5 ℃; As the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water, this coal gas can get into the later separation processing procedure afterwards then.Generating efficiency is through being calculated as 35.33% in this case.After the pump pressurization, turn back in the heat exchanger and carry out heat exchange from the water of condenser (saturation water that is condensed into by exhaust steam), to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 5]
Referring to Fig. 1, be generating working medium with water, with the Supercritical Water Oxidation of Municipal Sludge example.After the mud purification of raw materials, and to be mixed with concentration with water be 15% slurry.Aerating oxygen and steam are as gasifying agent in gasification oven simultaneously, and the operating temperature of gasification oven is about 480 ℃, and operation pressure is 24MPa.Carbonaceous material in the mud and above-mentioned gasifying agent at high temperature react, and generate carbon dioxide and water.Mixture comprises gaseous product, solid residue and unreacted gasifying agent etc. completely after going out the reaction of gasification oven.Make this reaction back mixture and 23MPa water heat exchange in second heat exchanger from compression pump; And make pressurized water become high temperature and high pressure steam; This high temperature and high pressure steam becomes exhaust steam after getting into the steam turbine expansion power generation; It is 0.0023MPa that this exhaust steam can be controlled in pressure, and temperature is 19.57 ℃, and exhaust steam gets into condenser condenses Cheng Shui.Mixture gets into segregating unit after the reaction after the heat exchange; With product gas and water, slag separates, and the gas after the separation is reduced to 7.00MPa through overexpansion step-down pressure; Temperature is reduced to 5.79 ℃; As the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into liquid water, this gas can get into the later separation processing procedure afterwards then.Generating efficiency is through being calculated as 35.76% in this case.After the pump pressurization, turn back in second heat exchanger and carry out heat exchange from the water of condenser (saturation water that is condensed into by exhaust steam), to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 6]
With reference to Fig. 1, being generating working medium with water also, is example with the supercritical water gasification of maize straw.Maize straw mixes with water through pulverize grinding to process behind the coal dust that to process concentration be 20% biological chylema, delivers in the gasification oven (reactor is a gasification oven among this embodiment) through the pump pressurization then.Aerating oxygen or air are as gasifying agent in gasification oven simultaneously, and the operating temperature of gasification oven is about 600 ℃, and operation pressure is 40MPa.Maize straw and above-mentioned gasifying agent at high temperature react, and generate the gaseous mixture that is rich in carbon monoxide, hydrogen, carbon dioxide, methane.Mixture comprises gaseous product, tar and unreacted gasifying agent etc. completely after going out the reaction of gasification oven.Make this reaction back mixture and 23MPa water heat exchange in second heat exchanger from compression pump; And make pressurized water become high temperature and high pressure steam; This high temperature and high pressure steam becomes exhaust steam after getting into the steam turbine expansion power generation; It is 0.0015MPa that this exhaust steam can be controlled in pressure, and temperature is 13.02 ℃, and exhaust steam gets into condenser condenses and becomes liquid water.Mixture gets into segregating unit after the reaction after the heat exchange; With coal gas and water, slag separates, and the mixed gas after the separation is reduced to 2.33MPa through overexpansion step-down pressure; Temperature is reduced to-24.42 ℃; As the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water, this mixed gas can get into subsequent separation process or get into follow-up gas turbine combustion generating afterwards then.Generating efficiency is through being calculated as 36.15% in this case.After the pump pressurization, turn back in second heat exchanger and carry out heat exchange from the water of condenser (saturation water that is condensed into by exhaust steam), to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 7]
With reference to Fig. 3, be generating working medium with water, 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% water coal slurry that (consumption be quality of pc 5%) and water are prepared into coal dust butt concentration.Water coal slurry is through pressurization, and preheating reaches 30MPa, and 550 ℃ get into gasification oven (reactor is a gasification oven among this embodiment), aerating oxygen in gasification oven simultaneously.The oxygen reaction of part water coal slurry and adding in gasification oven is with temperature increase to 680 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the mixed gas that is rich in methane.The main component of mixed gas is a methane, carbon monoxide, carbon dioxide, hydrogen etc.Go out the gasification oven product and comprise mixed gas, supercritical water and reaction back residue.This reaction back mixture and 23MPa water heat exchange in second heat exchanger from compression pump; Produce high temperature and high pressure steam, become exhaust steam behind the entering steam turbine expansion power generation, it is 34.16 ℃ that this exhaust steam can be controlled in temperature; Absolute pressure is 0.0053Mpa, and exhaust steam gets into condenser condenses and becomes liquid water.Mixed gas after the heat exchange gets into segregating unit, and with mixed gas and water, slag separates; Mixed gas after the separation is reduced to 3.67MPa through overexpansion step-down pressure, and temperature is reduced to-11.57 ℃, is used as the cooling medium of above-mentioned condenser then; So that exhaust steam is condensed into water; Meanwhile, also in this condenser, feeding temperature with pipeline independently is 28 ℃ normal temperature cooling water, jointly exhaust steam is cooled off; For example condenser is made as first and second parts; Wherein the cooling medium of first portion be the cooling medium of cooling water and second portion for the gas of from react the back mixture, separating after the expansion step-down, utilize first portion that the condensation first time is carried out in exhaust steam earlier, utilize second portion that the condensation second time is carried out in exhaust steam then.This mixed gas can get into subsequent separation process or get into follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 35.13% in this case.After the pump pressurization, turn back in second heat exchanger and carry out heat exchange from the water of condenser (saturation water that is condensed into by exhaust steam), to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 8]
With reference to Fig. 4, be generating working medium with water, 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 45% water coal slurry that (consumption be quality of pc 2%) and water are prepared into coal dust butt concentration.Water coal slurry is through pressurization, and preheating reaches 28MPa, and 550 ℃ get into gasification oven (reactor is a gasification oven among this embodiment), aerating oxygen in gasification oven simultaneously.The oxygen reaction of part water coal slurry and adding in gasification oven is with temperature increase to 700 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the mixed gas that is rich in methane.The main component of mixed gas is a methane, carbon monoxide, carbon dioxide, hydrogen etc.Go out the gasification oven product and comprise mixed gas, supercritical water and reaction back residue.This reaction back mixture and 23MPa water heat exchange in second heat exchanger from compression pump; Produce high temperature and high pressure steam, become exhaust steam behind the entering steam turbine expansion power generation, it is 21.08 ℃ that this exhaust steam can be controlled in temperature; Absolute pressure is 0.0025MPa, and exhaust steam gets into condenser condenses and becomes liquid water.Mixed gas after the heat exchange gets into segregating unit; With mixed gas and water; Slag separates; Mixed gas after the separation is reduced to 2.67MPa through overexpansion step-down pressure, and temperature is reduced to-20.67 ℃, and this mixed gas and conventional cooling water flow thigh carry out heat exchange in first heat exchanger then; To leave then this first heat exchanger mixed gas and generation the cooled cooling water of the mixed gas after the expansion step-down with separately independently pipeline feed respectively and be used as cooling medium in the condenser; (this moment, condenser had first and second parts, and wherein the cooling medium of first portion is the above-mentioned cooled cooling water of the mixed gas after the expansion step-down, and the cooling medium of second portion is the mixed gas that leaves this first heat exchanger jointly exhaust steam is condensed into water; Utilize first portion's condensation exhaust steam to utilize second portion to continue the condensation exhaust steam more earlier, this mixed gas can get into subsequent separation process or get into follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 35.43% in this case.After the pump pressurization, turn back in second heat exchanger and carry out heat exchange from the water of condenser (saturation water that is condensed into by exhaust steam), to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 9]
With reference to Fig. 5, be generating working medium with water, 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% water coal slurry that (consumption be quality of pc 6%) and water are prepared into coal dust butt concentration.Water coal slurry is through pressurization, and preheating reaches 23MPa, and 550 ℃ get into gasification oven (reactor is a gasification oven among this embodiment), aerating oxygen in gasification oven simultaneously.The oxygen reaction of part water coal slurry and adding in gasification oven is with temperature increase to 650 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the mixed gas and the slurry-like residual carbon that are rich in methane.The main component of mixed gas is a methane, carbon monoxide, carbon dioxide, hydrogen etc.Mixture comprises mixed gas and slurry-like residual carbon after going out the reaction of gasification oven.This product with from 23MPa water heat exchange in second heat exchanger of compression 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 0.0022MPa that this exhaust steam can be controlled in pressure, and temperature is 18.77 ℃, 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; Mixed gas after the separation is reduced to 3.33MPa through overexpansion step-down pressure; Temperature is reduced to-14.31 ℃; As the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into liquid water, this mixed gas can get into the later separation unit or get into follow-up gas turbine combustion generating afterwards then.Slurry-like residual carbon then is transported in the oxidation reactor.In this oxidation reactor, feed excessive oxygen, and the oxidation 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.Oxidation 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 structural material.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 liquide water and atmospheric carbon dioxide.Then this cryogenic liquide water also is passed in the said condenser, be used for said expansion step-down after mixed gas come together exhaust steam is cooled to condensed water.Generating efficiency is through being calculated as 35.88% in this case.To after pump pressurization, turn back in second heat exchanger and carry out heat exchange from this condensed water then, to produce high temperature and high pressure steam again from mixture after the reaction of the high temperature of gasification oven.
[embodiment 10]
With reference to Fig. 6, be generating working medium with water, 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% water coal slurry that (consumption be quality of pc 2%) and water are prepared into coal dust butt concentration.Water coal slurry is through pressurization, and preheating reaches 23MPa, and 550 ℃ get into gasification oven (reactor is a gasification oven among this embodiment), aerating oxygen in gasification oven simultaneously.The oxygen reaction of part water coal slurry and adding in gasification oven is with temperature increase to 650 ℃.Under supercritical state, coal and water react under the effect of catalyzer, generate the mixed gas and the slurry-like residual carbon that are rich in methane.The main component of mixed gas is a methane, carbon monoxide, carbon dioxide, hydrogen etc.Mixture comprises mixed gas and slurry-like residual carbon after going out the reaction of gasification oven.This product with from 23MPa water heat exchange in second heat exchanger of compression 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 0.0019MPa that this exhaust steam can be controlled in pressure, and temperature is 17.05 ℃, and exhaust steam gets into condenser condenses, and to become temperature be 16.88 ℃ liquid water.Mixture entering separator carries out gas/liquid-solid separation after the reaction after the heat exchange; Mixed gas after the separation is reduced to 3.67MPa through overexpansion step-down pressure; Temperature is reduced to-11.57 ℃; Be incorporated into certain heat exchanger (this heat exchanger is not a heat exchanger with the heat exchanger that usefulness generates said steam) then and as cooling medium cooling water cooled off, this mixed 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 oxidation 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.Oxidation 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 structural material.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 liquide water and atmospheric carbon dioxide.Then this cryogenic liquide water also is passed in said certain heat exchanger, be used for said expansion step-down after mixed gas come together cooling water is cooled off.To be sent in the condenser through the cooling water of cooling then carrying out heat exchange, and exhaust steam will be cooled to condensed water with exhaust steam.Generating efficiency is through being calculated as 36.01% in this case.This condensed water turns back to after pump pressurization in second heat exchanger and carries out heat exchange from mixture after the reaction of the high temperature of gasification oven then, to produce high temperature and high pressure steam again.
[embodiment 11]
According to the common step-down gas that need not expand, and with normal-temperature water like 32 ℃ of water cooling exhaust steam, 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 400 ℃; Pressure is 15MPa, and the temperature that goes out the exhaust steam 5 of steam turbine is 46 ℃, and pressure is 0.01Mpa; In this case, generating efficiency is about 33.42% through calculating.
Among the above embodiment, generating efficiency=(T
1C
V1-T
2C
V2)/Q
Raw material* 100%,
Wherein:
Q
Raw materialBe the calorific value of raw material, the coal among the promptly above embodiment, mud or stalk etc.;
T
1Be the initial state temperature of power generation medium, promptly power generation medium gets into steam turbine temperature before;
T
2Be the final state temperature of power generation medium, i.e. exhaust steam temperature;
C
V1Be power generation medium initial state thermal capacitance, promptly power generation medium gets into steam turbine thermal capacitance before;
C
V2Be power generation medium final state thermal capacitance, i.e. exhaust steam thermal capacitance;
Those skilled in the art utilizes the known technology collection and measures these parameters, according to above-mentioned formula, can calculate corresponding generating efficiency.
Obviously as a kind of optimal way, the inventive method also comprises utilizes the step that is absorbed the gas generation energy products after the expansion step-down behind the cold, for example produces methane or hydrogen or carbon monoxide.This is applicable to above-mentioned all embodiments of the present invention.
Although above all embodiments are generating working medium with water, it is any situation in water, carbon dioxide, the isoparaffin that the present invention is suitable for generating working medium equally; In addition; Can replace or other carbon-contained organic matter of increase on the basis of coal the feed coal that adds among the embodiment in the reactor; For example except the situation shown in the foregoing description; Raw material can comprise carbon-contained organic matters such as living beings, mud, high-concentration waste water, and raw material also can comprise the mixture of coal and living beings, and all these materials get into the high-temperature high-voltage reaction device with the form of slurry; High-temperature high-voltage reaction comprises ultra/subcritical gasification reaction, ultra/subcritical oxidation reaction and ultra/reaction types such as subcritical partial oxidation gasification reaction; Wherein, the general operational requirement(GOR) of ultra/subcritical oxidation reaction is: the temperature range of reaction is 350-750 ℃, and the pressure range of reaction is 15-40MPa.Preferably the pressure range through the gas (can be mixed gas) of overexpansion step-down is 0.1-7Mpa among the present invention.
The present invention also provides a kind of the gasification to produce the device of energy products and heat generating on the other hand.Shown in Fig. 1-4, although be flow chart shown in these accompanying drawings, combine this flow chart to help understanding device embodiment of the present invention, therefore when describing apparatus of the present invention, describe with reference to Fig. 1-4.
Particularly, apparatus of the present invention comprise: the expansion dropping equipment has the expansion step-down inlet that receives the step-down gas of waiting to expand, and discharges the expansion step-down outlet through the gas of overexpansion step-down; And condenser, have first heat exchanger channels that supplies to be loaded with the cooling medium from the cold of said gas through the overexpansion step-down and get into, and the exhaust steam that supplies generating to produce get into wherein second heat exchanger channels with said cooling medium heat exchange.Wherein, said gas through the overexpansion step-down gets into first heat exchanger channels as cooling medium, and the exhaust steam adverse current in the cooling medium in first heat exchanger channels and second heat exchanger channels is also carried out heat exchange through the wall of heat exchanger channels separately.Perhaps, apparatus of the present invention also comprise first heat exchanger, and said gas through the overexpansion step-down gets into a heat exchanger channels in first heat exchanger, and carry out heat exchange with cooling water in another heat exchanger channels of first heat exchanger; Through the wall of these two passages, cooling water with carry out heat exchange through the gas of overexpansion step-down, this cooling water after the heat exchange is discharged to first heat exchanger channels of above-mentioned condenser as cooling medium from described another heat exchanger channels.。
In one embodiment; Condenser comprises first portion and second portion; First portion and second portion have two heat exchanger channels that carry out heat exchange each other separately; Wherein two heat exchanger channels in the first portion are aforesaid first and second heat exchanger channels, and promptly first heat exchanger channels supplies to get into through the gas of overexpansion step-down, and the exhaust steam that second heat exchanger channels supplies generating to produce gets into.In two heat exchanger channels of second portion; A heat exchanger channels supplies exhaust steam entering, the but water entering of exhaust steam of another cooling after first portion's heat release; Exhaust steam and the water wall in passage separately and through passage carries out heat exchange each other, thereby exhaust steam is further cooled off.It may be noted that; The described cooling medium that is loaded with expansion step-down gas cold is meant two kinds of situation: the one, through the gas of overexpansion step-down itself, another by described through the liquid after the gas cooling of overexpansion step-down (the for example water after gas heat release after the expansion step-down).
Further again, apparatus of the present invention also comprise: use for raw material to surpass therein/reactor of subcritical gasification or oxidation reaction, this reactor has relief opening, discharges for the reaction mixture that reaction generates; Supply reaction mixture and generating working medium second heat exchanger of heat exchange each other therein; This second heat exchanger has heat transferring medium inlet and generating working medium outlet; The heat transferring medium inlet is communicated with the relief opening of reactor to receive the reaction mixture of autoreactor, and the generating working medium after the reaction mixture heat absorption is discharged through the generating working medium outlet; Utilize the turbine engine of the generating working medium generating after absorbing heat; This turbine engine have is communicated with generating working medium outlet (in generating working medium is under the situation of water in order to receive generating working medium after absorbing heat; Generating working medium becomes steam after in heat exchanger, absorbing heat) import; This turbine engine also has the exhaust steam outlet of the exhaust steam discharge that supplies the generating generation, and second heat exchanger channels of condenser is communicated with the exhaust steam outlet, carries out condensation therein to receive exhaust steam.
The present invention's device of producing energy products and heat generating that gasifies also comprises: the segregating unit that gas separation in the reaction mixture is come out.This segregating unit is connected between aforesaid second heat exchanger (that is, aforesaid confession reaction mixture and generating working medium therein the heat exchanger of heat exchange) each other and the expansion dropping equipment.This segregating unit is sent after gas separation is come out in the reaction mixture into the expansion dropping equipment, simultaneously this segregating unit discharge water and slag.The above-mentioned functions of this segregating unit also can be called purification function, in order to purify reaction mixture.
The present invention gasify the device of producing energy products and heat generating also comprise gas turbine and utilize the expansion step-down that is absorbed behind the cold after the device of gas generation energy products; Condenser directly since the self-expanding dropping equipment generate under the situation of gas as cooling medium of overexpansion step-down; Through the gas of overexpansion step-down in condenser with the exhaust steam heat-shift after be admitted to gas turbine fuel gas inlet for generating, or be admitted in the device of producing energy products to produce the energy products of methane for example or hydrogen or carbon monoxide or their combination in any etc.Is under the situation of medium at condenser with the cooling water of discharging from aforementioned second heat exchanger; Be admitted to after coming the gas through the overexpansion step-down of self-expanding dropping equipment in this second heat exchanger, to absorb heat in the fuel gas inlet of gas turbine for gas turbine power generation, or be admitted in the device of producing energy products to produce the energy products of methane for example or hydrogen or carbon monoxide or their combination in any etc.
The generating working medium (for example saturation water) that is cooled and produces at condenser for the recycle exhaust steam; Apparatus of the present invention also comprise compression pump, and generating working medium (for example saturation water) the pressurization back that will produce in order to being cooled is sent in aforesaid second heat exchanger as generating working medium.Compression pump has pump intake and pump discharge, and this second heat exchanger has the inlet that supplies generating working medium to flow into, and this inlet is communicated with pump discharge, and condenser has the outlet of generating working medium (for example saturation water) discharge that produces being cooled, and this outlet is communicated with pump intake.
To sum up; Method and apparatus of the present invention utilizes gas expansion step-down can produce the cooling medium lower than ambient temperature (for example room temperature) (for example-25～20 ℃ the gas through the overexpansion step-down); Replace traditional room temperature cooling water and be used for exhaust steam cooling, condensation, the temperature of exhaust steam can be set to below the ambient temperature, both can improve the generating efficiency of turbine power generation equipment; Being fit to of can making full use of again that gasification equal energy source production technology produced waits to expand the pressure of gas of step-down acting can; This energy also can be used for generating, thereby improves the energy utilization efficiency of whole process system, produces more clean electric power equal energy source product.
The above is merely the preferred embodiments of the present invention, is not limited to the present invention, and for a person skilled in the art, the present invention can have various changes and variation.All within spirit of the present invention and principle, any modification of being done, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (23)
1. electricity-generating method, the step that condensation is carried out in the exhaust steam that produces when comprising generating,
It is characterized in that, in this step, make said exhaust steam carry out heat exchange with gas directly or indirectly through the overexpansion step-down.
2. the method for claim 1 is characterized in that,
Said heat exchange is carried out in condenser, said condenser with by described water after the gas cooling of overexpansion step-down as cooling medium, said exhaust steam is directly carried out heat exchange with said cooling medium in said condenser.
3. the method for claim 1 is characterized in that,
Said heat exchange is carried out in condenser, said condenser directly with described gas through the overexpansion step-down as cooling medium, said exhaust steam is directly carried out heat exchange with said cooling medium in said condenser.
4. the method for claim 1 is characterized in that,
Said heat exchange is carried out in condenser; Said condenser comprises first portion and second portion; The cooling medium of said first portion is a water; The cooling medium of said second portion is described gas through the overexpansion step-down, and the cooling medium in said exhaust steam and said first and second parts directly carries out heat exchange.
5. like each described method among the claim 1-4, it is characterized in that, also comprise:
Raw material sent in the reactor surpass/subcritical gasification reaction or oxidation reaction formation reaction mixture;
Wherein, described gas through the overexpansion step-down is the gas of from reaction mixture, separating to be expanded obtain after the step-down.
6. method as claimed in claim 5 is characterized in that, also comprises:
Said reaction mixture imported in second heat exchanger carry out heat exchange with generating working medium;
Generate electricity in the generating working medium importing turbine engine with the said reaction mixture of absorption institute heat content; And
Utilize described gas generation energy products through the overexpansion step-down, said energy products are methane or hydrogen or carbon monoxide or electricity or their combination in any.
7. the method for claim 1 is characterized in that, the temperature of described gas through the overexpansion step-down is lower than ambient temperature, and said ambient temperature is meant 28-32 ℃.
8. method as claimed in claim 5 is characterized in that, said raw material is coal, living beings, mud or waste water, contains gasifying agent or oxygenant in the said reactor, and said gasifying agent or oxygenant are oxygen, steam, oxygen-enriched air, airborne at least a.
9. method as claimed in claim 6 is characterized in that, said generating working medium is water or carbon dioxide or isoparaffin.
10. method as claimed in claim 5 is characterized in that, the temperature conditions when said raw material takes place in said reactor ultra/subcritical gasification reaction or oxidation reaction is that 350-750 ℃, pressure condition are 15-40Mpa.
11. the method for claim 1 is characterized in that, described gas through the overexpansion step-down has the pressure of 0.1-7MPa.
12. method as claimed in claim 5 is characterized in that, the gas that said reaction mixture comprises is that raw material surpasses/gas that subcritical gasification reaction produces or the gas of raw material oxidation reaction generation.
13. one kind is used to gasify and produces the device of energy products and heat generating, it is characterized in that said device comprises:
The expansion dropping equipment has the expansion step-down inlet that receives the step-down gas of waiting to expand, and discharges the expansion step-down outlet through the gas of overexpansion step-down; And
Condenser, have first heat exchanger channels that the cooling medium of the cold that supplies to be loaded with said gas through the overexpansion step-down gets into, and the exhaust steam that supplies generating to produce get into wherein with said first heat exchanger channels in second heat exchanger channels of cooling medium heat exchange.
14. device as claimed in claim 13 is characterized in that, said expansion step-down outlet is communicated with said first heat exchanger channels, and wherein the gas through the overexpansion step-down gets into said first heat exchanger channels as said cooling medium.
15. device as claimed in claim 13; It is characterized in that, also comprise first heat exchanger, said gas through the overexpansion step-down gets into a heat exchanger channels in said first heat exchanger; And carry out heat exchange with cooling water in another heat exchanger channels of said first heat exchanger
Wherein, with said cooling water behind the gas converting heat of overexpansion step-down, be discharged to first heat exchanger channels of said condenser as cooling medium from described another heat exchanger channels.
16. device as claimed in claim 13; It is characterized in that; Said condenser comprises first portion and second portion; Said first and second heat exchanger channels are located in the said first portion, and said second portion has exhaust steam entering one of them heat exchanger channels and the confession of confession after the heat release of said first portion and gets into another heat exchanger channels wherein in order to the water that cools off exhaust steam in this heat exchanger channels.
17. like each described device among the claim 13-16, it is characterized in that, also comprise:
Use the reactor that reacts therein for raw material, have the relief opening of the reaction mixture discharge that supplies the reaction generation;
Supply reaction mixture and generating working medium second heat exchanger of heat exchange each other, have is communicated with said relief opening in order to the heat transferring medium inlet that receives reaction mixture and will export from the generating working medium of the generating working medium discharge after the reaction mixture heat absorption; And
Utilize the turbine engine of the generating working medium generating after absorbing heat; Have is communicated with generating working medium outlet in order to the import that receives the generating working medium after the heat absorption, and the exhaust steam that supplies generating the to produce exhaust steam outlet of discharging, said exhaust steam outlet enters the mouth with the exhaust steam of said condenser and is communicated with.
18. device as claimed in claim 17 is characterized in that, also comprises the segregating unit that gas separation in the reaction mixture is come out, and is connected between said second heat exchanger and the said expansion dropping equipment.
19. device as claimed in claim 14; It is characterized in that also comprise gas turbine, said gas turbine has fuel gas inlet; Said condenser has the outlet that the expansion step-down gas behind confession and the said exhaust steam heat-shift is discharged, and this outlet is communicated with said fuel gas inlet.
20. device as claimed in claim 15; It is characterized in that; Also comprise gas turbine; Said gas turbine has fuel gas inlet, and said first heat exchanger has the outlet that the expansion step-down gas after the cooling water heat exchange in another heat exchanger channels is discharged described in confession and this first heat exchanger, and this outlet is communicated with said fuel gas inlet.
21. device as claimed in claim 17 is characterized in that, also comprises compression pump, has pump intake and pump discharge,
Wherein, said second heat exchanger has the inlet that supplies generating working medium to flow into, and this inlet is communicated with the pump discharge of said compression pump,
Wherein, said condenser has the outlet that the saturation water that generates after the exhaust steam condensation is discharged, and this outlet is communicated with the pump intake of said compression pump.
22. device as claimed in claim 14 is characterized in that, also comprises:
Utilization is absorbed the device of gas generation energy products after the expansion step-down behind the cold, has the inlet that gas gets into after the said expansion step-down that supplies to be absorbed behind the cold,
Wherein, said condenser has the outlet that the expansion step-down gas behind confession and the said exhaust steam heat-shift is discharged, and this outlet is communicated with the said inlet of the device of said production energy products.
23. device as claimed in claim 15 is characterized in that, also comprises:
Utilization is absorbed the device of gas generation energy products after the expansion step-down behind the cold, has the inlet that gas gets into after the said expansion step-down that supplies to be absorbed behind the cold,
Wherein, said first heat exchanger has the outlet that the expansion step-down gas after the cooling water heat exchange in said another heat exchanger channels in confession and this first heat exchanger is discharged, and this outlet is communicated with the said inlet of the device of said production energy products.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210002533.4A CN102518489B (en) | 2012-01-06 | 2012-01-06 | Electricity-generating method, the device generated electricity for gasified production of energy products and heat |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210002533.4A CN102518489B (en) | 2012-01-06 | 2012-01-06 | Electricity-generating method, the device generated electricity for gasified production of energy products and heat |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102518489A true CN102518489A (en) | 2012-06-27 |
| CN102518489B CN102518489B (en) | 2016-08-03 |
Family
ID=46289526
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210002533.4A Active CN102518489B (en) | 2012-01-06 | 2012-01-06 | Electricity-generating method, the device generated electricity for gasified production of energy products and heat |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102518489B (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105112102A (en) * | 2015-09-07 | 2015-12-02 | 新奥科技发展有限公司 | Carbonaceous matter gasification treatment method and device |
| CN105604618A (en) * | 2015-12-25 | 2016-05-25 | 华北电力大学 | Supercritical water pulverized coal direct oxidation composite working medium circulating power generating system and method |
| CN106315586A (en) * | 2015-06-15 | 2017-01-11 | 内蒙古盾安光伏科技有限公司 | Polycrystalline silicon production system |
| CN109252842A (en) * | 2018-10-29 | 2019-01-22 | 邓晓亮 | Overcritical underground coal gasification(UCG) output mixed gas trilogy supply electricity generation system |
| CN110259534A (en) * | 2019-05-28 | 2019-09-20 | 江苏大学 | A kind of gasification of biomass organic rankine cycle system |
| CN111287812A (en) * | 2020-02-23 | 2020-06-16 | 刘希浩 | Production process for improving thermal efficiency of whole thermal power plant |
| CN111412022A (en) * | 2020-03-24 | 2020-07-14 | 西安交通大学 | Coal supercritical water gasification power generation system for controlling available energy loss and working method |
| WO2020211472A1 (en) * | 2019-04-15 | 2020-10-22 | 李华玉 | Single working medium steam combined cycle |
| WO2020211473A1 (en) * | 2019-04-17 | 2020-10-22 | 李华玉 | Combined steam cycle using single working medium |
| WO2020248592A1 (en) * | 2019-06-13 | 2020-12-17 | 李华玉 | Reverse single working medium steam combined cycle |
| CN112594695A (en) * | 2020-11-17 | 2021-04-02 | 光大环境科技（中国）有限公司 | Supercritical water gasification device for industrial garbage |
| CN114717026A (en) * | 2022-04-27 | 2022-07-08 | 西安交通大学 | Hydrogen supercritical hydrothermal combustion reaction device and application method thereof |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5880384A (en) * | 1981-10-26 | 1983-05-14 | ゲブリユ−ダ−・ズルツア−・アクチエンゲゼルシヤフト | Gas cooler for coal gasification 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 |
| JPH08246813A (en) * | 1995-03-10 | 1996-09-24 | Hitachi Ltd | Operation method and device for coal gasification compound generation plant |
| WO2010134037A1 (en) * | 2009-05-22 | 2010-11-25 | Sasol Technology (Proprietary) Limited | Process for co-producing synthesis gas and power |
| CN102015072A (en) * | 2006-12-15 | 2011-04-13 | 普莱克斯技术有限公司 | Electrical power generation method |
| CN102373090A (en) * | 2010-08-20 | 2012-03-14 | 新奥科技发展有限公司 | Coal gasification technology and steam turbine power generation technology coupled method |
| CN102373091A (en) * | 2010-08-20 | 2012-03-14 | 新奥科技发展有限公司 | Method for coupling coal gasification process and steam turbine power generation process |
| CN102559269A (en) * | 2010-08-20 | 2012-07-11 | 新奥科技发展有限公司 | Method for combining coal gasification process and vapor turbine power generation process |
-
2012
- 2012-01-06 CN CN201210002533.4A patent/CN102518489B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5880384A (en) * | 1981-10-26 | 1983-05-14 | ゲブリユ−ダ−・ズルツア−・アクチエンゲゼルシヤフト | Gas cooler for coal gasification 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 |
| JPH08246813A (en) * | 1995-03-10 | 1996-09-24 | Hitachi Ltd | Operation method and device for coal gasification compound generation plant |
| CN102015072A (en) * | 2006-12-15 | 2011-04-13 | 普莱克斯技术有限公司 | Electrical power generation method |
| WO2010134037A1 (en) * | 2009-05-22 | 2010-11-25 | Sasol Technology (Proprietary) Limited | Process for co-producing synthesis gas and power |
| CN102373090A (en) * | 2010-08-20 | 2012-03-14 | 新奥科技发展有限公司 | Coal gasification technology and steam turbine power generation technology coupled method |
| CN102373091A (en) * | 2010-08-20 | 2012-03-14 | 新奥科技发展有限公司 | Method for coupling coal gasification process and steam turbine power generation process |
| CN102559269A (en) * | 2010-08-20 | 2012-07-11 | 新奥科技发展有限公司 | Method for combining coal gasification process and vapor turbine power generation process |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106315586A (en) * | 2015-06-15 | 2017-01-11 | 内蒙古盾安光伏科技有限公司 | Polycrystalline silicon production system |
| CN106315586B (en) * | 2015-06-15 | 2018-09-18 | 内蒙古盾安光伏科技有限公司 | polycrystalline silicon production system |
| CN105112102A (en) * | 2015-09-07 | 2015-12-02 | 新奥科技发展有限公司 | Carbonaceous matter gasification treatment method and device |
| CN105604618A (en) * | 2015-12-25 | 2016-05-25 | 华北电力大学 | Supercritical water pulverized coal direct oxidation composite working medium circulating power generating system and method |
| CN105604618B (en) * | 2015-12-25 | 2018-05-25 | 华北电力大学 | Supercritical water coal dust direct oxidation composite work medium cycle generating system and method |
| CN109252842A (en) * | 2018-10-29 | 2019-01-22 | 邓晓亮 | Overcritical underground coal gasification(UCG) output mixed gas trilogy supply electricity generation system |
| CN109252842B (en) * | 2018-10-29 | 2024-04-12 | 邓晓亮 | Mixed gas triple power generation system produced by underground supercritical coal gasification |
| WO2020211472A1 (en) * | 2019-04-15 | 2020-10-22 | 李华玉 | Single working medium steam combined cycle |
| WO2020211473A1 (en) * | 2019-04-17 | 2020-10-22 | 李华玉 | Combined steam cycle using single working medium |
| CN110259534A (en) * | 2019-05-28 | 2019-09-20 | 江苏大学 | A kind of gasification of biomass organic rankine cycle system |
| GB2600047B (en) * | 2019-06-13 | 2023-03-29 | Li Huayu | Reverse single-working-medium vapor combined cycle |
| WO2020248592A1 (en) * | 2019-06-13 | 2020-12-17 | 李华玉 | Reverse single working medium steam combined cycle |
| GB2600047A (en) * | 2019-06-13 | 2022-04-20 | Li Huayu | Reverse single working medium steam combined cycle |
| CN111287812A (en) * | 2020-02-23 | 2020-06-16 | 刘希浩 | Production process for improving thermal efficiency of whole thermal power plant |
| CN111412022A (en) * | 2020-03-24 | 2020-07-14 | 西安交通大学 | Coal supercritical water gasification power generation system for controlling available energy loss and working method |
| CN112594695A (en) * | 2020-11-17 | 2021-04-02 | 光大环境科技（中国）有限公司 | Supercritical water gasification device for industrial garbage |
| CN114717026B (en) * | 2022-04-27 | 2023-02-07 | 西安交通大学 | Hydrogen supercritical hydrothermal combustion reaction device and application method thereof |
| CN114717026A (en) * | 2022-04-27 | 2022-07-08 | 西安交通大学 | Hydrogen supercritical hydrothermal combustion reaction device and application method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102518489B (en) | 2016-08-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102518489B (en) | Electricity-generating method, the device generated electricity for gasified production of energy products and heat | |
| CN108979770B (en) | Integrated coal gasification combined cycle power generation system and method using supercritical carbon dioxide as working medium | |
| KR101739494B1 (en) | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation | |
| RU2534077C2 (en) | Method of combined production of synthesis-gas and electric energy | |
| KR101767287B1 (en) | System for heat integration with methanation system | |
| CN108439336B (en) | Zero-emission hydrogen electric cogeneration system | |
| CN102373097B (en) | Coupling method of coal gasification process, residual carbon oxidation process and steam turbine power generation process | |
| CN106414330B (en) | The technique for producing ammonia and its derivative, especially urea | |
| JP5695377B2 (en) | Carbon capture cooling system and method | |
| CN113090349B (en) | Photo-thermal type coal supercritical water gasification hydrogen-heat-power cogeneration system and working method | |
| US20120039430A1 (en) | Nuclear powered facility that generates consumable fuels | |
| CN102850172A (en) | Coal chemical poly-generation process and system | |
| CN109181776B (en) | Coal-based poly-generation system and method for integrated fuel cell power generation | |
| EP2251626A2 (en) | Efficiently compressing nitrogen in a combined cycle power plant | |
| CN102559269B (en) | Method for combining coal gasification process and vapor turbine power generation process | |
| CN216198494U (en) | Novel gas turbine reheating combined cycle power generation device | |
| CN102373090B (en) | Coal gasification technology and steam turbine power generation technology coupled method | |
| CN113292394B (en) | Coke oven gas coupling waste incineration power generation system methyl alcohol device | |
| CN102373091B (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 | |
| CN102373099B (en) | Method for coupling coal gasification process and steam turbine power generation process | |
| CN106761990B (en) | A kind of apparatus and method to be generated electricity using IGCC low grade residual heats | |
| CN102373092B (en) | Coupling method of coal gasification technology and steam turbine generating technology | |
| CN208982131U (en) | Using supercritical carbon dioxide as the integrated gasification combined cycle for power generation system of working medium | |
| 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 |