CN102518489B - Electricity-generating method, the device generated electricity for gasified production of energy products and heat - Google Patents
Electricity-generating method, the device generated electricity for gasified production of energy products and heat Download PDFInfo
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Abstract
The present invention provides a kind of electricity-generating method, the step condensed including the exhaust steam produced during to generating, in this step, makes exhaust steam carry out heat exchange with the gas through expansion blood pressure lowering directly or indirectly.The present invention also provides for a kind of device for gasified production of energy products with hot generating, and this device includes: expand dropping equipment, has and receives the expansion depressurization outlet of gas after the expansion blood pressure lowering entrance and discharge expanding blood pressure lowering gas expands blood pressure lowering；And condenser, have for be loaded with the first heat exchanger channels that the cooling medium of the cold of gas enters after self-expanding blood pressure lowering and the exhaust steam produced for generating enter wherein with the second heat exchanger channels of cooling medium heat exchange.Methods and apparatus of the present invention utilizes gas after expanding blood pressure lowering to produce cold, the temperature of exhaust steam is reduced to below ambient temperature, has both taken full advantage of the pressure energy of gas, improved again the generating efficiency of turbine power generation equipment.
Description
Technical field
The present invention relates to a kind of electricity-generating method and for gasified production of energy products and the device of heat generating.
Background technology
IGCC (integrated gasification combined cycle plants) technology achieves and coal gasification is combined with gas and steam turbine combined generating system, is a kind of Clean Coal Power Generating Technologies.The oxygen that coal after process comes with air separation unit generates mixed gas in gasification furnace, the sensible heat recovered generation steam of mixed gas, mixed gas is after clean unit purifies, burning driving gas turbine power generation, the heat energy of the flue gas that gas turbine is discharged is reclaimed by waste heat boiler, heating produces steam, and steam drive steam turbine generates electricity.In IGCC technique, this product stream stock of mixed gas is utilized to first pass through gas turbine Brayton circulating generation, water is heated into steam by the fume afterheat of heat exchange and/or discharge of gas turbine, steam and then drive steam turbine turbine power generation by Rankine circulation.Relatively independent, the coupling of the shortage degree of depth or synergism between coal gasifying process and Brayton circulation and Rankine circulation technology, the generating efficiency of i.e. Rankine circulation is only affected by the temperature of produced steam, and coal gasifying process does not directly affect the generating efficiency of Rankine circulation.In other words, above coal gasification and the united technique of steam turbine generation only be make use of by the steam thermal energy produced in coal gasification course, the most only made coal gasifying process and steam turbine generation method contact by the steam of the generation in coal gasification course.If the product of coal gasification is not exclusively for burned for energy, but production energy products, such as methane, hydrogen and carbon monoxide etc., then the degree of coupling between coal gasification and the step Optimum utilization of gas and steam turbine combined generating system energy and cell process is required to improve further.
Additionally, steam turbine generating generally uses thermodynamic process based on Rankine circulation.One preferable Rankine circulation, its thermal efficiency (generating efficiency) depends on the temperature and pressure of endothermic process and exothermic process.For the exothermic process carried out in steam turbines, the temperature reducing 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.Such as, in usual steam turbine power generation process, the cooling medium of steam cooling segment is often with cooling water.Owing to cooling down the restriction of aqueous medium, the steam i.e. temperature of exhaust steam going out turbine is normally controlled in more than ambient temperature.Such as, the usual operating mode of cooling water is gauge pressure 0.52MPa, temperature 32 DEG C, thus limit exhaust steam be normally controlled in more than 32 DEG C.(about being discussed in detail of Rankine circulation, refer to " Modern Coal converts and Coal Chemical Industry New Technologies practicality pandect ", chapter 9, the 6th, steam integrated coal gasification combined cycle, Liao Hanxiang edits, 2004, and " integrated gasification combined cycle thermoelectric oil multi-production process technical characterstic and application ", Chen Chongliang, Yuan Longjun, coal engineering, 11 phases in 2008).
Preferably Rankine circulation can also describe with tephigram (T-S figure) as shown in Figure 7.The theoretical merit that steam is externally done is equivalent to the area that in Fig. 7, curve 1 → 2 → 3 → 4 → 5 → 6 → 1 is surrounded.Wherein the heat absorption (1 → 2 → 3 → 4) in circulation and exothermic process (5 → 6) are isobaric process, and expansion (4 → 5) and the condensed water boost process (6 → 1) of steam are isentropic procedure.
Additionally, in the material direct generations of electricity such as the material of high water content such as brown coal, mud coal, mud and rubbish or gasification, containing substantial amounts of steam in flue gas or product gas, owing to the latent heat of water evaporation is the biggest, substantial amounts of heat is caused to be walked by flue gas or the product band of gas, hence it is evident that to reduce generating and gasification efficiency.
Having supercritical technology to couple with generation technology in existing supercritical technology, major way is that the heat energy utilizing product carries out turbine power generation by changing thermogenetic steam, but can utilize the pressure of product gas.
The generation technology combined with coal chemical technology, is only made coal gasifying process and steam turbine generation method contact by the steam of the generation in coal gasification course.
Existing steam turbine generation technology exhaust steam temperature controls, more than ambient temperature, to limit generating efficiency.
It addition, the material direct generation of electricity of high water content, substantial amounts of heat is taken away by water vapour and flue gas, hence it is evident that reduce generating efficiency.
The high pressure energy of the product that supercritical water oxidation/gasification technology produces is not applied by prior art.The energy of system fails to be fully used.
Summary of the invention
For problem present in correlation technique, it is an object of the invention to provide a kind of electricity-generating method and for gasified production of energy products and the device of heat generating, with the cold utilizing the gas through expanding blood pressure lowering to produce, the temperature of exhaust steam is reduced to below ambient temperature, both the pressure energy of gas had been taken full advantage of, the generating efficiency of turbine power generation equipment is improved, it is achieved thereby that produce the lifting of the overall efficiency of energy utilization of the device of energy products and heat generating further through reducing the temperature of exhaust steam in Rankine circulation.
On the one hand, the present invention provides a kind of electricity-generating method, the step condensed including the exhaust steam produced during to generating, in this step, makes described exhaust steam carry out heat exchange with the gas through expansion blood pressure lowering directly or indirectly.
Preferably, described heat exchange is carried out within the condenser, described condenser using by described water after the gas cooling expanding blood pressure lowering as cooling medium, described exhaust steam directly carries out heat exchange in described condenser with described cooling medium.
Preferably, heat exchange is carried out within the condenser, and described condenser is directly using the described gas through expanding blood pressure lowering as cooling medium, and described exhaust steam directly carries out heat exchange in described condenser with described cooling medium.
Preferably, heat exchange is carried out within the condenser, described condenser includes Part I and Part II, the cooling medium of described Part I is water, the cooling medium of described Part II is the described gas through expanding blood pressure lowering, and described exhaust steam directly carries out heat exchange with the cooling medium in described first and second parts.
Preferably, the method also includes: is sent into by raw material and carries out surpassing/subcritical gasification reaction or oxidation reaction reaction of formation mixture in reactor；Wherein, the described gas through expanding blood pressure lowering, be carry out the gas separated from reactant mixture expanding blood pressure lowering after obtain.
Preferably, the method also includes: is imported by described reactant mixture in the second heat exchanger and carries out heat exchange with generating working medium；The generating working medium absorbing described reactant mixture institute heat content is imported in turbine and generates electricity；And the gas generation energy products through expanding blood pressure lowering described in utilizing, described energy products are methane or hydrogen or carbon monoxide or electricity or they combination in any.
Preferably, the method is less than ambient temperature through the temperature expanding the gas of blood pressure lowering, and this ambient temperature refers to 28-32 DEG C.
Preferably, the method raw material is coal, biomass, mud or waste water, and containing gasifying agent or oxidant in described reactor, described gasifying agent or oxidant are at least one in oxygen, steam, oxygen-enriched air, air.
Preferably, generating working medium is water or carbon dioxide or isoparaffin.
Preferably, raw material occurs temperature conditions when super/subcritical gasification reaction or oxidation reaction to be 350-750 DEG C in described reactor, pressure condition is 15-40MPa.
Preferably, there is the pressure of 0.1-7MPa through expanding the gas of blood pressure lowering.
Preferably, there is the temperature of-25～20 DEG C through expanding the gas of blood pressure lowering.
Preferably, the gas that reactant mixture comprises be raw material super/gas that produces of the gas that produces of subcritical gasification reaction or raw material oxidation reaction.
On the other hand, the present invention also provides for a kind of for gasified production of energy products with the device of heat generating, including: expand dropping equipment, have and receive expanding blood pressure lowering entrance and discharging the expansion depressurization outlet of gas through expansion blood pressure lowering of blood pressure lowering gas to be expanded；And condenser, have for be loaded with from described through expansion blood pressure lowering gas cold cooling medium enter the first heat exchanger channels and for generating produce exhaust steam enter wherein with the second heat exchanger channels of cooling medium heat exchange in described first heat exchanger channels.
Preferably, through expanding gas described first heat exchanger channels of entrance of blood pressure lowering as described cooling medium.
Preferably, apparatus of the present invention also include First Heat Exchanger, a heat exchanger channels in First Heat Exchanger is entered through expanding the gas of blood pressure lowering, and carry out heat exchange with the cooling water in another heat exchanger channels of First Heat Exchanger, wherein, cooling water with after the described gas converting heat through expanding blood pressure lowering, is discharged to the first heat exchanger channels of described condenser as cooling medium from another described heat exchanger channels.
Preferably, condenser includes Part I and Part II, described first and second heat exchanger channels are located in described Part I, and described Part II has confession exhaust steam after described Part I heat release and enters one of them heat exchanger channels and for water entrance another heat exchanger channels therein in order to cool down exhaust steam in this heat exchanger channels.
Preferably, apparatus of the present invention also include: with the reactor reacted wherein for raw material, have the air vent of the reactant mixture discharge generated for reaction；For the second heat exchanger of reactant mixture and generating working medium heat exchange each other, have connect with described air vent in order to the heat transferring medium entrance receiving reactant mixture and the generating working medium outlet will discharged from the generating working medium after reactant mixture absorbs heat；Utilize the turbine of the generating working medium generating after heat absorption, having the import in order to the generating working medium after receiving heat absorption with generating working medium outlet and the exhaust steam for the exhaust steam discharge of generating generation exports, described exhaust steam outlet connects with the exhaust steam entrance of described condenser.
Preferably, apparatus of the present invention also include the segregation apparatus separated by gas in reactant mixture, are connected between described second heat exchanger and described expansion dropping equipment.
Preferably, apparatus of the present invention also include that gas turbine, described gas turbine have fuel gas inlet, described condenser have for described exhaust steam heat-shift after expand blood pressure lowering gas discharge outlet, this outlet connects with described fuel gas inlet.
Preferably, apparatus of the present invention also include gas turbine, described gas turbine has fuel gas inlet, described First Heat Exchanger have for in another heat exchanger channels described in this First Heat Exchanger cooling water heat exchange after expand blood pressure lowering gas discharge outlet, this outlet connects with described fuel gas inlet.
Preferably, apparatus of the present invention also include force (forcing) pump, there is pump intake and pump discharge, wherein, described second heat exchanger has the entrance flowed into for generating working medium, and this entrance connects with the pump discharge of described force (forcing) pump, wherein, described condenser has the outlet discharged by the saturation water generated after exhaust steam condensation, and this outlet connects with the pump intake of described force (forcing) pump.
Preferably, apparatus of the present invention also include: the device of gas generation energy products after the expansion blood pressure lowering after utilizing by absorption cold, there is the entrance for being entered by gas after the described expansion blood pressure lowering after absorption cold, wherein, described condenser have for described exhaust steam heat-shift after expand blood pressure lowering gas discharge outlet, this outlet connects with the described entrance of the device of described production energy products.
Preferably, apparatus of the present invention also include: the device of gas generation energy products after the expansion blood pressure lowering after utilizing by absorption cold, there is the entrance for being entered by gas after the described expansion blood pressure lowering after absorption cold, wherein, described First Heat Exchanger have for this First Heat Exchanger in described in expand the outlet that blood pressure lowering gas is discharged after cooling water heat exchange in another heat exchanger channels, this outlet connects with the described entrance of the device of described production energy products.
In the present invention, the heat exchanger used can be any suitably for the heat exchanger of indirect heat exchange, such as tubular heat exchanger, finned heat exchanger etc., and the type of these heat exchangers and specific configuration are to well known to a person skilled in the art, condenser essence is also heat exchanger, repeats no more here.The expansion gear used includes pressure drop capillary tube, dropping valve, decompressor etc., more than makes the method and apparatus of gas expansion blood pressure lowering all well known to a person skilled in the art, does not repeats them here.
Methods and apparatus of the present invention has the advantages that and makes the exhaust steam discharged from turbine carry out heat exchange with the gas through expansion blood pressure lowering directly or indirectly, utilize and the lower cooling medium of relatively ambient temperature (28-32 DEG C) (gases through expanding blood pressure lowering of such as-25～20 DEG C) after expanding blood pressure lowering, can be produced, exhaust steam being lowered the temperature, condense, the pressure both having taken full advantage of generating working medium can generate electricity；Improve the generating efficiency of turbine power generation equipment, produce more clean electric power, also can make full use of the pressure energy of the gas being suitable for blood pressure lowering to be expanded acting produced by coal gasification equal energy source production technology, this energy can also be used for generating, thus improves the energy utilization efficiency of whole process system.
nullIn more detail，Due to the fact that and carry out expanding blood pressure lowering to the gas in the reactant mixture generated after super/subcritical gasification reaction or oxidation reaction，Expand the gas temperature after blood pressure lowering and can be reduced to below ambient temperature (such as 0 DEG C)，Then utilize the gas after expanding blood pressure lowering that exhaust steam is condensed，The lower cooling medium of relatively ambient temperature (gases through expanding blood pressure lowering of such as-25～20 DEG C) can be produced after expanding blood pressure lowering hence with gas，The cooling water (typically with 32 DEG C of water as cooling medium) of cooling steam when replacing the steam turbine turbine power generation of common Rankine circulation driving，Just the exhaust steam (such as 5～10 DEG C) of lower temperature can be lowered the temperature、Condensation，Lower (the most common ambient temperature that the temperature of exhaust steam just can be arranged，Such as room temperature 18～27 DEG C)，Just can improve the generating efficiency of turbine power generation equipment.For prior art, the present invention uses the cooling medium (gas through expanding blood pressure lowering of such as-25～20 DEG C that the relatively ambient temperature through expanding blood pressure lowering generation is lower, it is preferably 0～20 DEG C) directly substitute or part substitutes the cooling water of common ambient temperature and lowers the temperature exhaust steam, condensation, or indirect utilization is through expanding the cold of the gas of blood pressure lowering (such as, by the cooling water of ambient temperature is cooled down, with this cooling water, exhaust steam is lowered the temperature again, condensation), just can the temperature of exhaust steam be arranged is lower, not only can improve the generating efficiency of turbine power generation equipment, and, the expansion pressure reduction acting that super/subcritical gasification reaction or oxidation reaction can also be utilized to produce raw gas generates electricity, further increase generated energy, improve whole process system energy utilization efficiency.
Cooling down exhaust steam further with the gas after above-mentioned expanded blood pressure lowering, in prior art merely with cooling water cooling exhaust steam, the present invention the most just can reduce the consumption consumption of cooling water, thus saves cooling water.
Furthermore, isolated gas the reactant mixture generated when super/subcritical gasification reaction or oxidation reaction, process owing to having carried out expansion blood pressure lowering, through the heat exchange with exhaust steam, temperature and pressure is gentleer, therefore it is easy to follow-up process, such as, is convenient for separating treatment to produce energy products or to enter follow-up gas turbine combustion generating.
Accompanying drawing explanation
Fig. 1 is the indicative flowchart of the embodiment 1,4,5,6 of electricity-generating method of the present invention；
Fig. 2 is the indicative flowchart of embodiment 2-3 of electricity-generating method of the present invention；
Fig. 3 is the indicative flowchart of the embodiment 7 of electricity-generating method of the present invention；
Fig. 4 is the indicative flowchart of the embodiment 8 of electricity-generating method of the present invention；
Fig. 5 is the indicative flowchart of the embodiment 9 of electricity-generating method of the present invention；
Fig. 6 is the indicative flowchart of the embodiment 10 of electricity-generating method of the present invention；
Fig. 7 is the tephigram (T-S figure) of Rankine circulation.
Detailed description of the invention
The present invention provides a kind of electricity-generating method, the step that it exhaust steam produced when including generating condenses: make exhaust steam carry out heat exchange with the gas through expansion blood pressure lowering directly or indirectly, in other words, in this step, exhaust steam absorbs the cold contained by the gas through expanding blood pressure lowering within the condenser to be lowered the temperature, to condense.Preferably, condenser using by described water after the gas cooling expanding blood pressure lowering as cooling medium；Or condenser is directly using the described gas through expanding blood pressure lowering as cooling medium；Or condenser includes Part I and Part II, the cooling medium of Part I is water, and the cooling medium of Part II is the described gas through expanding blood pressure lowering.
Further, the electricity-generating method of the present invention also includes that following generation to carry out expanding the step of blood pressure lowering gas: is sent into by raw material and carries out surpassing/subcritical gasification reaction or oxidation reaction reaction of formation mixture in reactor；Wherein, the described gas through expanding blood pressure lowering, be carry out the gas separated from reactant mixture expanding blood pressure lowering after obtain.In order to generate electricity, aforesaid reactant mixture be imported in the second heat exchanger and carry out heat exchange with generating working medium；Then the generating working medium absorbing reactant mixture institute heat content is imported in turbine and generate electricity.Gas after wherein expanding blood pressure lowering can be utilized to produce energy products after discharging its cold.
Hereinafter see accompanying drawing, the electricity-generating method of the present invention is described in detail.
[embodiment 1]
See Fig. 1, with generating working medium as water, as a example by the catalytic gasification that bituminous coal and supercritical water occur.Coal makes the granularity coal dust less than 150 microns through attrition grinding, with catalyst n a2CO3It is the water-coal-slurry of 40% that (consumption is the 10% of quality of pc) and water are prepared as coal dust butt concentration.Water-coal-slurry is pressurized, and preheating reaches 23MPa, and 550 DEG C enter in reactor (in this embodiment, reactor is gasification furnace), are passed through oxygen (in this embodiment, gasifying agent is oxygen) simultaneously in gasification furnace.In gasification furnace, part water-coal-slurry and the oxygen reaction of addition, be promoted to 650 DEG C by temperature.In the supercritical state, coal reacts under the effect of catalyst with water, generates the mixed gas rich in methane.Mixed gas be mainly composed of methane, carbon monoxide, carbon dioxide, hydrogen etc..The pyroreaction mixture reacted through supercritical gasification (that is, mixture after going out the reaction of gasification furnace) product from gasification furnace includes residue after mixed gas, supercritical water and reaction.This product and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump, produce temperature and be 400 DEG C and absolute pressure is the high temperature and high pressure steam of 15MPa, this high temperature and high pressure steam becomes exhaust steam after entering turbine (for steam turbines in this embodiment) expansion power generation, it is 0.00087MPa that this exhaust steam can be controlled in pressure, temperature is 5 DEG C, and exhaust steam enters condenser and is condensed into water.The mixed gas separated from reactant mixture after heat exchange enters clean unit, by mixed gas and water, slag separates, mixed gas after separation is through expanding blood pressure lowering, pressure is reduced to 5.68MPa, and temperature is down to 0 DEG C, is then used as the cooling medium of above-mentioned condenser, exhaust steam carries out heat exchange within the condenser to be condensed into aqueous water with cooling medium, and this mixed gas can enter later separation unit or enter follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 36.30% in this case.Come the water of condenser return to after pump pressurizes in the second heat exchanger with from gasification furnace after gasification reaction pyroreaction mixture carry out heat exchange, to regenerate high temperature and high pressure steam.
[embodiment 2]
Also referring to Fig. 2, with water as generating working medium, as a example by the supercritical water gasification of bituminous coal.It is 50% water-coal-slurry that bituminous coal makes concentration through controlling wet-type finishing machine grinding, then delivers in gasification furnace (in this embodiment, reactor is gasification furnace) through pump pressurization.Being passed through oxygen or air in gasification furnace is about 750 DEG C as gasifying agent, the operation temperature of gasification furnace simultaneously, and operation pressure is 27.0MPa.Coal at high temperature reacts with above-mentioned gasifying agent, generates rich in carbon monoxide, hydrogen, carbon dioxide, the coal gas of methane.After going out the reaction of gasification furnace, mixture includes coal gas and tar and unreacted gasifying agent completely etc..Make mixture and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump after this reaction, and make pressure (hydraulic) water become temperature to be 400 DEG C and absolute pressure is the high temperature and high pressure steam of 15MPa, this high temperature and high pressure steam becomes exhaust steam after entering steam turbines expansion power generation, it is 0.0025MPa that this exhaust steam can be controlled in pressure, temperature is 21.08 DEG C, and exhaust steam enters condenser and is condensed into aqueous water.After reaction after heat exchange, mixture enters segregation apparatus, by coal gas and water, slag separates, coal gas after separation pressure after expanding blood pressure lowering is reduced to 5.00MPa, temperature is down to-2.82 DEG C, then with it, cooling that temperature is 32 DEG C is water-cooled to 18 DEG C in First Heat Exchanger, and this coal gas can enter subsequent separation process or enter follow-up gas turbine combustion generating afterwards, the cooling water after coal gas cooling after expanded blood pressure lowering is then 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.The water carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 3]
See Fig. 2, with water as generating working medium, as a example by the catalytic gasification that brown coal and supercritical water occur.Coal is prepared as the granularity water-coal-slurry less than 150 microns through wet mill, and water coal slurry concentration is 35%, the K Han catalyst in water-coal-slurry2CO3(consumption is the 3% of quality of pc).Water-coal-slurry is pressurized, and preheating reaches 35MPa, and 450 DEG C enter gasification furnace (in this embodiment, reactor is gasification furnace), are passed through oxygen in gasification furnace simultaneously.In gasification furnace, part water-coal-slurry and the oxygen reaction of addition, be promoted to 570 DEG C by temperature.In the supercritical state, coal reacts under the effect of catalyst with water, generates the mixed gas rich in methane.Mixed gas be mainly composed of methane, carbon monoxide, carbon dioxide, hydrogen etc..Go out gasification furnace product and include residue after mixed gas, supercritical water and reaction.This product and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump, producing high temperature and high pressure steam, become exhaust steam after entering steam turbine expansion power generation, it is 0.0024MPa that this exhaust steam can be controlled in pressure, temperature is 20.34 DEG C, and exhaust steam enters condenser and is condensed into liquid water.Mixed gas after heat exchange enters clean unit, by mixed gas and water, slag separates, mixed gas after separation is reduced to 4.76MPa through expanding blood pressure lowering pressure, temperature is down to-4.73 DEG C, then in First Heat Exchanger, with it, cooling that temperature is 28 DEG C is water-cooled to 16 DEG C, this mixed gas can enter subsequent separation process or enter follow-up gas turbine combustion generating afterwards, the cooling water after mixed gas cooling after expanded blood pressure lowering is then 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.The water (saturation water being condensed into by exhaust steam) carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 4]
See Fig. 1, with water as generating working medium, as a example by the complete oxidation of high-concentration waste water.It is that 7% high-concentration waste water tentatively filters by concentration.Being delivered to gasification furnace after being pressurizeed by waste water, being passed through oxygen and steam in gasification furnace is about 450 DEG C as gasifying agent, the operation temperature of gasification furnace simultaneously, and operation pressure is 15MPa.Carbonaceous material in waste water at high temperature reacts with above-mentioned gasifying agent, generates carbon dioxide and water.After going out the reaction of gasification furnace, mixture includes gaseous product, solid residue and unreacted gasifying agent completely etc..Make mixture and the 23MPa water heat exchange in heat exchanger from force (forcing) pump after this reaction, and make pressure (hydraulic) water become high temperature and high pressure steam, this high temperature and high pressure steam becomes exhaust steam after entering steam turbines expansion power generation, it is 0.0032MPa that this exhaust steam can be controlled in pressure, temperature is 25.16 DEG C, and exhaust steam enters condenser and is condensed into aqueous water.After reaction after heat exchange, mixture enters segregation apparatus, by product and water, slag separates, gas after separation pressure after expanding blood pressure lowering is reduced to 6.11MPa, temperature is down to 2.5 DEG C, being then used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water, this coal gas can enter later separation processing procedure afterwards.Generating efficiency is through being calculated as 35.33% in this case.The water (saturation water being condensed into by exhaust steam) carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in heat exchanger after pump pressurizes.
[embodiment 5]
See Fig. 1, with water as generating working medium, as a example by the supercritical water oxidation of mud.After mud purification of raw materials, and it is configured to the slurry that concentration is 15% together with water.Being passed through oxygen and steam in gasification furnace is about 480 DEG C as gasifying agent, the operation temperature of gasification furnace simultaneously, and operation pressure is 24MPa.Carbonaceous material in mud at high temperature reacts with above-mentioned gasifying agent, generates carbon dioxide and water.After going out the reaction of gasification furnace, mixture includes gaseous product, solid residue and unreacted gasifying agent completely etc..Make mixture and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump after this reaction, and make pressure (hydraulic) water become high temperature and high pressure steam, this high temperature and high pressure steam becomes exhaust steam after entering steam turbines expansion power generation, it is 0.0023MPa that this exhaust steam can be controlled in pressure, temperature is 19.57 DEG C, and exhaust steam enters condenser and is condensed into water.After reaction after heat exchange, mixture enters segregation apparatus, by product gas and water, slag separates, gas after separation is reduced to 7.00MPa through expanding blood pressure lowering pressure, temperature is down to 5.79 DEG C, being then used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into aqueous water, this gas can enter later separation processing procedure afterwards.Generating efficiency is through being calculated as 35.76% in this case.The water (saturation water being condensed into by exhaust steam) carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 6]
Also referring to Fig. 1, with water as generating working medium, as a example by the supercritical water gasification of corn straw.Corn straw mixes with water after attrition grinding makes coal dust makes the biological chylema that concentration is 20%, then delivers in gasification furnace (in this embodiment, reactor is gasification furnace) through pump pressurization.Being passed through oxygen or air in gasification furnace is about 600 DEG C as gasifying agent, the operation temperature of gasification furnace simultaneously, and operation pressure is 40MPa.Corn straw at high temperature reacts with above-mentioned gasifying agent, generates rich in carbon monoxide, hydrogen, carbon dioxide, the admixture of gas of methane.After going out the reaction of gasification furnace, mixture includes gaseous product, tar and unreacted gasifying agent completely etc..Make mixture and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump after this reaction, and make pressure (hydraulic) water become high temperature and high pressure steam, this high temperature and high pressure steam becomes exhaust steam after entering steam turbines expansion power generation, it is 0.0015MPa that this exhaust steam can be controlled in pressure, temperature is 13.02 DEG C, and exhaust steam enters condenser and is condensed into aqueous water.After reaction after heat exchange, mixture enters segregation apparatus, by coal gas and water, slag separates, mixed gas after separation is reduced to 2.33MPa through expanding blood pressure lowering pressure, temperature is down to-24.42 DEG C, being then used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water, this mixed gas can enter subsequent separation process or enter follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 36.15% in this case.The water (saturation water being condensed into by exhaust steam) carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 7]
With reference to Fig. 3, with water as generating working medium, as a example by the catalytic gasification that bituminous coal and supercritical water occur.Coal makes the granularity coal dust less than 150 microns through attrition grinding, with catalyst n a2CO3It is the water-coal-slurry of 40% that (consumption is the 5% of quality of pc) and water are prepared as coal dust butt concentration.Water-coal-slurry is pressurized, and preheating reaches 30MPa, and 550 DEG C enter gasification furnace (in this embodiment, reactor is gasification furnace), are passed through oxygen in gasification furnace simultaneously.In gasification furnace, part water-coal-slurry and the oxygen reaction of addition, be promoted to 680 DEG C by temperature.In the supercritical state, coal reacts under the effect of catalyst with water, generates the mixed gas rich in methane.Mixed gas be mainly composed of methane, carbon monoxide, carbon dioxide, hydrogen etc..Go out gasification furnace product and include residue after mixed gas, supercritical water and reaction.Mixture and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump after this reaction, producing high temperature and high pressure steam, become exhaust steam after entering steam turbine expansion power generation, it is 34.16 DEG C that this exhaust steam can be controlled in temperature, absolute pressure is 0.0053Mpa, and exhaust steam enters condenser and is condensed into aqueous water.Mixed gas after heat exchange enters segregation apparatus, by mixed gas and water, slag separates, mixed gas after separation is reduced to 3.67MPa through expanding blood pressure lowering pressure, temperature is down to-11.57 DEG C, it is then used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into water, meanwhile, also in this condenser, it is passed through, with independent pipeline, the room temperature cooling water that temperature is 28 DEG C, jointly exhaust steam is cooled down, such as condenser is set to the first and second parts, wherein the cooling medium of Part I is cooling water and the cooling medium of Part II is the gas separated mixture after reaction after expanded blood pressure lowering, carry out condensing for the first time to exhaust steam first with Part I, then utilize Part II that exhaust steam carries out second time to condense.This mixed gas can enter subsequent separation process or enter follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 35.13% in this case.The water (saturation water being condensed into by exhaust steam) carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 8]
With reference to Fig. 4, with water as generating working medium, as a example by the catalytic gasification that bituminous coal and supercritical water occur.Coal makes the granularity coal dust less than 150 microns through attrition grinding, with catalyst n a2CO3It is the water-coal-slurry of 45% that (consumption is the 2% of quality of pc) and water are prepared as coal dust butt concentration.Water-coal-slurry is pressurized, and preheating reaches 28MPa, and 550 DEG C enter gasification furnace (in this embodiment, reactor is gasification furnace), are passed through oxygen in gasification furnace simultaneously.In gasification furnace, part water-coal-slurry and the oxygen reaction of addition, be promoted to 700 DEG C by temperature.In the supercritical state, coal reacts under the effect of catalyst with water, generates the mixed gas rich in methane.Mixed gas be mainly composed of methane, carbon monoxide, carbon dioxide, hydrogen etc..Go out gasification furnace product and include residue after mixed gas, supercritical water and reaction.Mixture and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump after this reaction, producing high temperature and high pressure steam, become exhaust steam after entering steam turbine expansion power generation, it is 21.08 DEG C that this exhaust steam can be controlled in temperature, absolute pressure is 0.0025MPa, and exhaust steam enters condenser and is condensed into aqueous water.nullMixed gas after heat exchange enters segregation apparatus，By mixed gas and water，Slag separates，Mixed gas after separation is reduced to 2.67MPa through expanding blood pressure lowering pressure，Temperature is down to-20.67 DEG C，Then this mixed gas and conventional chilling water stream carry out heat exchange in First Heat Exchanger，Then the cooling water after mixed gas cooling after leaving the mixed gas of this First Heat Exchanger and the expanded blood pressure lowering of generation each leads into the most independent pipeline and is used as cooling medium in condenser，Jointly exhaust steam is condensed into water, (now condenser has the first and second parts，The cooling water after mixed gas cooling after wherein the cooling medium of Part I is above-mentioned expanded blood pressure lowering，And the cooling medium of Part II is the mixed gas leaving this First Heat Exchanger，Condensation exhaust steam is continued first with Part I condensation exhaust steam recycling Part II，This mixed gas can enter subsequent separation process or enter follow-up gas turbine combustion generating afterwards.Generating efficiency is through being calculated as 35.43% in this case.The water (saturation water being condensed into by exhaust steam) carrying out condenser returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 9]
With reference to Fig. 5, with water as generating working medium, as a example by the catalytic gasification that bituminous coal and supercritical water occur.Coal makes the granularity coal dust less than 150 microns through attrition grinding, with catalyst n a2CO3It is the water-coal-slurry of 40% that (consumption is the 6% of quality of pc) and water are prepared as coal dust butt concentration.Water-coal-slurry is pressurized, and preheating reaches 23MPa, and 550 DEG C enter gasification furnace (in this embodiment, reactor is gasification furnace), are passed through oxygen in gasification furnace simultaneously.In gasification furnace, part water-coal-slurry and the oxygen reaction of addition, be promoted to 650 DEG C by temperature.In the supercritical state, coal reacts under the effect of catalyst with water, generates the mixed gas rich in methane and slurry-like residual carbon.Mixed gas be mainly composed of methane, carbon monoxide, carbon dioxide, hydrogen etc..After going out the reaction of gasification furnace, mixture includes mixed gas and slurry-like residual carbon.This product and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump, produce temperature and be 400 DEG C and absolute pressure is the high temperature and high pressure steam of 15MPa, this high temperature and high pressure steam becomes exhaust steam after entering steam turbines expansion power generation, it is 0.0022MPa that this exhaust steam can be controlled in pressure, temperature is 18.77 DEG C, and exhaust steam enters condenser and is condensed into water.After reaction after heat exchange, mixture enters separator and carries out gas/liquid and admittedly separate, mixed gas after separation is through expanding blood pressure lowering pressure drop as little as 3.33MPa, temperature is down to-14.31 DEG C, it is then used as the cooling medium of above-mentioned condenser, so that exhaust steam is condensed into aqueous water, this mixed gas can enter later separation unit or enter follow-up gas turbine combustion generating afterwards.Slurry-like residual carbon is then transported in oxidation reactor.In this oxidation reactor, it is passed through excessive oxygen, and relies on the oxidation reaction liberated heat of carbon residue and oxygen that the temperature and pressure in this oxidation reactor all rises to subcritical state or the supercriticality of water.Oxidation reaction is persistently carried out, and obtains comprising CO after reaction2And H2The fluid mixture of O and lime-ash, the produced heat of reaction for preheating water coal slurry or produces steam.Lime-ash discharges oxidation reactor, as construction material.CO is comprised described in and2And H2The mixture of O is then cooled off, then purifying and dedusting by preheating water coal slurry, expands and is depressurized to about about 2 DEG C, then carries out gas-liquid separation, obtain cryogenic liquid water and atmospheric carbon dioxide.Then this cryogenic liquid water is also passed in described condenser, for described expansion blood pressure lowering after mixed gas come together exhaust steam is cooled to condensed water.Generating efficiency is through being calculated as 35.88% in this case.Then will return to the second heat exchanger carries out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace after pump pressurizes from this condensed water.
[embodiment 10]
With reference to Fig. 6, with water as generating working medium, as a example by the catalytic gasification that bituminous coal and supercritical water occur.Coal makes the granularity coal dust less than 150 microns through attrition grinding, with catalyst n a2CO3It is the water-coal-slurry of 40% that (consumption is the 2% of quality of pc) and water are prepared as coal dust butt concentration.Water-coal-slurry is pressurized, and preheating reaches 23MPa, and 550 DEG C enter gasification furnace (in this embodiment, reactor is gasification furnace), are passed through oxygen in gasification furnace simultaneously.In gasification furnace, part water-coal-slurry and the oxygen reaction of addition, be promoted to 650 DEG C by temperature.In the supercritical state, coal reacts under the effect of catalyst with water, generates the mixed gas rich in methane and slurry-like residual carbon.Mixed gas be mainly composed of methane, carbon monoxide, carbon dioxide, hydrogen etc..After going out the reaction of gasification furnace, mixture includes mixed gas and slurry-like residual carbon.This product and the 23MPa water heat exchange in the second heat exchanger from force (forcing) pump, produce temperature and be 400 DEG C and absolute pressure is the high temperature and high pressure steam of 15MPa, this high temperature and high pressure steam becomes exhaust steam after entering steam turbine expansion power generation, it is 0.0019MPa that this exhaust steam can be controlled in pressure, temperature is 17.05 DEG C, and exhaust steam enters condenser and is condensed into the aqueous water that temperature is 16.88 DEG C.After reaction after heat exchange, mixture enters separator and carries out gas/liquid and admittedly separate, mixed gas after separation is reduced to 3.67MPa through expanding blood pressure lowering pressure, temperature is down to-11.57 DEG C, then being incorporated into certain heat exchanger (this heat exchanger be used for generate the heat exchanger of described steam be not a heat exchanger) to cool down cooling water as cooling medium, this mixed gas can enter later separation unit or enter follow-up gas turbine combustion generating afterwards.Slurry-like residual carbon is then transported in oxidation reactor.In this oxidation reactor, it is passed through excessive oxygen, and relies on the oxidation reaction liberated heat of carbon residue and oxygen that the temperature and pressure in this oxidation reactor all rises to subcritical state or the supercriticality of water.Oxidation reaction is persistently carried out, and obtains comprising CO after reaction2And H2The fluid mixture of O and lime-ash, the produced heat of reaction for preheating water coal slurry or produces steam.Lime-ash discharges oxidation reactor, as construction material.CO is comprised described in and2And H2The mixture of O is then cooled off, then purifying and dedusting by preheating water coal slurry, expands and is depressurized to about about 2 DEG C, then carries out gas-liquid separation, obtain cryogenic liquid water and atmospheric carbon dioxide.Then this cryogenic liquid water is also passed in certain heat exchanger described, for described expansion blood pressure lowering after mixed gas come together will to cooling water cool down.Then it is sent in condenser carry out heat exchange with exhaust steam by cooled cooling water, and exhaust steam is cooled to condensed water.Generating efficiency is through being calculated as 36.01% in this case.Then this condensed water returns to carry out heat exchange, to regenerate high temperature and high pressure steam with mixture after the reaction of the high temperature of gasification furnace in the second heat exchanger after pump pressurizes.
[embodiment 11]
Blood pressure lowering gas need not be expanded according to common, and with such as 32 DEG C water cooling exhaust steam of normal-temperature water, in the case of using water and dry saturated steam as Rankine circulatory mediator, the temperature of the dry saturated steam entering steam turbine is 400 DEG C, pressure is 15MPa, and the temperature going out the exhaust steam 5 of steam turbine is 46 DEG C, and pressure is 0.01Mpa, in this case, generating efficiency is computed about 33.42%.
In above example, generating efficiency=(T1Cv1-T2Cv2)/QRaw material× 100%,
Wherein:
QRaw materialIt is the coal in the calorific value of raw material, i.e. above example, mud or straw etc.；
T1It is the initial state temperature of power generation medium, the temperature before i.e. power generation medium enters steam turbines；
T2The final state temperature of power generation medium, i.e. exhaust steam temperature；
Cv1It is power generation medium initial state thermal capacitance, the thermal capacitance before i.e. power generation medium enters steam turbines；
Cv2Power generation medium final state thermal capacitance, i.e. exhaust steam thermal capacitance；
Those skilled in the art utilizes 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 includes the step of the gas generation energy products after the expanded blood pressure lowering after utilizing by absorption cold, such as, produce methane or hydrogen or carbon monoxide.This is applicable to above-mentioned all embodiments of the present invention.
Although all above embodiment is with water as generating working medium, but present invention is equally suited to generating working medium is the situation of any one in water, carbon dioxide, isoparaffin；Additionally, the feed coal added in reactor in embodiment can be replaced or increases other carbon-contained organic matter on the basis of coal, such as in addition to the situation shown in above-described embodiment, raw material can include biomass, mud, the carbon-contained organic matters such as high-concentration waste water, raw material can also include the mixture of coal and biomass, all these materials enter high-temperature high-voltage reaction device in a form of slurry, high-temperature high-voltage reaction includes surpassing/subcritical gasification reaction, the response types such as super/subcritical oxidation reaction and super/subcritical partial oxidation gasification reaction, wherein, the general operational requirement(GOR) of super/subcritical oxidation reaction is: the temperature range of reaction is 350-750 DEG C, the pressure limit of reaction is 15-40MPa.The pressure limit preferably passing through the gas (can be mixed gas) expanding blood pressure lowering in the present invention is 0.1-7Mpa.
On the other hand the present invention also provides for a kind of gasified production of energy products and the device of heat generating.See shown in Fig. 1-4, although these accompanying drawings are illustrated that flow chart, but combine this flow chart and be conducive to understanding assembly of the invention detailed description of the invention, be therefore described with reference to Fig. 1-4 when describing apparatus of the present invention.
Specifically, apparatus of the present invention include: expand dropping equipment, have and receive expanding blood pressure lowering entrance and discharging the expansion depressurization outlet passing through the gas expanding blood pressure lowering of blood pressure lowering gas to be expanded；And condenser, there is the first heat exchanger channels entered for the cooling medium being loaded with from the cold of the described gas through expanding blood pressure lowering and the exhaust steam produced for generating enter wherein with the second heat exchanger channels of described cooling medium heat exchange.Wherein, the gas that described process expands blood pressure lowering enters the first heat exchanger channels and countercurrently and carries out heat exchange by the wall of respective heat exchanger channels as cooling medium, the cooling medium in the first heat exchanger channels and the exhaust steam in the second heat exchanger channels.Or, apparatus of the present invention also include that First Heat Exchanger, the described gas through expanding blood pressure lowering enter a heat exchanger channels in First Heat Exchanger, and carry out heat exchange with the cooling water in another heat exchanger channels of First Heat Exchanger；By the wall of the two passage, cooling water carries out heat exchange with the gas through expansion blood pressure lowering, and this cooling water after heat exchange is discharged to the first heat exchanger channels of above-mentioned condenser as cooling medium from another described heat exchanger channels..
In one embodiment, condenser includes Part I and Part II, Part I and Part II each have two heat exchanger channels carrying out heat exchange each other, wherein two heat exchanger channels in Part I are aforesaid first and second heat exchanger channels, i.e. first heat exchanger channels is for the gas entrance through expanding blood pressure lowering, and the exhaust steam that the second heat exchanger channels produces for generating enters.In two heat exchanger channels of Part II, one heat exchanger channels is for the exhaust steam entrance after Part I heat release, another water entrance supplying to cool down exhaust steam, exhaust steam and water carry out heat exchange in respective passage and by the wall of passage each other, thus cool down exhaust steam further.It may be noted that, described being loaded with expands the cooling medium of blood pressure lowering gas cold and refers to two kinds of situations: one is the gas itself through expanding blood pressure lowering, and another is by described liquid after the gas cooling expanding blood pressure lowering (such as after expansion blood pressure lowering water) after gas heat release.
Further, apparatus of the present invention also include: with surpassing wherein for raw material/and subcritical gasification or the reactor of oxidation reaction, this reactor has air vent, and the reactant mixture generated for reaction is discharged；The second heat exchanger for reactant mixture with generating working medium heat exchange the most each other, this second heat exchanger has heat transferring medium entrance and generating working medium outlet, heat transferring medium entrance connects to receive the reactant mixture of autoreactor with the air vent of reactor, and the generating working medium after reactant mixture absorbs heat is discharged through generating working medium outlet；Utilize the turbine of the generating working medium generating after heat absorption, this turbine have with generating working medium outlet in order to receive the generating working medium after heat absorption (when generating working medium is water, generating working medium becomes steam after absorbing heat in heat exchanger) import, this turbine also has the exhaust steam outlet of the exhaust steam discharge produced for generating, second heat exchanger channels of condenser and exhaust steam outlet, condense wherein receiving exhaust steam.
The device of gasified production of energy products of the present invention and heat generating also includes: the segregation apparatus separated by gas in reactant mixture.This segregation apparatus is connected between aforesaid second heat exchanger (that is, aforesaid for reactant mixture and the heat exchanger of generating working medium heat exchange the most each other) and expansion dropping equipment.This segregation apparatus sends into expansion dropping equipment after gas is separated in reactant mixture, and this segregation apparatus discharges water and slag simultaneously.The above-mentioned functions of this segregation apparatus is referred to as purification function, in order to purify reactant mixture.
With the device of heat generating, gasified production of energy products of the present invention also includes that gas turbine and utilization are by the device of gas generation energy products after the expansion blood pressure lowering after absorption cold, when the gas through expansion blood pressure lowering that self-expanding dropping equipment generates since condenser is directly is as cooling medium, it is admitted to the fuel gas inlet of gas turbine for generating with after exhaust steam heat-shift within the condenser through expanding the gas of blood pressure lowering, or is admitted to produce in the device of energy products to produce such as methane or hydrogen or carbon monoxide or the energy products of their combination in any etc..At condenser with from when cooling down water as medium of aforementioned second heat exchanger discharge, carry out being admitted in the fuel gas inlet of gas turbine for gas turbine power generation after expanding the gas of blood pressure lowering and absorbing heat in this second heat exchanger of self-expanding dropping equipment, or be admitted in the device of production energy products to produce such as methane or hydrogen or carbon monoxide or the energy products of their combination in any etc..
In order to recycle exhaust steam condenser be cooled produce generating working medium (such as saturation water), apparatus of the present invention also include force (forcing) pump, in order to send in aforesaid second heat exchanger as generating working medium after the generating working medium (such as saturation water) of cooled generation being pressurizeed.Force (forcing) pump has pump intake and pump discharge, this second heat exchanger has the entrance flowed into for generating working medium, this entrance connects with pump discharge, and condenser has the outlet generating working medium (such as saturation water) of cooled generation discharged, and this outlet connects with pump intake.
To sum up, methods and apparatus of the present invention utilizes gas expansion blood pressure lowering can produce the lower cooling medium of relatively ambient temperature (such as room temperature) (gases through expanding blood pressure lowering of such as-25～20 DEG C), replace traditional room temperature cooling water to lower the temperature for exhaust steam, condensation, the temperature of exhaust steam can arrange below ambient temperature, both the generating efficiency of turbine power generation equipment can have been improved, the pressure energy of the gas being suitable for blood pressure lowering to be expanded acting produced by coal gasification equal energy source production technology can be made full use of again, this energy can also be used for generating, thus improve the energy utilization efficiency of whole process system, produce more clean electric power equal energy source product.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, any modification, equivalent substitution and improvement etc. made, should be included within the scope of the present invention.
Claims (22)
1. an electricity-generating method, the step condensed including the exhaust steam produced during to generating,
It is characterized in that, in this step, make described exhaust steam carry out heat exchange with the gas through expansion blood pressure lowering directly or indirectly,
Wherein, the step of described condensation farther includes: described exhaust steam and cooled cooling water carry out heat exchange；
Pulpous state carbon residue is transported to carbon dioxide and the mixture of water produced after oxidation reactor, and the mixture of this carbon dioxide and water obtains after dedusting, expansion blood pressure lowering and gas-liquid separation the liquid water of low temperature, and the liquid water of described low temperature is used as to cool down the cooling medium of described cooling water.
2. the method for claim 1, it is characterised in that
Described heat exchange is carried out within the condenser, described condenser using by described water after the gas cooling expanding blood pressure lowering as cooling medium, described exhaust steam directly carries out heat exchange in described condenser with described cooling medium.
3. the method for claim 1, it is characterised in that
Described heat exchange is carried out within the condenser, and described condenser is directly using the described gas through expanding blood pressure lowering as cooling medium, and described exhaust steam directly carries out heat exchange in described condenser with described cooling medium.
4. the method for claim 1, it is characterised in that
Described heat exchange is carried out within the condenser, described condenser includes Part I and Part II, the cooling medium of described Part I is water, the cooling medium of described Part II is the described gas through expanding blood pressure lowering, and described exhaust steam directly carries out heat exchange with the cooling medium in described Part I and Part II.
5. the method as according to any one of claim 1-4, it is characterised in that also include:
Raw material is sent into reactor carries out surpassing/subcritical gasification reaction or oxidation reaction reaction of formation mixture；
Wherein, the described gas through expanding blood pressure lowering, be carry out the gas separated from reactant mixture expanding blood pressure lowering after obtain.
6. method as claimed in claim 5, it is characterised in that also include:
Described reactant mixture is imported in the second heat exchanger and carry out heat exchange with generating working medium；
The generating working medium absorbing described reactant mixture institute heat content is imported in turbine and generates electricity；And
The gas generation energy products through expanding blood pressure lowering described in utilization, described energy products are methane or hydrogen or carbon monoxide or electricity or they combination in any.
7. the method for claim 1, it is characterised in that the temperature of the described gas through expanding blood pressure lowering is less than ambient temperature, and described ambient temperature refers to 28-32 DEG C.
8. method as claimed in claim 5, it is characterised in that described raw material is coal, biomass, mud or waste water, and containing gasifying agent or oxidant in described reactor, described gasifying agent or oxidant are at least one in oxygen, steam, air.
9. method as claimed in claim 6, it is characterised in that described generating working medium is water or carbon dioxide or isoparaffin.
10. method as claimed in claim 5, it is characterised in that described raw material occurs to surpass in described reactor/and subcritical gasification reaction or temperature conditions during oxidation reaction be 350-750 DEG C, pressure condition is 15-40Mpa.
11. the method for claim 1, it is characterised in that the described pressure through expanding the gas of blood pressure lowering with 0.1-7MPa.
12. methods as claimed in claim 5, it is characterised in that the gas that described reactant mixture comprises be raw material super/gas that produces of the gas that produces of subcritical gasification reaction or raw material oxidation reaction.
13. 1 kinds for gasified production of energy products and the device of heat generating, it is characterised in that described device includes:
Expand dropping equipment, have and receive expanding blood pressure lowering entrance and discharging the expansion depressurization outlet passing through the gas expanding blood pressure lowering of blood pressure lowering gas to be expanded；And
Condenser, have for be loaded with described through expansion blood pressure lowering gas cold cooling medium enter the first heat exchanger channels and for generating produce exhaust steam enter wherein with the second heat exchanger channels of cooling medium heat exchange in described first heat exchanger channels,
Wherein, described condenser includes Part I and Part II, described first heat exchanger channels and the second heat exchanger channels are located in described Part I, and described Part II has confession exhaust steam after described Part I heat release and enters one of them heat exchanger channels and for water entrance another heat exchanger channels therein in order to cool down exhaust steam in this heat exchanger channels.
14. devices as claimed in claim 13, it is characterised in that described expansion depressurization outlet connects with described first heat exchanger channels, wherein through expanding gas described first heat exchanger channels of entrance of blood pressure lowering as described cooling medium.
15. devices as claimed in claim 13, it is characterized in that, also include that First Heat Exchanger, the described gas through expanding blood pressure lowering enter a heat exchanger channels in described First Heat Exchanger, and carry out heat exchange with the cooling water in another heat exchanger channels of described First Heat Exchanger
Wherein, with the cooling water after the described gas converting heat through expanding blood pressure lowering, another heat exchanger channels described in from First Heat Exchanger is discharged in the first heat exchanger channels of described condenser as cooling medium.
16. devices as according to any one of claim 13-15, it is characterised in that also include:
With the reactor reacted wherein for raw material, this reactor has the air vent of the reactant mixture discharge generated for reaction；
For the second heat exchanger of reactant mixture and generating working medium heat exchange each other, this second heat exchanger have connect with described air vent in order to the heat transferring medium entrance receiving reactant mixture and the generating working medium outlet will discharged from the generating working medium after reactant mixture absorbs heat；And
Utilize the turbine of the generating working medium generating after heat absorption, this turbine has the import in order to the generating working medium after receiving heat absorption with generating working medium outlet and the exhaust steam for the exhaust steam discharge of generating generation exports, and described exhaust steam outlet connects with the exhaust steam entrance of described condenser.
17. devices as claimed in claim 16, it is characterised in that also including the segregation apparatus separated by gas in reactant mixture, this segregation apparatus is connected between described second heat exchanger and described expansion dropping equipment.
18. devices as claimed in claim 14, it is characterized in that, also include that gas turbine, described gas turbine have fuel gas inlet, described condenser have for described exhaust steam heat-shift after expand blood pressure lowering gas discharge outlet, this outlet connects with described fuel gas inlet.
19. devices as claimed in claim 15, it is characterized in that, also include gas turbine, described gas turbine has fuel gas inlet, described First Heat Exchanger have for in another heat exchanger channels described in this First Heat Exchanger cooling water heat exchange after expand blood pressure lowering gas discharge outlet, this outlet connects with described fuel gas inlet.
20. devices as claimed in claim 16, it is characterised in that also include force (forcing) pump, there is pump intake and pump discharge,
Wherein, described second heat exchanger has the entrance flowed into for generating working medium, and this entrance connects with the pump discharge of described force (forcing) pump,
Wherein, described condenser has the outlet discharged by the saturation water generated after exhaust steam condensation, and this outlet connects with the pump intake of described force (forcing) pump.
21. devices as claimed in claim 14, it is characterised in that also include:
The device of gas generation energy products after expansion blood pressure lowering after utilizing by absorption cold, has the entrance for being entered by gas after the described expansion blood pressure lowering after absorption cold,
Wherein, described condenser have for described exhaust steam heat-shift after expand blood pressure lowering gas discharge outlet, this outlet connects with the described entrance of the device of described production energy products.
22. devices as claimed in claim 15, it is characterised in that also include:
The device of gas generation energy products after expansion blood pressure lowering after utilizing by absorption cold, has the entrance for being entered by gas after the described expansion blood pressure lowering after absorption cold,
Wherein, described First Heat Exchanger have for this First Heat Exchanger in described in expand the outlet that blood pressure lowering gas is discharged after cooling water heat exchange in another heat exchanger channels, this outlet connects with the described entrance of the device of described production energy products.
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Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| CN109252842B (en) * | 2018-10-29 | 2024-04-12 | 邓晓亮 | Mixed gas triple power generation system produced by underground supercritical coal gasification |
| CN111636935A (en) * | 2019-04-15 | 2020-09-08 | 李华玉 | Single working medium steam combined cycle |
| CN111608758A (en) * | 2019-04-17 | 2020-09-01 | 李华玉 | Single working medium steam combined cycle |
| CN110259534A (en) * | 2019-05-28 | 2019-09-20 | 江苏大学 | A kind of gasification of biomass organic rankine cycle system |
| CN115478920A (en) * | 2019-06-13 | 2022-12-16 | 李华玉 | 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 |
| CN111412022B (en) * | 2020-03-24 | 2021-02-09 | 西安交通大学 | Coal supercritical water gasification power generation system for controlling available energy loss and working method |
| 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 |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH656637A5 (en) * | 1981-10-26 | 1986-07-15 | Sulzer Ag | GAS COOLER ARRANGEMENT TO COAL GASIFICATION SYSTEM. |
| JPH08246813A (en) * | 1995-03-10 | 1996-09-24 | Hitachi Ltd | Operation method and device for coal gasification compound generation plant |
| UA107461C2 (en) * | 2009-05-22 | 2015-01-12 | Sasol Tech (Proprietary) Ltd | A metod for synthesis gas and power co-producing |
-
2012
- 2012-01-06 CN CN201210002533.4A patent/CN102518489B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
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