CN1830757A - Method and device for transforming solar energy into fuel chemical energy - Google Patents
Method and device for transforming solar energy into fuel chemical energy Download PDFInfo
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- CN1830757A CN1830757A CNA2005100544571A CN200510054457A CN1830757A CN 1830757 A CN1830757 A CN 1830757A CN A2005100544571 A CNA2005100544571 A CN A2005100544571A CN 200510054457 A CN200510054457 A CN 200510054457A CN 1830757 A CN1830757 A CN 1830757A
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- 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
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- 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
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Abstract
A method for converting the solar energy to the chemical energy of fuel features that the solar energy is used for the reaction of decomposing methol, bimether, etc into CO and H2. Its apparatus is composed of a light gathering solar heat collector for heating the thermal medium, a catalytic reactor containing solid catalyst connected to said solar heat collector for receiving heated thermal medium, a preheating evaporator connected to catalytic reactor and raw material tank, and a condensing separator connected with catalytic reactor and preheating evaporator for separating the resultant.
Description
Technical field
The present invention relates to a kind of is the method for fuel chemical energy with solar energy converting.
The invention still further relates to a kind of energy conversion device of realizing aforesaid method.At length, relate to a kind of disc type solar energy heat collector and substituted liquid fluid fuel and decompose the integrated of catalytic reaction device, the two has constituted solar heat chemical transformation device together with subsystem separately.Device of the present invention can be realized the complementation of sun power and conventional energy resources, device of the present invention specifically can realize comprising that the cascade utilization of fuel chemical energies such as methyl alcohol or dme and low-grade solar thermal energy promote to the grade of higher-grade fuel chemical energy, utilizes sun power to change liquid fuel into high heating value clean air synthol.
Background technology
The reserves of world oil have been difficult to bear ever-increasing consumers demand with production, and oil will be broken in the absolute status in international energy field.The rapid growth of oil consumption has a negative impact to the mankind's Sustainable development.Crude oil price rises steadily and is indicating the fact that " petroleum times " disappears, and has also strengthened the progressively demand of alternative oil of liquid cleaning synthols such as methyl alcohol, dme simultaneously.Methyl alcohol is as " the omnipotent intermediate " of chemical industry, can be synthetic from coal, Sweet natural gas, biomass equal energy source, be only except that synthetic ammonia can be by gasification and the simple chemical of the extensive synthetic of gas renormalizing.Methyl alcohol and dme are as important cleaning synthol, have the combustioncharacteristics of similar oil product and advantage easy to carry and transport, in the application that will obtain aspect the energy, the power more and more widely, carry out methyl alcohol and dimethyl ether fuel and efficiently utilize research imperative.Burning on the ordinary meaning is exactly to utilize boiler or cooking stove, and the direct oxidation thermopositive reaction-directly burning of methyl alcohol and oxygen takes place, and this is the main mode of utilizing of present methyl alcohol and dimethyl ether fuel.
Sun power is the most extensive on the earth, the direct energy, but owing to problems such as energy density are low and discontinuous, need convert thereof into the energy of other form usually when utilizing, and the conversion regime of at present widespread use is the photo-thermal conversion.The collection of sun power is general adopts various condensing apparatuss, from low temperature heat collectors such as flat, electron tubes types to the dish formula, high temperature heat collector such as tower, sun power is risen to higher grade be used.General heat-collecting temperature is high more, and corresponding cost is also high more.Solving the discontinuous problem of energy, can adopt the means of accumulation of heat, is a difficult problem but how to reduce the regenerative apparatus volume all the time, also has inevitable thermosteresis, and application is restricted.Therefore the approach of sun power and conventional energy resources integrated complementary use is subjected to paying close attention to biglyyer, at present general way is sun power and fuel (comprising electric power) having complementary functions on isolated footing separately, promptly when sun power does not reach temperature required or do not have the sun power available (cloudy day, night) by fuel feed, complementary system on this class simple physical meaning is in solar-heating, refrigeration, and is extensive use of in the solar heat power generation system.This complementary system only is the simple superposition of sun power and fossil oil, perhaps only is confined to the cascade utilization of physical energy, can not fundamentally improve the utilising efficiency of sun power.
Summary of the invention
The object of the present invention is to provide a kind of is the method for fuel chemical energy with solar energy converting.
Another purpose of the present invention is to provide a kind of energy conversion device that is used to realize aforesaid method.
For achieving the above object, provided by the invention a kind of be the method for fuel chemical energy with solar energy converting, be to be 180 ℃～300 ℃ middle low temperature solar thermal energy with solar energy converting, and absorb solar thermal energy with the round-robin thermal medium, fuel reaction heat supply for decomposing obtains degradation production; In this process, solar thermal energy is converted, is stored in the chemical energy of degradation production, further makes fuel and uses;
It is thermal oil more than 200 ℃ that described thermal medium is to use temperature.
Described fuel is methyl alcohol or dme liquid;
Described degradation production is with H
2With CO be the synthetic gas of main component.
Provided by the inventionly be used to realize that the transfer equipment of aforesaid method can be no regenerative apparatus, mainly comprise:
Focus solar collector is used to heat the thermal medium from the thermal medium storage tank;
Catalyticreactor is fixed bed heat exchange type reactor, in be filled with solid catalyst, this catalyticreactor is connected with solar energy collector, makes the thermal medium after being heated enter catalyticreactor;
Preheating evaporator is wall-type heat exchange equipment, connects catalyticreactor and head tank respectively, receives raw material from head tank in this heat exchange, and raw material is preheated, evaporates; Thermal source is the thermal medium from catalyticreactor;
Condensation separator is wall-type heat exchange equipment, connects catalyticreactor, separates the degradation production from catalyticreactor;
It is thermal oil more than 200 ℃ that described thermal medium is to use temperature;
By said apparatus, be sent to after solar energy collector is heated from the thermal medium of thermal medium storage tank, enter catalyticreactor, to solid catalyst bed and decomposition reaction heat supply, enter preheating evaporator then raw material is carried out heat supply, return the thermal medium storage tank afterwards and recycle; Raw material enters catalyticreactor again through preheating evaporator earlier and reacts, and reacted product enters condensation separator and isolates gas and liquid.
Energy conversion device provided by the invention can also be that regenerative apparatus is arranged, and comprising:
Focus solar collector is used to heat the thermal medium from the thermal medium storage tank;
Catalyticreactor is fixed bed heat exchange type reactor, in be filled with solid catalyst, this catalyticreactor is connected with solar energy collector, makes the thermal medium after being heated enter catalyticreactor;
Preheating evaporator is wall-type heat exchange equipment, connects catalyticreactor and head tank respectively, receives raw material from head tank in this heat exchange, and raw material is preheated, evaporates; Thermal source is the degradation production of discharging from catalyticreactor, is the backheat utilization;
Condensation separator is wall-type heat exchange equipment, connects preheating evaporator, separates the degradation production from preheating evaporator;
It is thermal oil more than 200 ℃ that described thermal medium is to use temperature;
By said apparatus, be sent to after solar energy collector is heated from the thermal medium of thermal medium storage tank, enter catalyticreactor, to solid catalyst bed and decomposition reaction heat supply, return the thermal medium storage tank afterwards and recycle; Raw material enters catalyticreactor again through preheating evaporator earlier and reacts, and reacted degradation production enters preheating evaporator as thermal source, enters condensation separator again and isolates gas and liquid.
Solar energy collector is the paraboloid of revolution heat collector of various single dishes or DVD multidisc form in the said apparatus.
Catalyticreactor is the shell and tube catalyticreactor of single tube or multitube in the said apparatus.
The isolated liquid product of condensation separator returns head tank and carries out circulating reaction in the said apparatus.
Condensation separator is connected with water coolant in the said apparatus.
Thermal medium circulates by the thermal medium pump in the said apparatus.
Head tank connects a feedstock pump in the said apparatus.
The present invention has following two aspect advantages:
1) energy transformation and utilize the aspect: the fuel chemical energy that decomposes back methyl alcohol, dme is converted to H
2With the fuel chemical energy of CO, solar thermal energy also is converted to H simultaneously
2Chemical energy with CO.Native system is the calorific value that has increased methyl alcohol, dimethyl ether fuel in the effect of first law of thermodynamics aspect, and the part of increase equals the solar thermal energy that decomposition reaction absorbs; Effect on second law of thermodynamics aspect is embodied in the lifting of solar thermal energy grade, and low-grade solar thermal energy is converted to high-grade H
2With the chemical energy of CO, increased the acting ability of solar thermal energy.Total effect is to reduce fuel chemical energy in the traditional combustion process to the heat energy switching process
Loss has improved efficiency of energy utilization.
2) following user had greater advantages: need geseous fuel and do not have user's (as surrounding city, the area that gas distributing system does not cover, topographical conditions such as mountain area, island are unfavorable for the area of supplying gas) of combustion gas access conditions; Solar irradiation resource good (most of area, the especially west area of China); Methyl alcohol, dimethyl ether fuel consumption possess certain scale (distributed energy station, methyl alcohol, dme heat supply or power, power generation system), are the user of feedstock production synthetic gas with methyl alcohol, dme.
Description of drawings
Fig. 1 decomposes substituted liquid fluid fuel reaction energy system schematic for sun power of the present invention.
Fig. 2 does not have the connection diagram of regenerative apparatus for the present invention.
Fig. 3 has the connection diagram of regenerative apparatus for the present invention.
Embodiment
The fundamental diagram of apparatus of the present invention sees also Fig. 1.The present invention utilizes 180 ℃～300 ℃ middle low-temperature solar energy to provide heat energy to material benzenemethanol or the reaction of dme thermal endothermic decomposition, and the production major ingredient is H
2With the synthetic gas of CO, middle low-temperature solar energy is changed into the chemical energy of synthetic gas.
In order more to be expressly understood the present invention, below to lift two examples and be described.
Example 1: sun power decomposes the substituted liquid fluid fuel does not have regenerative apparatus.Please in conjunction with Fig. 2, the present invention is made up of solar energy collector, catalyticreactor, heat medium circulation system and other utility appliance.
Thermal medium storage tank 5, the thermal medium that stores in it is the thermal oil of use temperature more than 200 ℃, send into by thermal medium pump 7 and pipeline 21 in the resorber 9 of solar energy collector 8, receive sun power, can control the flow of thermal medium by valve 10 from solar energy collector 8; Thermal medium is heated to 180 ℃～300 ℃, enter the shell side of catalyticreactor 3 in catalyticreactor 3 bottoms by pipeline 22, temperature of reaction in the catalyticreactor 3 is maintained 160-280 ℃, then enter the top of preheating evaporator 2 by pipeline 23, provide the vaporization heat of charging and liter to be warmed to 160-280 ℃ from the top of catalyticreactor 3.Thermal medium after release of heat, temperature reduce is got back to thermal medium storage tank 5 by the pipeline 24 of preheating evaporator 2 bottoms, finishes the circulation of thermal medium.
Material benzenemethanol in the head tank 1 or dme are pressed air speed 500-10000h through feedstock pump 6
-1Send into from preheating evaporator 2 bottoms by pipeline 14,15, after 160-280 ℃ of heating down, evaporation, enter catalyticreactor 3 from the top of preheating evaporator 2 by pipeline 16, under gauge pressure 0-6atm reaction pressure, 160-280 ℃ of temperature of reaction and catalyst action issue the reaction of separating estranged, produce to become to contain H
2, CO and unreacting material and byproduct mix products, this mix products enters the shell side middle part of condensation separator 4 by pipeline 17, is cooled to below 20 ℃ and separates, wherein major ingredient H
2With CO be well behaved gas synthol, discharge by pipeline 19 by condensation separator 4 upper ends, directly utilize or store by valve 11 control fed downstream.Unreacted raw material and small amount of liquid by product are separated from condensation separator 4 lower ends, return head tank 1 by pipeline 18, are mixed into preheating evaporator 2 circulating reactions with raw material in the jar.The water coolant of condensation separator 4 cools off by 25,26 pairs of condensation separators 4 of pipeline, and water coolant is by valve 12 controls.
Example 2: sun power decomposes the substituted liquid fluid fuel regenerative apparatus.In conjunction with Fig. 3, contrast Fig. 2 as can be known, the key distinction of example 2 and example 1 is 180 ℃～300 ℃ thermal medium from resorber 9, after entering catalyticreactor 3 release of heat by pipeline 22, directly return thermal medium storage tank 5 by pipeline 27, finish the circulation of thermal medium from catalyticreactor 3 tops.
Simultaneously enter the top of preheating evaporator 2 by pipeline 28, provide the vaporization heat of charging and liter to be warmed to 160-280 ℃ from the degradation production of catalyticreactor 3.Degradation production after release of heat, temperature reduce enters condensation separator 4 condensation separation by the pipeline 29 of preheating evaporator 2 bottoms.
The difference of two examples is: in embodiment 1, the pre-thermal evaporation of raw material provides heat by thermal medium (sun power), is called no backheat flow process; Reclaim 160-280 ℃ entrained heat of degradation production among the embodiment 2, use its preheating material, being called has the backheat flow process.
Need to prove that the various device in apparatus of the present invention is known technology, as:
The solar energy collector that the present invention adopts can be various paraboloid of revolution heat collectors, comprises single dish or DVD multidisc form.
Catalyticreactor of the present invention is a fixed bed heat exchange type reactor, can be the shell and tube catalyticreactor of single tube or multitube, and solid catalyst is seated in one section that manages between interior or pipe.
Preheating evaporator of the present invention can be various wall-type heat exchange equipment.
The catalyzer that the present invention adopts can be the known catalyzer that is used for methyl alcohol or dme building-up reactions, as solid metal oxide catalyst etc.
Condensation separator of the present invention can be a vertical sleeve formula interchanger.
Because the emphasis of discussion of the present invention is to change sun power the chemical energy of fuel product into by the solar heat chemical process, so the above-mentioned concrete equipment that belongs to known technology is not described in detail.
Following embodiment can illustrate effect of the present invention:
Adopt no backheat flow process, with the maximum heat outputting power multi-disc type solar energy heating device that is 5kW, thermal medium is for using the conduction oil of temperature more than 200 ℃, and raw material is the liquid industrial methanol of 99.9% concentration under the normal temperature and pressure, and catalyst is Cu/ZnO/Al2O
3The catalysis of series solid metal oxide Agent.
From the liquid-phase product that the lower end of condensation separator is separated, mainly be unreacted raw material and a small amount of liquid accessory substance, the gaseous products that separate the condensation separator upper end is the H more than 90%2With CO adds the synthesis gas that a small amount of flammable raw material forms.
In the present embodiment, as solar irradiation 780W/m2, 6 l/hs of methanol feeding amounts, i.e. solar energy thermal output 4.8kW, 260 ℃ of sun heat energy temperature, reaction volume air speed 1700h-1Under the condition, Methanol conversion reaches 60.5%, and hydrogen and carbon monoxide selective reach respectively 83.8% and 56.4%, Reaction system heat absorption 4.2kW, sun utilization efficiency of heat energy reaches 87.5%, and heat loss mainly comprises heat The heat radiation loss of medium transport process and reaction unit self.
Present embodiment is from the angle of energy grade, and advantage is more obvious. The concept of energy grade, for Its value of heat energy equals Carnot cycle efficient. Under above-mentioned reaction condition, 260 ℃ of sun heat energy are through first The alcohol decomposition reaction is converted to the chemical energy of catabolite mist, and energy grade is thus lifted to by 0.44 0.98, greatly increased its acting ability, can make simultaneously energy utilize system in the fuel link of burning Loss reduces 30.8% in the relatively directly burning process.
The present invention can be used for multiple use, such as heat supply, refrigeration, fuel-solar combined power generating, combustion gas Produce etc., utilize solar energy that synthesis gas fuel or the raw material of high-quality are provided for the user.
Claims (9)
1. one kind is the method for fuel chemical energy with solar energy converting, it is characterized in that:
With solar energy converting is 180 ℃～300 ℃ solar thermal energy, and absorbs solar thermal energy with the round-robin thermal medium, and the decomposition reaction heat supply for fuel obtains degradation production; In this process, solar thermal energy is converted, is stored in the chemical energy of degradation production, further makes fuel and uses;
It is thermal oil more than 200 ℃ that described thermal medium is to use temperature;
Described fuel is methyl alcohol or dme liquid;
Described degradation production is with H
2With CO be the synthetic gas of main component.
2. transfer equipment of realizing the described method of claim 1 mainly comprises:
Focus solar collector is used to heat the thermal medium from the thermal medium storage tank;
Catalyticreactor is fixed bed heat exchange type reactor, in be filled with solid catalyst, this catalyticreactor is connected with solar energy collector, makes the thermal medium after being heated enter catalyticreactor;
Preheating evaporator is wall-type heat exchange equipment, connects catalyticreactor and head tank respectively, receives raw material from head tank in this heat exchange, and raw material is preheated, evaporates; Thermal source is the thermal medium from catalyticreactor;
Condensation separator is wall-type heat exchange equipment, connects catalyticreactor, separates the degradation production from catalyticreactor;
It is thermal oil more than 200 ℃ that described thermal medium is to use temperature;
By said apparatus, be sent to after solar energy collector is heated from the thermal medium of thermal medium storage tank, enter catalyticreactor, to solid catalyst bed and decomposition reaction heat supply, enter preheating evaporator then raw material is carried out heat supply, return the thermal medium storage tank afterwards and recycle; Raw material enters catalyticreactor again through preheating evaporator earlier and reacts, and reacted product enters condensation separator and isolates gas and liquid.
3. transfer equipment of realizing the described method of claim 1 mainly comprises:
Focus solar collector is used to heat the thermal medium from the thermal medium storage tank;
Catalyticreactor is fixed bed heat exchange type reactor, in be filled with solid catalyst, this catalyticreactor is connected with solar energy collector, makes the thermal medium after being heated enter catalyticreactor;
Preheating evaporator is wall-type heat exchange equipment, connects catalyticreactor and head tank respectively, receives raw material from head tank in this heat exchange, and raw material is preheated, evaporates; Thermal source is the degradation production of discharging from catalyticreactor;
Condensation separator is wall-type heat exchange equipment, connects preheating evaporator, separates the degradation production from preheating evaporator;
It is thermal oil more than 200 ℃ that described thermal medium is to use temperature;
By said apparatus, be sent to after solar energy collector is heated from the thermal medium of thermal medium storage tank, enter catalyticreactor, to solid catalyst bed and decomposition reaction heat supply, return the thermal medium storage tank afterwards and recycle; Raw material enters catalyticreactor again through preheating evaporator earlier and reacts, and reacted degradation production enters preheating evaporator as thermal source, enters condensation separator again and isolates gas and liquid.
4. claim 2 or 3 device is characterized in that solar energy collector is the paraboloid of revolution heat collector of various single dishes or DVD multidisc form.
5. claim 2 or 3 device is characterized in that catalyticreactor is the shell and tube catalyticreactor of single tube or multitube.
6. claim 2 or 3 device is characterized in that the isolated liquid product of condensation separator returns head tank and carries out circulating reaction.
7. claim 2 or 3 device is characterized in that condensation separator is connected with water coolant.
8. claim 2 or 3 device is characterized in that thermal medium circulates by the thermal medium pump.
9. claim 2 or 3 device is characterized in that head tank connects a feedstock pump.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100544571A CN100376468C (en) | 2005-03-07 | 2005-03-07 | Method and device for transforming solar energy into fuel chemical energy |
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| CNB2005100544571A CN100376468C (en) | 2005-03-07 | 2005-03-07 | Method and device for transforming solar energy into fuel chemical energy |
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| CN1830757A true CN1830757A (en) | 2006-09-13 |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289164B (en) * | 2007-04-18 | 2010-09-15 | 中国科学院工程热物理研究所 | System and process for preparing hydrogen by solar energy middle-low temperature thermal driven thermal chemical reaction |
| CN102797650A (en) * | 2011-05-27 | 2012-11-28 | 中国科学院工程热物理研究所 | Low-CO2-emisison solar energy and methanol complementary thermodynamic cycle system and method |
| CN103189603A (en) * | 2010-10-04 | 2013-07-03 | 西门子公司 | Continuous flow steam generator having an integrated reheater |
| CN103194285A (en) * | 2012-01-05 | 2013-07-10 | 东莞市久能二甲醚应用技术专利有限公司 | Industrial combustion method of dimethyl ether used for replacing natural gas through conversion |
| CN103245087A (en) * | 2012-02-14 | 2013-08-14 | 中国科学院工程热物理研究所 | Indirect intermediate-temperature chemical energy storage device for solar heat on basis of chemical-looping combustion |
| CN103803491A (en) * | 2012-11-13 | 2014-05-21 | 中国科学院工程热物理研究所 | Mid-and-low temperature solar and fossil fuel thermo-chemical complementary power generation system and method |
| CN106374815A (en) * | 2016-09-20 | 2017-02-01 | 中国科学院工程热物理研究所 | Nano-catalyst-based solar photovoltaic-thermochemical composite apparatus and power generation system |
| CN107758614A (en) * | 2016-08-19 | 2018-03-06 | 江苏天超细金属粉末有限公司 | A kind of method and apparatus of solar energy Thermochemical Decomposition water hydrogen manufacturing |
| CN108036523A (en) * | 2017-11-28 | 2018-05-15 | 深圳信息职业技术学院 | A kind of miniature solar energy heat collector of preparing hydrogen by reforming methanol |
| CN108455528A (en) * | 2018-01-15 | 2018-08-28 | 清华大学 | A kind of methane is low-temperature catalyzed to reform the device and method for producing solar energy fuel |
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| DE3337078A1 (en) * | 1983-10-12 | 1985-05-02 | M.A.N. Maschinenfabrik Augsburg-Nürnberg AG, 8000 München | METHOD AND DEVICE FOR PRODUCING SYNTHESIS GAS |
| US4668494A (en) * | 1984-12-24 | 1987-05-26 | Foster Wheeler Energy Corporation | Method of using solar energy in a chemical synthesis process |
| JP2807053B2 (en) * | 1989-07-21 | 1998-09-30 | 三井化学株式会社 | Decomposition method of methanol |
| DE3933285A1 (en) * | 1989-10-05 | 1991-04-18 | Steinmueller Gmbh L & C | Continuous prodn. of synthesis gas - by reforming methane using carbon di:oxide as fuel gas |
| CN1034271C (en) * | 1993-10-18 | 1997-03-19 | 李宗英 | Processing method for preparing hydrogen with solar energy from bioplasm and water and its equipment |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101289164B (en) * | 2007-04-18 | 2010-09-15 | 中国科学院工程热物理研究所 | System and process for preparing hydrogen by solar energy middle-low temperature thermal driven thermal chemical reaction |
| CN103189603A (en) * | 2010-10-04 | 2013-07-03 | 西门子公司 | Continuous flow steam generator having an integrated reheater |
| CN102797650A (en) * | 2011-05-27 | 2012-11-28 | 中国科学院工程热物理研究所 | Low-CO2-emisison solar energy and methanol complementary thermodynamic cycle system and method |
| CN103194285A (en) * | 2012-01-05 | 2013-07-10 | 东莞市久能二甲醚应用技术专利有限公司 | Industrial combustion method of dimethyl ether used for replacing natural gas through conversion |
| CN103245087A (en) * | 2012-02-14 | 2013-08-14 | 中国科学院工程热物理研究所 | Indirect intermediate-temperature chemical energy storage device for solar heat on basis of chemical-looping combustion |
| CN103803491A (en) * | 2012-11-13 | 2014-05-21 | 中国科学院工程热物理研究所 | Mid-and-low temperature solar and fossil fuel thermo-chemical complementary power generation system and method |
| CN107758614A (en) * | 2016-08-19 | 2018-03-06 | 江苏天超细金属粉末有限公司 | A kind of method and apparatus of solar energy Thermochemical Decomposition water hydrogen manufacturing |
| CN107758614B (en) * | 2016-08-19 | 2020-12-25 | 江苏天一超细金属粉末有限公司 | Method and equipment for producing hydrogen by solar energy thermochemical decomposition of water |
| CN106374815A (en) * | 2016-09-20 | 2017-02-01 | 中国科学院工程热物理研究所 | Nano-catalyst-based solar photovoltaic-thermochemical composite apparatus and power generation system |
| CN106374815B (en) * | 2016-09-20 | 2019-05-17 | 中国科学院工程热物理研究所 | Photovoltaic based on nanocatalyst-heat chemistry set composite and electricity generation system |
| CN108036523A (en) * | 2017-11-28 | 2018-05-15 | 深圳信息职业技术学院 | A kind of miniature solar energy heat collector of preparing hydrogen by reforming methanol |
| CN108455528A (en) * | 2018-01-15 | 2018-08-28 | 清华大学 | A kind of methane is low-temperature catalyzed to reform the device and method for producing solar energy fuel |
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