WO2014075219A1 - 中低温太阳能与化石燃料热化学互补的发电系统与方法 - Google Patents

中低温太阳能与化石燃料热化学互补的发电系统与方法 Download PDF

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Publication number
WO2014075219A1
WO2014075219A1 PCT/CN2012/084522 CN2012084522W WO2014075219A1 WO 2014075219 A1 WO2014075219 A1 WO 2014075219A1 CN 2012084522 W CN2012084522 W CN 2012084522W WO 2014075219 A1 WO2014075219 A1 WO 2014075219A1
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Prior art keywords
fuel
solar
raw material
power generation
solar energy
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PCT/CN2012/084522
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English (en)
French (fr)
Inventor
金红光
刘启斌
洪慧
隋军
韩巍
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中国科学院工程热物理研究所
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Priority to US14/345,465 priority Critical patent/US9316124B2/en
Priority to PCT/CN2012/084522 priority patent/WO2014075219A1/zh
Publication of WO2014075219A1 publication Critical patent/WO2014075219A1/zh

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K15/00—Adaptations of plants for special use
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
    • F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
    • F03G6/00—Devices for producing mechanical power from solar energy
    • F03G6/06—Devices for producing mechanical power from solar energy with solar energy concentrating means
    • F03G6/064—Devices for producing mechanical power from solar energy with solar energy concentrating means having a gas turbine cycle, i.e. compressor and gas turbine combination
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
    • F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
    • F03G6/00—Devices for producing mechanical power from solar energy
    • F03G6/06—Devices for producing mechanical power from solar energy with solar energy concentrating means
    • F03G6/065—Devices for producing mechanical power from solar energy with solar energy concentrating means having a Rankine cycle
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0855—Methods of heating the process for making hydrogen or synthesis gas by electromagnetic heating
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E10/00—Energy generation through renewable energy sources
    • Y02E10/40—Solar thermal energy, e.g. solar towers
    • Y02E10/46—Conversion of thermal power into mechanical power, e.g. Rankine, Stirling or solar thermal engines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight

Definitions

  • the present invention relates to the field of solar energy technologies, and in particular, to a power generation system and method for thermo-chemical complementary of medium-low temperature solar energy and fossil fuel, in particular to utilizing low-concentration light.
  • Solar energy has the characteristics of unlimited reserves and cleanliness. The development and utilization of solar energy is of great significance to meet the growing energy needs of civilization and reduce greenhouse gas emissions. Because solar energy itself has the characteristics of low energy density, instability, and discontinuity, the power generation efficiency of solar thermal power generation technology alone is only 10%-17%, and there are problems such as high energy storage cost.
  • Solar thermal chemistry is a kind of solar thermal utilization technology. It converts the collected solar energy into fuel chemical energy through an endothermic chemical reaction process, and the converted fuel can realize storage and high-efficiency power generation, thereby realizing solar heat energy. Efficient use of storage and solar energy.
  • thermochemical technology with a reaction temperature above 600 °C, mainly including solar pyrolysis water hydrogen production, solar energy driven fossil energy hydrogen production and other directions.
  • high-temperature thermochemical processes require expensive solar concentrating devices to concentrate high-grade solar energy to provide the heat energy required for the reaction, while high-temperature solar thermochemical processes exist. Difficulties and bottlenecks such as low thermal efficiency, difficulty in sun tracking, and high requirements on reactor materials make it difficult to achieve large-scale promotion and application.
  • the object of the present invention is to provide a power generation system and method for thermo-chemical complementary of low-temperature solar energy and fossil fuel, which can greatly improve the net power generation efficiency of solar energy, lower the operating temperature, thereby reducing the power generation cost, and by chemical energy storage. Break through the technical bottleneck of unstable output of solar thermal power generation system.
  • the present invention provides a power generation system in which a medium-low temperature solar energy and a fossil fuel thermal chemistry are complementary, the system comprising:
  • a raw material supply device for storing fossil fuel and outputting the stored fossil fuel to the raw material mixing device
  • a raw material mixing device for receiving and mixing the fossil fuel from the raw material supply device and the unreacted material separated from the gas-liquid separator, and outputting the obtained mixture to the raw material metering device;
  • a raw material metering device for controlling the amount of raw materials entering the raw material preheating device per unit time, and outputting the raw materials received from the raw material mixing device to the raw material preheating device according to the solar energy resource and the user end demand;
  • a raw material preheating device that heats the raw material received from the raw material metering device by using the exhaust heat of the power generation equipment to generate a fossil fuel vapor output to the solar energy absorption reactor;
  • the solar absorption reactor drives the fossil fuel vapor received from the raw material preheating device to undergo decomposition or reforming reaction under the action of the absorbed solar heat to convert solar energy into hydrogen-rich fuel chemical energy to generate solar fuel;
  • Solar collector for integrating low-energy flow-density solar energy into high-energy flow-density medium-low temperature heat energy in a linear focusing manner, converting solar energy into fossil fuel in solar energy absorption reactor The fuel reacts to provide heat;
  • a condenser for cooling a reaction product received from the solar absorption reactor, and outputting the cooled reaction product to the gas-liquid separator
  • a gas-liquid separator for performing gas-liquid separation on the mixture received from the condenser, and the separated gas phase reaction product is output to the fuel splitting device, and the obtained liquid phase reaction product is output to the raw material mixing device;
  • the fuel splitting device controls the solar fuel flow to the power generating equipment and the gas storage tank according to the solar energy resource and the user's energy requirement, thereby realizing the regulation of the solar thermal chemical complementary power generation system;
  • the solar energy resources when the solar energy resources are sufficient, the excess solar fuel is stored to realize chemical energy storage; when the solar energy resources are insufficient, the solar fuel in the gas storage tank is supplemented into the power generation equipment to realize the system output regulation;
  • Power generation equipment using solar fuel as fuel, drives the generator set to generate electricity and output electrical work.
  • the present invention also provides a power generation method for thermo-chemical complementary of medium-low temperature solar energy and fossil fuel, which is applied to the system, the method comprising:
  • the raw material mixing device thoroughly mixes the fossil fuel input from the raw material supply device and the unreacted material input from the gas-liquid separator, and outputs it to the raw material metering device;
  • the raw material metering device outputs the raw material input from the raw material mixing device to the preheater at a certain rate, and the preheater preheats the received raw material, and then outputs the raw material to the solar energy absorption reactor;
  • the solar absorption reactor utilizes the absorbed solar heat for the raw material received from the preheater to undergo decomposition or reforming reaction in its own reaction tube, and the reaction product enters the condenser;
  • the condenser cools the reaction product from the solar absorption reactor, and outputs the cooled reaction product to the gas-liquid separator;
  • the gas-liquid separator performs gas-liquid separation on the reaction product received from the condenser cooling, and the gas phase reaction product obtained after separation is output to the fuel splitting device, and the obtained liquid phase reaction product is output to the raw material mixing device;
  • the fuel splitting device controls a certain amount of solar fuel to flow to the power generating device, allows excess solar fuel to flow to the gas storage tank, or makes the solar fuel in the gas storage tank make up the flow Power generation equipment;
  • the power generation equipment burns the solar fuel from the fuel splitting device, outputs electric energy, and the discharged heat is introduced into the raw material preheater to preheat the raw material.
  • the chemical energy of the raw materials such as methanol, ethanol and dimethyl ether after the endothermic reaction is converted into the chemical energy of the solar fuel, and the solar thermal energy that drives the endothermic reaction is also converted into chemical energy.
  • the effect of the system provided by the present invention on the first law of thermodynamics is to increase the energy of the reaction product, and the increased portion is equal to the solar thermal energy absorbed by the solar fuel conversion reaction; the effect on the second law of thermodynamics is reflected in the improvement of the solar thermal energy grade.
  • the endothermic reaction of conversion to solar fuels such as methanol, ethanol and dimethyl ether promotes low-grade solar thermal energy to high-grade fuel chemical energy. High-grade solar fuels achieve high-efficiency power generation through power units, which greatly increases the net power generation efficiency of solar energy.
  • the solar collector adopts a parabolic trough concentrating structure, that is, a single-axis tracking solar parabolic trough concentrating device, and has a simple structure, and the inner surface of the parabolic trough is coated with high reflectivity and low absorption rate for sunlight.
  • the selective coating provides heat in the temperature range of 150 ° C to 300 ° C to the raw material reforming reaction in the solar absorption reactor. Compared with high temperature solar collectors, the manufacturing and operating costs are lower, which is advantageous for large scale. Promotion and application.
  • the solar absorption reactor integrates the solar absorber with the reactor equipment, and the integrated device placed on the focal axis of the solar concentrating device is both a solar receiver and a reactor, and the high energy flow density of the gathering
  • the direct sunlight is directly irradiated on the solar absorption reactor to directly supply heat for the endothermic chemical reaction.
  • the system flow is simple, the cost of using the heat medium is greatly reduced, and the heat loss caused by the storage and transfer of the heat medium is also avoided. Integration of absorption/reactor structural features not only helps to reduce heat loss, but also facilitates the decomposition or reforming reaction, achieves coupling of heat transfer and reaction, and achieves good solar energy conversion.
  • the amount of solar fuel generated is greater than the power
  • the fuel demand of the generator set is required, excessive solar fuel enters the gas storage tank to realize chemical energy storage; when the solar energy resources are insufficient and the amount of solar fuel generated cannot meet the fuel demand of the power generating unit, the solar fuel output stored in the gas storage tank To the power generator set, to make up the required fuel, so as to realize the regulation of the operation of the power generation system in which the low-temperature solar energy and the fossil fuel are thermochemically complementary, breaking through the technical bottleneck of the unstable output of the solar thermal power generation system; due to the discontinuity of the solar energy resources,
  • the thermoelectrically complementary power generation system of low-temperature solar energy and fossil fuel needs to start and stop periodically.
  • the gas storage tank outputs solar fuel to the power generation equipment to start, generating flue gas preheating raw materials, avoiding the use of extra energy to start the system.
  • the present invention has greater advantages for the following users: factories and users who need small and medium-sized power supply; users who need gaseous fuel without gas access conditions (such as urban areas, areas not covered by natural gas pipeline networks, mountains, islands, etc.) Terrain conditions are not conducive to gas supply); solar radiation resources are good (most parts of China, especially the western region;).
  • FIG. 1 is a schematic structural view of a power generation system in which a medium-low temperature solar energy and a fossil fuel are thermochemically complementary;
  • thermochemical complementary thermo-chemical combination of low-temperature solar energy and fossil fuel provided by the present invention
  • FIG. 3 is a schematic diagram of a power generation system for thermo-chemical complementary of medium-low temperature solar energy and fossil fuel according to an embodiment of the present invention
  • 1 is a raw material tank
  • 2 is a raw material mixing device
  • 3 is a raw material metering device
  • 4 is a raw material preheating device
  • 5 is a solar collector
  • 6 is a solar absorption reactor
  • ⁇ is a condenser.
  • 8 is a gas-liquid separator
  • 9 is a fuel splitting device
  • 10 is a gas storage tank
  • 11 is a power generation device.
  • FIG. 1 is a schematic structural view of a power generation system in which a medium-low temperature solar energy and a fossil fuel are thermochemically complementary, and the system includes a raw material supply device 1, a raw material mixing device 2, a raw material metering device 3, and a raw material preheating.
  • the apparatus 4 the solar absorption reactor 5, the solar collector 6, the condenser 7, the gas-liquid separator 8, the fuel splitting device 9, the gas tank 10, and the power generating equipment 11.
  • the raw material supply device 1 is for storing fossil fuel, and outputs the stored fossil fuel to the raw material mixing device 2.
  • the raw material supply device is a fuel tank in which the stored fossil fuel is methanol, ethanol, dimethyl ether or the like.
  • the raw material mixing device 2 is for receiving and mixing the unreacted materials separated from the fossil fuel and the gas-liquid separator 8 in the raw material supply device 1, and outputs the obtained mixture to the raw material metering device 3.
  • the raw material mixing device is a mixer for mixing unreacted materials separated from the fossil fuel in the raw material tank and the gas-liquid separator.
  • the raw material metering device 3 is for controlling the amount of the raw material entering the preheater 4 per unit time, and the raw material received from the raw material mixing device 2 is output to the raw material preheating device 4 at a certain rate according to the solar energy resource and the demand of the customer end.
  • the raw material metering device is a metering pump, and the raw material is pumped into the heat exchanger of the raw material preheating device, and the flow rate of the output raw material is adjusted according to the solar energy resource and the user's demand.
  • the raw material preheating device 4 heats the raw material from the raw material measuring device 3 by the exhaust heat of the power generating device 11 to generate the fossil fuel vapor to be output to the solar energy absorbing reactor 5.
  • the raw material preheating device includes a heat exchanger that uses the exhaust gas of the power generation equipment to exchange heat with the raw materials, and the generated fossil fuel vapor is introduced into the solar absorption reactor.
  • the solar absorption reactor 5 uses the absorbed solar heat to drive the fossil fuel vapor received from the raw material preheating device 4 to undergo decomposition or reforming reaction under the action of a catalyst to convert solar energy into hydrogen-rich fuel chemical energy to produce solar fuel.
  • the solar absorption reactor is a chemical reactor, and the structure is tubular.
  • the material is steel, copper, aluminum and the like with good thermal conductivity.
  • the tube is filled with a solid metal series catalyst such as copper, nickel or platinum palladium.
  • the outer surface is coated with a selective coating having a high absorptivity to sunlight and a low reflectivity emissivity.
  • a high transmittance glass cover is mounted on the outside of the tube, and a vacuum or non-vacuum between the glass cover and the tube.
  • Solar collector 6 is used to integrate low energy density solar energy in a linear focusing manner
  • the low-energy thermal energy of high energy flow density provides heat to the fossil fuel conversion solar fuel reaction in the solar absorption reactor 5: the solar collector 6 adopts a parabolic trough concentrating structure, and the solar absorption reactor 5 is located in the solar collector On the linear focus line, the inner surface of the parabolic trough is a selective material having high reflectivity and low absorptivity to sunlight, and provides heat energy of 150 ° C to 300 ° C to the raw material conversion reaction in the solar absorption reactor;
  • the condenser 7 is for cooling the reaction product from the solar absorption reactor 5, and outputs the cooled reaction product to the gas-liquid separator 8.
  • the condenser is a partition wall heat exchange device, which is cooled by circulating water and connected with circulating cooling water.
  • the gas-liquid separator 8 is for gas-liquid separation of the mixture received from the condenser 7, and the gas phase reaction product obtained after the separation is output to the fuel splitting device 9, and the obtained liquid phase reaction product is output to the raw material mixing device 2.
  • the gas phase reaction product obtained after the separation of the gas-liquid separator is a solar fuel such as hydrogen or carbon monoxide and a small amount of by-product, and the liquid phase reaction product is an unreacted raw material, water or the like.
  • the fuel splitting device 9 controls the flow of solar fuel to the power generating equipment 11 and the gas storage tank 10 according to the solar energy resources and the user's energy demand, thereby realizing the regulation of the solar thermal chemical complementary power generation system.
  • the fuel splitting device is a flow regulating device, which controls the flow of the solar fuel to the power generating device, so that the excess solar fuel enters the gas storage tank; when the solar energy resource is insufficient, the solar fuel in the gas storage tank is regulated to be replenished into the power generating device. To meet the fuel demand of power generation equipment.
  • the gas storage tank 10 When the solar energy resources are sufficient, the gas storage tank 10 accumulates excess solar fuel to realize chemical energy storage. When the solar energy resources are insufficient, the solar fuel in the gas storage tank 10 is supplemented into the power generation equipment 11 to realize system output regulation.
  • the gas storage tank is a pressure-resistant container for storing solar fuel from the flow dividing device to realize energy storage, and outputs solar fuel to supplement the fuel required for the power generation equipment when the solar energy resource is insufficient.
  • Power generation equipment 11 using solar fuel as fuel, drives the generator set to generate electricity and output electrical work.
  • the power generation equipment is an internal combustion engine or a micro-combustion engine generator set that combusts solar fuel to generate electricity and outputs electrical energy.
  • FIG. 2 is a schematic structural view of a power generation system in which a medium-low temperature solar energy and a fossil fuel are thermochemically complementary, and FIG. 2 illustrates a medium-low temperature solar energy and fossil fuel thermochemistry provided by the present invention.
  • Step 201 The raw material mixing device thoroughly mixes the fossil fuel input from the raw material supply device and the unreacted material input from the gas-liquid separator, and outputs the same to the raw material metering device;
  • Step 202 The raw material metering device outputs the raw material input from the raw material mixing device to the preheater at a certain rate, and the preheater preheats the received raw material, and then outputs the raw material to the solar energy absorption reactor;
  • Step 203 The solar absorption reactor utilizes the absorbed solar heat for the raw material received from the preheater to undergo decomposition or reforming reaction in its own reaction tube, and the reaction product enters the condenser;
  • Step 204 The condenser cools the reaction product from the solar absorption reactor, and outputs the cooled reaction product to the gas-liquid separator;
  • Step 205 The gas-liquid separator performs gas-liquid separation on the reaction product received from the condenser cooling, and the gas phase reaction product obtained after the separation is output to the fuel splitting device, and the obtained liquid phase reaction product is output to the raw material mixing device;
  • Step 206 The fuel splitting device controls a certain amount of solar fuel to flow to the power generating device, and the excess solar fuel flows to the gas storage tank, or the solar fuel in the gas storage tank is supplemented to the power generating device;
  • Step 207 The power generation device burns the solar fuel from the fuel splitting device, outputs the electric energy, and the discharged flue gas is introduced into the raw material preheater to preheat the raw material.
  • the raw material supply device of step 201 is a fuel tank, wherein the stored fossil fuel is methanol, ethanol, etc., dimethyl ether, etc.; the raw material mixing device in step A is a mixer for receiving fossil fuel from the raw material tank. The unreacted material separated from the gas-liquid separator is mixed.
  • the raw material metering device described in step 202 is a metering pump for pumping raw materials into the heat exchanger of the raw material preheating device, and adjusting the flow rate of the output raw material according to the solar energy resource and the user's demand.
  • Step 203 includes: the raw material outputted to the solar absorption reactor by the raw material preheating device becomes superheated steam after being preheated by the raw material preheating device and evaporated by the solar absorption reactor, at a normal pressure, a reaction temperature of 150 to 300 ° C, and a copper system, Under the action of a nickel-based or platinum-palladium-based solid metal catalyst, the amount of solar energy collected from the solar collector is decomposed or reformed.
  • the gas phase reaction product is solar fuel hydrogen, carbon monoxide and a small amount of by-products.
  • the product should be unreacted fossil fuel and water which is passed from the solar absorption reactor to the condenser.
  • the condenser is a partition wall heat exchange device, which is cooled by circulating water and connected with circulating cooling water.
  • the gas phase reaction product in the step 205 is a solar fuel such as hydrogen or carbon monoxide and a small amount of by-products, and the liquid phase reaction product is an unreacted raw material, water or the like.
  • the fuel splitting device is a flow regulating valve that controls the flow of solar fuel to the power generating equipment, so that excess solar fuel enters the gas storage tank, and when the solar energy is insufficient, the solar fuel in the gas storage tank is adjusted to enter the power.
  • Power generation equipment to meet the fuel demand of the power generation equipment;
  • the gas storage tank is a pressure-resistant container, equipped with a safety valve and a pressure gauge for storing solar fuel from the flow dividing device to realize energy storage, and when the solar energy resources are insufficient
  • the output of solar fuel complements the fuel required for power generation equipment.
  • the power generating device in step 207 is an internal combustion engine generator set that combusts solar energy to output electrical energy, and the discharged residual heat is introduced into the raw material preheater to preheat the raw material.
  • Power generation equipment can also use micro-combustion generator sets.
  • FIG. 1 is a schematic structural view of a power generation system in which a medium-low temperature solar energy and a fossil fuel are thermochemically complementary, and a flowchart of a power generation method in which a medium-low temperature solar energy and a fossil fuel are thermochemically complementary, and the following is a specific embodiment.
  • the invention further details the power generation method using thermo-chemical complementary of medium-low temperature solar energy and fossil fuel.
  • FIG. 3 is a schematic diagram of a power generation system in which a medium-low temperature solar energy and a methanol are thermochemically complementary according to an embodiment of the present invention.
  • the methanol in the raw material supply device 1 and the liquid phase product from the gas-liquid separator S are thoroughly mixed in the raw material mixing device 2, and after passing through the pipe 12, the raw material metering device 3 is fed into the raw material through the pipe 13 at a volume flow rate of 5.57 1 /min.
  • the heat device 4 exchanges heat with the exhaust gas of the internal combustion engine at 450 °C in the raw material preheating device 4, and the generated methanol vapor enters the solar absorption reactor 5 through the pipe 14.
  • the device 5 absorbs and converts into thermal energy, and drives the decomposition reaction of methanol under the action of the copper-based catalyst in the form of reaction heat to produce a syngas solar fuel having a molar ratio of H 2 to CO of 2:1.
  • the syngas solar fuel is cooled by the circulating cooling water in the condenser 7 through the pipe 15, and the cooled mixture is passed through the pipe 16 to effect gas-liquid separation in the gas-liquid separator 8.
  • the separated liquid phase reaction product is unreacted methanol and a small amount of by-product, and the liquid phase reaction product is returned to the raw material mixing device 2 through the pipe 17;
  • the gas phase reaction product is mainly a synthesis gas having a molar ratio of H 2 to CO of 2:1, and is synthesized.
  • the gas solar fuel passes through the pipe 18, and under the action of the fuel splitting device 9, according to the fuel demand of the internal combustion engine generator set 11, flows to the internal combustion engine generator set 11 to realize electric energy output, or flows to the gas storage tank 10 to realize chemical energy storage.
  • the syngas solar fuel in the gas storage tank 10 is mixed with the syngas generated in real time through the pipeline 21 to make up the fuel demand of the internal combustion engine generator set 11, and flows through the pipeline 22 to the internal combustion engine generator set 11 for combustion work. .
  • the 450 ° C flue gas discharged from the internal combustion engine generator set 11 is introduced into the raw material preheating device 4 through the line 23 to preheat the methanol raw material, and is discharged to the environment through the pipe 24.
  • a parabolic trough solar collector with a concentration ratio of 82:1 is used.
  • the opening width of the collector is 5.76 m
  • the mirror field is 715 m 2
  • the length of the mirror field is 124 m .
  • the raw material is liquid industrial methanol at room temperature of 99.9%, solar absorption.
  • the filler in the reactor is a Cu/ZnO/Al 2 O 3 solid metal series catalyst, and the power generation efficiency of the internal combustion engine generator set is 42%, and the exhaust gas temperature is 450 °C.
  • the liquid phase product separated from the lower end of the separator is mainly unreacted methanol and a small amount of liquid by-product, and the gas phase products separated at the upper end of the condensing separator are mainly H 2 and CO.
  • the solar absorption reactor can generate 267 kg/hr of syngas solar fuel, of which 43 kg/hr of syngas.
  • Solar fuel enters the gas storage tank for chemical energy storage, 224 kg/hr of syngas solar fuel is input into the combustion work of the internal combustion engine generator set, and the internal combustion engine generator set outputs 600 kW of electric power to the outside, and the net solar power generation efficiency reaches 28%.
  • Exceeding solar power alone generates 10-17% of the level.
  • the solar absorption reactor can generate 401 kg/hr of syngas solar fuel, and the mass flow of solar fuel flowing to the gas storage tank is increased to 177 kg/hr.
  • the unit's solar fuel mass flow is still 224 kg / hr; when the solar radiation intensity is reduced to 300 W / m 2 , solar absorption response
  • the device can generate 134 kg/hr of syngas solar fuel.
  • the mass flow rate of solar fuel flowing to the gas storage tank is 0, and the storage tank outputs the stored syngas solar fuel, and the output syngas mass flow rate is 90 kg/hr. Therefore, the mass flow rate of the syngas solar fuel entering the internal combustion engine generator set is still 224 kg/hr.
  • the internal combustion engine generator set is stable under the rated working condition, breaking through the technical bottleneck of the drastic decline of the performance of the power generation equipment under the variable irradiation condition.
  • the invention can be applied in a variety of applications, especially to achieve small-scale power supply in remote areas, opening up a way to achieve thermo-chemical complementary power generation between low-temperature solar energy and fossil fuels.

Abstract

一种中低温太阳能与化石燃料化学互补的发电系统与方法。该系统包括：原料供应装置（1），用于贮存化石燃料；原料混合装置（2），用于混合原料和未反应物；原料计量装置（3），用于控制单位时间内原料进入预热器（4）的量；预热器，用于对原料进行预热；太阳能吸收反应器（5），利用吸收的太阳能热量驱动化石燃料进行分解或者重整反应，将太阳能转换为富氢的燃料化学能，产生太阳能燃料；太阳能集热器（6），将低能流密度的太阳能聚集成高能流密度的中低温热能，向分解或重整反应提供热量；冷凝器（7），用于冷却反应产物；气液分离器（8），用于对混合物进行气液分离；燃料分流装置（9），调节用于蓄能或发电的太阳能燃料的比例；储气罐（10），储存太阳能燃料；动力发电设备（11），燃烧太阳能燃料对外输出电能。该系统实现了太阳能的高效发电利用。

Description

中低温太阳能与化石燃料热化学互补的发电系统与方法 技术领域 本发明涉及太阳能技术领域， 尤其涉及一种中低温太阳能与化石燃 料热化学互补的发电系统与方法， 特别是一种利用低聚光比太阳能聚光 装置将中低品位太阳能转换为髙品位太阳能燃料并实现发电的系统及 方法。
背景技术 随着人类社会的发展进步， 由于提高生活水平和推动社会发展的需 要， 人类对于能源的需求日益增加， 而传统化石能源总量有限， 不可再 生， 同时化石能源的使用过程伴随着严重的污染物产生和温室气体排 放。 日益枯竭的化石能源和人类不断增加的能源需求， 以及对环境保护 的迫切要求形成了尖锐的矛盾， 严重影响人类的可持续发展。 开发和利 用太阳能等清洁的可再生能源是缓解能源供需矛盾， 保护自然环境， 实 现可持续发展的重要途径。
太阳能具有储量无限性、 清洁性的特点， 开发和利用太阳能对于满 足人类日益增长的能源需求、 减少温室气体排放具有重要意义。 由于太 阳能本身具有能量密度低、 不稳定、 不连续等特点， 单独太阳能热发电 利用技术的发电效率仅为 10%-17%， 并存在蓄能成本高等问题。
太阳能热化学技术是太阳能热利用技术的一种， 它通过吸热化学反 应过程， 将所聚集的太阳能转化为燃料的化学能， 转化后的燃料可以实 现蓄存和高效发电， 从而实现太阳热能的蓄存和太阳能的高效利用。
目前国际上对太阳能热化学的研究集中于反应温度 600°C以上的高 温热化学技术， 主要包括太阳能高温分解水制氢、 太阳能驱动化石能源 制氢等方向。 但高温热化学过程需要昂贵的太阳能聚光装置， 聚集高品 位的太阳能， 以提供反应所需热能， 同时高温太阳能热化学过程存在集 热效率低、 太阳跟踪困难、 对反应器材料要求高等难点与瓶颈， 难以实 现大规模推广应用。
发明内容
(一） 要解决的技术问题
有鉴于此， 本发明的目的是提出一种中低温太阳能与化石燃料热化 学互补的发电系统及方法， 以大幅提高太阳能净发电效率， 降低操作温 度以实现降低发电成本， 并通过化学蓄能来突破太阳能热发电系统输出 不稳定的技术瓶颈。
(二） 技术方案
为达到上述目的， 本发明提供了一种中低温太阳能与化石燃料热化 学互补的发电系统， 该系统包括：
原料供应装置， 用于贮存化石燃料， 并将贮存的化石燃料输出给原 料混合装置；
原料混合装置， 用于接收并混合来自原料供应装置中的化石燃料和 来自气液分离器中分离出来的未反应物， 并将得到的混合物输出给原料 计量装置；
原料计量装置， 用于控制单位时间内原料进入原料预热装置的量， 根据太阳能资源和用户端需求将接收自原料混合装置的原料按一定的 速率输出给原料预热装置；
原料预热装置， 利用动力发电设备的排烟余热加热接收自原料计量 装置的原料， 产生化石燃料蒸气输出给太阳能吸收反应器；
太阳能吸收反应器， 利用吸收的太阳能热量驱动接收自原料预热装 置的化石燃料蒸气在催化剂作用下进行分解或重整反应， 将太阳能转换 为富氢的燃料化学能， 产生太阳能燃料；
太阳能集热器， 用于以线性聚焦方式将低能流密度的太阳能聚集成 高能流密度的中低温热能， 为太阳能吸收反应器中的化石燃料转换太阳 能燃料反应提供热量；
冷凝器， 用于冷却接收自太阳能吸收反应器的反应产物， 并将冷却 后的反应产物输出给气液分离器；
气液分离器， 用于对接收自冷凝器冷却的混合物进行气液分离， 分 离后得到的气相反应产物输出到燃料分流装置， 得到的液相反应产物输 出给原料混合装置；
燃料分流装置， 根据太阳能资源和用户用能需要控制流向动力发电 设备与储气罐的太阳能燃料流量， 从而实现太阳能热化学互补发电系统 的调控；
储气罐， 在太阳能资源充足时， 将过量的太阳能燃料蓄存起来， 实 现化学蓄能； 在太阳能资源不足时， 储气罐中的太阳能燃料补充进入动 力发电设备， 实现系统输出调控；
动力发电设备， 以太阳能燃料作为燃料， 驱动发电机组发电并输出 电功。
为达到上述目的， 本发明还提供了一种中低温太阳能与化石燃料热 化学互补的发电方法， 应用于所述的系统， 该方法包括：
A、 原料混合装置将原料供应装置输入的化石燃料和气液分离器输 入的未反应物充分混合， 并输出给原料计量装置；
B、 原料计量装置将原料混合装置输入的原料按一定的速率输出给 预热器，预热器对接收的原料进行预热，然后输出给太阳能吸收反应器；
C、 太阳能吸收反应器利用吸收的太阳能热量供接收自预热器的原 料在自身的反应管中发生分解或重整反应， 反应产物进入冷凝器；
D、 冷凝器冷却来自太阳能吸收反应器的反应产物， 并将冷却后的 反应产物输出给气液分离器；
E、 气液分离器对接收自冷凝器冷却的反应产物进行气液分离， 分 离后得到的气相反应产物输出给燃料分流装置， 得到的液相反应产物输 出给原料混合装置；
F、 燃料分流装置控制一定量的太阳能燃料流向动力发电设备， 使 过量的太阳能燃料流向储气罐， 或使储气罐中的太阳能燃料补足流向动 力发电设备；
G、动力发电设备燃烧来自燃料分流装置的太阳能燃料， 输出电能， 排出的佘热通入原料预热器中预热原料。
(三） 有益效果
从上述技术方案可以看出， 本发明具有以下有益效果-
1、 在能量转换及利用方面， 经过吸热反应后的后甲醇、 乙醇及二 甲醚等的原料化学能转换为太阳能燃料的化学能， 同时驱动吸热反应进 行的太阳热能也转化为化学能储存到到反应产物中。 本发明提供的系统 在热力学第一定律层面的效果是增加了反应产物的能量， 增加的部分等 于太阳能燃料转化反应吸收的太阳热能； 在热力学第二定律层面上的效 果体现在太阳热能品位的提升， 通过甲醇、 乙醇及二甲醚等向太阳能燃 料转化的吸热反应， 使得低品位的太阳热能提升为高品位的燃料化学 能。 高品位太阳能燃料通过动力装置实现高效发电， 从而大幅提高了太 阳能净发电效率。
2、 利用本发明， 太阳能集热器采用抛物槽式聚光结构， 即单轴跟 踪的太阳能抛物槽聚光装置， 结构简单， 抛物槽内表面涂有对太阳光具 有高反射率、 低吸收率的选择性镀膜， 向太阳能吸收反应器中的原料重 整反应提供 150°C至 300°C温度范围的热量，与高温太阳能集热器相比， 制造和运行成本较低， 有利于大规模的推广和应用。
3、 利用本发明， 太阳能吸收反应器将太阳能吸收器与反应器设备 集成一体化， 置于太阳能聚光装置的焦轴上的一体化设备既是太阳能接 收器， 也是反应器， 聚集的高能流密度的太阳光直接照射在太阳能吸收 反应器上， 直接为吸热化学反应供热， 系统流程简单， 大大减少了采用 热介质带来的费用， 同时也避免了热介质储存、 传递产生的热损失。 通 过吸收 /反应器结构特征一体化不仅有利于减少散热损失，而且有利于分 解或重整反应的进行， 实现传热和反应的耦合， 获得良好的太阳能转换 效果。
4、 利用本发明， 当太阳能资源充足， 产生太阳能燃料量大于动力 发电机组燃料需求时， 过量的太阳能燃料进入储气罐， 实现化学蓄能； 当太阳能资源不足， 产生的太阳能燃料量不能满足动力发电机组的燃料 需求时， 储气罐中蓄存的太阳能燃料输出到动力发电机组， 补足所需的 燃料， 从而实现中低温太阳能与化石燃料热化学互补的发电系统运行的 调节， 突破了太阳能热发电系统输出不稳定的技术瓶颈； 由于太阳能资 源的不连续性， 中低温太阳能与化石燃料热化学互补的发电系统需周期 性启停， 系统启动时， 储气罐输出太阳能燃料供给动力发电设备启动， 产生烟气预热原料， 避免了用额外的能量启动系统。
5、 本发明对下列用户具有更大优势： 需要中小规模供电的工厂及 用户； 需要气体燃料而没有燃气接入条件的用户 （如城市周边， 天然气 管网覆盖不到的地区， 山区、 岛屿等地形条件不利于送气的地区）； 太 阳辐照资源良好 （我国的大部分地区， 尤其是西部地区；)。
附图说明 图 1为本发明提供的中低温太阳能与化石燃料热化学互补的发电系 统的结构示意图；
图 2为本发明提供的中低温太阳能与化石燃料热化学互补的发电方 法流程图；
图 3为依照本发明实施例提供的中低温太阳能与化石燃料热化学互 补的发电系统的示意图；
在图 1和图 3中， 1为原料罐， 2为原料混合装置， 3为原料计量装 置， 4为原料预热装置， 5为太阳能集热器， 6为太阳能吸收反应器， Ί 为冷凝器， 8为气液分离器， 9为燃料分流装置， 10为储气罐， 11为动 力发电设备。
具体实施方式 为使本发明的目的、 技术方案和优点更加清楚明白， 以下结合具体 实施例， 并参照附图， 对本发明进一步详细说明。
如图 1所示， 图 1为本发明提供的中低温太阳能与化石燃料热化学 互补的发电系统的结构示意图， 该系统包括原料供应装置 1、 原料混合 装置 2、 原料计量装置 3、 原料预热装置 4、 太阳能吸收反应器 5、 太阳 能集热器 6、 冷凝器 7、 气液分离器 8、 燃料分流装置 9、 储气罐 10、 动 力发电设备 11。
其中， 原料供应装置 1用于贮存化石燃料， 并将贮存的化石燃料输 出给原料混合装置 2。 所述原料供应装置为燃料罐， 其中贮存的化石燃 料为甲醇、 乙醇、 二甲醚等。
原料混合装置 2用于接收并混合来自原料供应装置 1中的化石燃料 和气液分离器 8中分离出来的未反应物， 并将得到的混合物输出给原料 计量装置 3。 所述原料混合装置为混合器， 用于将接收自原料罐中的化 石燃料与气液分离器中分离出来的未反应物进行混合。
原料计量装置 3用于控制单位时间内原料进入预热器 4的量， 根据 太阳能资源和用户端需求将接收自原料混合装置 2的原料按一定的速率 输出给原料预热装置 4。 所述原料计量装置为计量泵， 向原料预热装置 的换热器中泵入原料， 根据太阳能资源与用户需求调节输出原料流量。
原料预热装置 4利用动力发电设备 11 的排烟余热加热来自原料计 量装置 3的原料， 产生化石燃料蒸气输出给太阳能吸收反应器 5。 原料 预热装置包括一个换热器， 利用动力发电设备的排烟与原料换热， 产生 的化石燃料蒸气通入太阳能吸收反应器。
太阳能吸收反应器 5利用吸收的太阳能热量驱动接收自原料预热装 置 4的化石燃料蒸气在催化剂作用下发生分解或重整反应， 将太阳能转 化为富氢的燃料化学能， 产生太阳能燃料。 所述太阳能吸收反应器是化 学反应器， 其结构为管状， 材料为导热性能良好的钢、 铜、 铝等材料， 管子内填装铜系、 镍系或者铂钯系等固体金属系列催化剂， 管子外表面 涂有对太阳光具有高吸收率、 低反射率发射率的选择性镀膜， 管子外面 安装有高透射率的玻璃罩， 玻璃罩与管子之间为真空或者非真空。
太阳能集热器 6用于以线性聚焦方式将低能流密度的太阳能聚集成 高能流密度的中低温热能， 向太阳能吸收反应器 5中的化石燃料转换太 阳能燃料反应提供热量： 该太阳能集热器 6采用抛物槽式聚光结构， 太 阳能吸收反应器 5位于太阳能集热器的线性聚焦线上， 抛物槽内表面为 对太阳光具有高反射率、 低吸收率的选择性材料， 向太阳能吸收反应器 中的原料转换反应提供 150°C至 300°C的热能；
冷凝器 7用于冷却来自太阳能吸收反应器 5的反应产物， 并将冷却 后的反应产物输出给气液分离器 8。 所述冷凝器为间壁式换热设备， 采 用循环水进行冷却， 连接有循环冷却水。
气液分离器 8用于对接收自冷凝器 7冷却的混合物进行气液分离， 分离后得到的气相反应产物输出到燃料分流装置 9， 得到的液相反应产 物输出给原料混合装置 2。 所述气液分离器分离后得到的气相反应产物 为氢气、 一氧化碳等太阳能燃料和少量副产品， 液相反应产物为未反应 的原料、 水等。
燃料分流装置 9根据太阳能资源和用户用能需要控制流向动力发电 设备 11与储气罐 10的太阳能燃料流量， 从而实现太阳能热化学互补发 电系统的调控。 所述燃料分流装置为流量调节闽， 控制太阳能燃料流向 动力发电设备的流量， 使过量的太阳能燃料进入储气罐蓄存； 太阳能资 源不足时调控储气罐内的太阳能燃料补充进入动力发电设备， 以满足动 力发电设备的燃料需求。
储气罐 10在太阳能资源充足时， 将过量的太阳能燃料蓄存起来， 实现化学蓄能， 在太阳能资源不足时， 储气罐 10 中的太阳能燃料补充 进入动力发电设备 11 , 实现系统输出调控。 储气罐为耐压容器， 用于储 存来自分流装置的太阳能燃料， 实现蓄能， 并在太阳能资源不足时输出 太阳能燃料补足动力发电设备所需燃料。
动力发电设备 11， 以太阳能燃料作为燃料， 驱动发电机组发电并输 出电功。 所述动力发电设备为内燃机或微燃机发电机组， 燃烧太阳能燃 料发电并输出电能。
基于图 1所述的中低温太阳能与化石燃料热化学互补的发电系统的 结构示意图， 图 2示出了本发明提供的中低温太阳能与化石燃料热化学 互补的发电方法流程图， 该方法包括以下步骤：
歩骤 201 : 原料混合装置将原料供应装置输入的化石燃料和气液分 离器输入的未反应物充分混合， 并输出给原料计量装置；
步骤 202: 原料计量装置将原料混合装置输入的原料按一定的速率 输出给预热器， 预热器对接收的原料进行预热， 然后输出给太阳能吸收 反应器；
步骤 203 : 太阳能吸收反应器利用吸收的太阳能热量供接收自预热 器的原料在自身的反应管中发生分解或重整反应， 反应产物进入冷凝 器；
步骤 204: 冷凝器冷却来自太阳能吸收反应器的反应产物， 并将冷 却后的反应产物输出给气液分离器；
步骤 205: 气液分离器对接收自冷凝器冷却的反应产物进行气液分 离， 分离后得到的气相反应产物输出给燃料分流装置， 得到的液相反应 产物输出给原料混合装置；
步骤 206: 燃料分流装置控制一定量的太阳能燃料流向动力发电设 备， 使过量的太阳能燃料流向储气罐， 或使储气罐中的太阳能燃料补足 流向动力发电设备；
步骤 207: 动力发电设备燃烧来自燃料分流装置的太阳能燃料， 输 出电能， 排出的烟气通入原料预热器中预热原料。
步骤 201所述原料供应装置为燃料罐，其中贮存的化石燃料为甲醇、 乙醇等， 二甲醚等； 步骤 A中所述原料混合装置为混合器， 用于将接收 自原料罐中的化石燃料与气液分离器中分离出来的未反应物进行混合。
歩骤 202中所述原料计量装置为计量泵， 用于向原料预热装置的换 热器中泵入原料， 根据太阳能资源与用户需求调节输出原料流量。
步骤 203包括： 原料预热装置输出给太阳能吸收反应器的原料在经 过原料预热装置预热和太阳能吸收反应器蒸发后成为过热蒸气， 在常 压、 150至 300°C反应温度及铜系、 镍系或者铂钯系固体金属系列催化 剂作用下， 利用来自太阳能集热器收集的太阳能量发生分解或重整反 应， 气相反应产物为太阳能燃料氢气、 一氧化碳和少量副产品， 液相反 应产物为未反应的化石燃料和水， 该混合物从太阳能吸收反应器进入冷 凝器。
步骤 204中冷凝器为间壁式换热设备， 采用循环水进行冷却， 连接 有循环冷却水。
步骤 205中所述气相反应产物为氢气、 一氧化碳等太阳能燃料和少 量副产品， 液相反应产物为未反应的原料、 水等。
步骤 206中所述燃料分流装置为流量调节阀， 控制太阳能燃料流向 动力发电设备的流量， 使过量的太阳能燃料进入储气罐蓄存， 太阳能资 源不足时调控储气罐内的太阳能燃料补充进入动力发电设备， 以满足动 力发电设备的燃料需求； 所述储气罐为耐压容器， 装有安全阀、压力表， 用于储存来自分流装置的太阳能燃料， 实现蓄能， 并在太阳能资源不足 时输出太阳能燃料补足动力发电设备所需燃料。
步骤 207中所述动力发电设备为内燃机发电机组， 燃烧太阳能燃料 输出电能， 排出的余热通入原料预热器中预热原料。 动力发电设备还可 以采用微燃机发电机组。
基于图 1所述的中低温太阳能与化石燃料热化学互补的发电系统的 结构示意图， 以及图 2所示的中低温太阳能与化石燃料热化学互补的发 电方法流程图， 以下结合具体的实施例对本发明利用中低温太阳能与化 石燃料热化学互补的发电方法进一步详细说明。
实施例
本实施例利用中低温太阳能与甲醇互补， 制备 H2与 CO摩尔比约 2:1 的合成气作为太阳能燃料， 以内燃机发电机组作为动力发电设备实 现电能输出。 结合图 3， 图 3为依照本发明实施例提供的中低温太阳能 与甲醇热化学互补的发电系统的示意图。
原料供应装置 1中的甲醇与来自气液分离器 S的液相产物在原料混 合装置 2中充分混合， 通过管道 12后由原料计量装置 3以 5.57 1/min的 体积流量经管道 13输入原料预热装置 4， 在原料预热装置 4中与 450°C 的内燃机排烟产生热交换， 产生的甲醇蒸气经过管道 14进入太阳能吸 收反应器 5中。 太阳能集热器 6聚集的高能流密度的太阳能由吸收反应 器 5吸收并转化为热能， 以反应热的形式驱动甲醇在铜基催化剂的作用 下发生吸热的分解反应，产生 H2与 CO摩尔比 2: 1的合成气太阳能燃料。 合成气太阳能燃料通过管道 15，在冷凝器 7中的循环冷却水的作用下实 现冷却，冷却后的混合物经过管路 16，在气液分离器 8中实现气液分离。 分离出的液相反应产物为未反应甲醇和少量副产物， 液相反应产物经管 道 17回到原料混合装置 2中；气相反应产物主要是 H2与 CO摩尔比 2: 1 的合成气，合成气太阳能燃料通过管道 18，在燃料分流装置 9的作用下， 根据内燃机发电机组 11的燃料需求， 流向内燃机发电机组 11实现电能 输出， 或流向储气罐 10 实现化学能蓄存。 当太阳能资源不足时， 储气 罐 10中的合成气太阳能燃料经过管路 21与实时产生的合成气混合， 补 足内燃机发电机组 11的燃料需求，经过管路 22流向内燃机发电机组 11 燃烧作功发电。 内燃机发电机组 11排出的 450°C烟气通过管路 23通入 原料预热装置 4中预热甲醇原料， 通过管路 24排放到环境中。
以下的实施例可以说明本发明的效果：
采用聚光比为 82: 1的抛物槽式太阳能集热器，集热器开口宽度 5.76 米， 镜场面积 715m2， 镜场长度 124m; 原料为常温下 99.9%浓度的液体 工业甲醇，太阳能吸收反应器中填料为 Cu/ZnO/Al2O3固体金属系列催化 剂， 内燃机发电机组发电效率 42%， 排烟温度 450°C。
从分离器下端分离出来的液相产品， 主要是未反应的甲醇和少量液 体副产物， 冷凝分离器上端分离出来的气相产品主要是 H2和 CO。
在本实施例中，当太阳辐照为 600W/m2，原料甲醇进料量 5.57 1/min, 太阳能吸收反应器可产生 267 kg/hr的合成气太阳能燃料， 其中 43 kg/hr 的合成气太阳能燃料进入储气罐用于化学蓄能， 224 kg/hr的合成气太阳 能燃料输入到内燃机发电机组中燃烧作功， 内燃机发电机组向外输出 600kW 电功， 太阳能净发电效率达到 28%， 远超于太阳能单独发电 10-17%的水平。 当太阳辐照强度提高到 900 W/m2时， 太阳能吸收反应 器可产生 401 kg/hr的合成气太阳能燃料，此时流向储气罐的太阳能燃料 质量流量提高到 177kg/hr， 进入内燃机发电机组的太阳能燃料质量流量 仍为 224 kg/hr; 当太阳辐照强度降低至 300 W/m2时， 太阳能吸收反应 器可产生 134 kg/hr的合成气太阳能燃料，此时流向储气罐的太阳能燃料 质量流量为 0， 储气罐输出储存的合成气太阳能燃料， 输出的合成气质 量流量为 90 kg/hr, 从而进入内燃机发电机组的合成气太阳能燃料质量 流量仍为 224 kg/hr， 由此， 内燃机发电机组稳定工作在额定工况， 突破 了变辐照条件下动力发电设备性能急剧下降的技术瓶颈， 实现了变辐照 条件下中低温太阳能与化石燃料热化学互补的发电系统运行的调节。
本发明可以在多种场合得到应用， 尤其是实现偏远地区的小规模电 力供给， 为实现中低温太阳能与化石燃料热化学互补发电开辟了一条途 径。
以上所述的具体实施例， 对本发明的目的、 技术方案和有益效果进 行了进一步详细说明， 所应理解的是， 以上所述仅为本发明的具体实施 例而己， 并不用于限制本发明， 凡在本发明的精神和原则之内， 所做的 任何修改、 等同替换、 改进等， 均应包含在本发明的保护范围之内。

Claims

权利要求
1、 一种中低温太阳能与化石燃料热化学互补的发电系统， 其特征 在于， 该系统包括：
原料供应装置， 用于贮存化石燃料， 并将贮存的化石燃料输出给原 料混合装置；
原料混合装置， 用于接收并混合来自原料供应装置中的化石燃料和 来自气液分离器中分离出来的未反应物， 并将得到的混合物输出给原料 计量装置；
原料计量装置， 用于控制单位时间内原料进入原料预热装置的量， 根据太阳能资源和用户端需求将接收自原料混合装置的原料按一定的 速率输出给原料预热装置；
原料预热装置， 利用动力发电设备的余热加热接收自原料计量装置 的原料， 产生化石燃料蒸气输出给太阳能吸收反应器；
太阳能吸收反应器， 利用吸收的太阳能热量驱动接收自原料预热装 置的化石燃料蒸气在催化剂作用下进行分解或重整反应， 将太阳能转化 为富氢的燃料化学能， 产生太阳能燃料；
太阳能集热器， 用于以线性聚焦方式将低能流密度的太阳能聚集成 高能流密度的中低温热能， 为太阳能吸收反应器中的化石燃料转换太阳 能燃料反应提供热量；
冷凝器， 用于冷却接收自太阳能吸收反应器的反应产物， 并将冷却 后的反应产物输出给气液分离器；
气液分离器， 用于对接收自冷凝器冷却的混合物进行气液分离， 分 离后得到的气相反应产物输出到燃料分流装置， 得到的液相反应产物输 出给原料混合装置；
燃料分流装置， 根据太阳能资源和用户用能需要控制流向动力发电 设备与储气罐的太阳能燃料流量， 实现太阳能热化学互补发电系统的调 控；
储气罐， 在太阳能资源充足时， 将过量的太阳能燃料蓄存起来， 实 现化学蓄能； 在太阳能资源不足时， 储气罐中的太阳能燃料补充进入动 力发电设备， 实现系统输出调控；
动力发电设备， 以太阳能燃料作为燃料， 驱动发电机组发电并输出 电功。
2、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述原料供应装置为燃料罐， 其中贮存的化石 燃料为甲醇、 乙醇或二甲醚。
3、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述原料混合装置为混合器， 用于将接收自原 料罐中的化石燃料与气液分离器中分离出来的未反应物进行混合。
4、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述原料计量装置为计量泵， 用于向原料预热 装置的换热器中输入原料， 根据太阳能资源与用户需求调节输出原料流
5、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述原料预热装置包括换热器， 利用动力发电 设备的余热与原料换热， 产生的化石燃料蒸气通入太阳能吸收反应器。
6、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述太阳能吸收反应器是化学反应器， 其结构 为管状， 材料为钢、 铜或铝， 管子内填装铜系、 镍系或铂钯系固体金属 系列催化剂， 管子外表面涂有对太阳光具有高吸收率、 低反射率发射率 的选择性镀膜， 管子外面安装有高透射率的玻璃罩， 玻璃罩与管子之间 为真空或者非真空。
7、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述太阳能集热器采用抛物槽式聚光结构， 所 述太阳能吸收反应器位于所述太阳能集热器的线性聚焦线上， 抛物槽内 表面涂有对太阳光具有高反射率、 低吸收率的选择性镀膜， 向太阳能吸 收反应器中的原料分解或重整反应提供 150°C至 300°C温度范围的热
8、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述冷凝器为间壁式换热设备， 采用循环水进 行冷却， 连接有循环冷却水。
9、 根据权利要求 1 所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述气液分离器分离后得到气相反应产物和液 相反应产物， 其中气相反应产物为太阳能燃料氢气、 一氧化碳和少量副 产品， 液相反应产物为未反应的化石燃料和水。
10、 根据权利要求 1所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述燃料分流装置为流量调节阀， 控制太阳能 燃料流向动力发电设备的流量， 使过量的太阳能燃料进入储气罐蓄存， 太阳能资源不足时调控储气罐内的太阳能燃料补充进入动力发电设备， 以满足动力发电设备的燃料需求。
11、 根据权利要求 1所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述储气罐为耐压容器， 用于储存来自分流装 置的太阳能燃料， 实现蓄能， 并在太阳能资源不足时输出太阳能燃料补 足动力发电设备所需燃料。
12、 根据权利要求 1所述的中低温太阳能与化石燃料热化学互补的 发电系统， 其特征在于， 所述动力发电设备为内燃机机组或微燃机发电 机组， 燃烧太阳能燃料输出电能， 排出的余热通入原料预热器中预热原 料。
13、 一种中低温太阳能与化石燃料热化学互补的发电方法， 应用于 权利要求 1至 12中任一项所述的系统， 其特征在于， 该方法包括：
A、 原料混合装置将原料供应装置输入的化石燃料和气液分离器输 入的未反应物充分混合， 并输出给原料计量装置；
B、 原料计量装置将原料混合装置输入的原料按一定的速率输出给 预热器，预热器对接收的原料进行预热，然后输出给太阳能吸收反应器；
C、 太阳能吸收反应器利用吸收的太阳能热量供接收自预热器的原 料在自身的反应管中发生分解或重整反应， 反应产物进入冷凝器；
D、 冷凝器冷却来自太阳能吸收反应器的反应产物， 并将冷却后的 反应产物输出给气液分离器；
E、 气液分离器对接收自冷凝器冷却的反应产物进行气液分离， 分 离后得到的气相反应产物输出给燃料分流装置， 得到的液相反应产物输 出给原料混合装置；
F、 燃料分流装置控制一定量的太阳能燃料流向动力发电设备， 使 过量的太阳能燃料流向储气罐， 或使储气罐中的太阳能燃料补足流向动 力发电设备；
G、动力发电设备燃烧来自燃料分流装置的太阳能燃料， 输出电能， 排出的余热通入原料预热器中预热原料。
14、 根据权利要求 11 所述的中低温太阳能与化石燃料热化学互补 的发电方法， 其特征在于，
步骤 A所述原料供应装置为燃料罐， 其中贮存的化石燃料为甲醇、 乙醇或二甲醚；
步骤 A中所述原料混合装置为混合器，用于将接收自原料罐中的化 石燃料与气液分离器中分离出来的未反应物进行混合。
15、 根据权利要求 11 所述的中低温太阳能与化石燃料热化学互补 的发电方法， 其特征在于， 步骤 B中所述原料计量装置为计量泵， 用于 向原料预热装置的换热器中输入原料， 根据太阳能资源与用户需求调节 输出原料流量。
16、 根据权利要求 11 所述的中低温太阳能与化石燃料热化学互补 的发电方法， 其特征在于， 所述歩骤 C包括：
原料预热装置输出给太阳能吸收反应器的原料在经过原料预热装 置预热和太阳能吸收反应器蒸发后成为过热蒸气， 在 150至 300°C反应 温度及铜系、 镍系或者铂钯系固体金属系列催化剂作用下， 利用来自太 阳能集热器收集的太阳能量发生分解或重整反应， 气相反应产物为太阳 能燃料氢气、 一氧化碳和少量副产品， 液相反应产物为未反应的化石燃 料和水， 该混合物从太阳能吸收反应器进入冷凝器。
17、 根据权利要求 11 所述的中低温太阳能与化石燃料热化学互补 的发电方法， 其特征在于， 歩骤 D中冷凝器为间壁式换热设备， 采用循 环水进行冷却， 连接有循环冷却水。
18、 根据权利要求 11 所述的中低温太阳能与化石燃料热化学互补 的发电方法， 其特征在于，
步骤 F中所述燃料分流装置为流量调节阀， 控制太阳能燃料流向动 力发电设备的流量， 使过量的太阳能燃料进入储气罐蓄存， 太阳能资源 不足时调控储气罐内的太阳能燃料补充进入动力发电设备， 以满足动力 发电设备的燃料需求；
步骤 F中所述储气罐为耐压容器， 用于储存来自分流装置的太阳能 燃料， 实现蓄能， 并在太阳能资源不足时输出太阳能燃料补足动力发电 设备所需燃料。
19、 根据权利要求 11 所述的中低温太阳能与化石燃料热化学互补 的发电方法， 其特征在于， 步骤 G中所述动力发电设备为内燃机或微燃 机发电机组， 燃烧太阳能燃料输出电能， 排出的余热通入原料预热器中 预热原料。
PCT/CN2012/084522 2012-11-13 2012-11-13 中低温太阳能与化石燃料热化学互补的发电系统与方法 WO2014075219A1 (zh)

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