CN116026057B - Thermochemical combined heat and power generation system based on composite solar reactor - Google Patents
Thermochemical combined heat and power generation system based on composite solar reactor Download PDFInfo
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Abstract
The present disclosure provides a thermochemical cogeneration system based on a composite solar reactor, comprising: the fuel pretreatment subsystem is used for preheating raw materials by utilizing the flue gas after the thermochemical reaction of the flue gas thermochemical regeneration subsystem; the solar thermal chemistry subsystem is used for absorbing solar energy by using the heat conduction oil, and the heat conduction oil after absorbing the solar energy heats the fuel working medium, so that the fuel working medium generates a first synthesis gas through a thermal chemistry reaction, the heat storage tank stores the high-temperature heat conduction oil, and the high-temperature heat conduction oil is released to heat the fuel working medium when solar radiation is insufficient; the flue gas thermochemical heat recovery subsystem is used for exchanging heat between flue gas generated after the cold and hot electric output subsystem performs power generation and a fuel working medium, so that the fuel working medium generates thermochemical reaction to generate second synthesis gas; the cold-heat electric output subsystem is used for generating electricity by utilizing combustion work of raw materials or synthetic gas, and the generated smoke provides cold and heat output for users. The system overcomes the defects of discontinuous and unstable solar energy and realizes the full recovery of the waste heat of the flue gas.
Description
Technical Field
The disclosure relates to the technical field of solar thermochemical utilization, in particular to a thermochemical combined heat and power generation system based on a composite solar reactor.
Background
The energy source is an important basis for the important progress of human civilization and the stable development of the economy and the society. Along with the rapid development of science and technology, the demands of various industries in society for energy are continuously increased, the environmental problems are increasingly prominent, and energy conservation and emission reduction and various renewable energy utilization technologies are increasingly emphasized.
At present, fossil energy such as petroleum, coal, natural gas and the like is still the main energy consumption. The long-term use of fossil energy and improper energy utilization mode cause a series of problems of low energy conversion rate, environmental pollution and the like, and the search for clean and renewable alternative energy sources has become a current problem to be solved urgently.
In recent years, solar energy has been widely focused on advantages such as wide distribution, green and clean, and abundant resources. Fully develop the solar energy utilization technology, and have important significance for solving the energy utilization problem, reducing the use of fossil fuel, reducing environmental pollution and promoting the social development. At present, solar energy is mainly utilized in a solar photovoltaic power generation and solar photo-thermal utilization mode to realize the utilization of solar energy resources. However, due to the day-night, season and space-time changes, the solar radiation generates larger fluctuation, and discontinuous and unstable conditions exist, so that the continuous and stable solar energy supply for users cannot be ensured. On the other hand, the solar energy utilization technology has high equipment cost and needs to be provided with a large-capacity energy storage device, so that the large-scale development and utilization of solar energy utilization are limited. Therefore, overcoming the unstable and discontinuous energy attribute of solar energy is the key to fully utilizing solar energy and meeting the future energy development demands.
Disclosure of Invention
In view of the above technical problems, the present disclosure provides a thermochemical combined heat and power generation system based on a composite solar reactor, which is used for at least partially solving the technical problems that the existing solar energy utilization technology cannot well overcome the instability and discontinuity of solar energy.
The utility model provides a thermochemical combined heat and power generation system based on compound solar reactor, including fuel pretreatment subsystem, solar thermal chemistry subsystem, flue gas thermochemical heat regeneration subsystem and cold heat electricity output subsystem, wherein: the fuel pretreatment subsystem is used for preheating raw materials to obtain a fuel working medium by utilizing medium-temperature flue gas after thermochemical reaction of the flue gas thermochemical regeneration subsystem, and conveying the fuel working medium to the solar thermal chemical subsystem and the flue gas thermochemical regeneration subsystem; the solar thermal chemical subsystem is used for absorbing solar energy by utilizing low-temperature heat conduction oil, and exchanging heat between the high-temperature heat conduction oil after heat absorption and a fuel working medium to enable the fuel working medium to generate a thermochemical reaction under the action of a catalyst to generate first synthetic gas, wherein a solar thermal chemical reactor of the solar thermal chemical subsystem adopts a composite parabolic trough type solar reactor with a heat storage interlayer; the flue gas thermochemical heat recovery subsystem is used for exchanging heat between the high-temperature flue gas output by the cold-heat electric output subsystem after power generation and the fuel working medium, so that the fuel working medium generates a thermochemical reaction to generate second synthesis gas; the cold-heat electric output subsystem is used for generating power by utilizing raw materials or first synthesis gas or second synthesis gas to burn, and inputting generated high-temperature flue gas into the flue gas thermochemical heat recovery subsystem to exchange heat with fuel working medium or utilizing the high-temperature flue gas to provide cold and heat output for users.
According to an embodiment of the present disclosure, a fuel pretreatment subsystem includes a fuel storage tank, a working fluid pump, a fuel preheater, a condenser, a separator, and a syngas storage tank, wherein: the fuel storage tank is used for storing raw materials; the working medium pump is used for conveying raw materials from the fuel storage tank to the fuel preheater so that the fuel preheater preheats the raw materials by utilizing medium-temperature flue gas conveyed by the flue gas thermochemical heat regeneration subsystem to obtain a fuel working medium; the condenser is used for condensing the first synthesis gas or the second synthesis gas; the separator is used for separating raw materials from the condensed first synthetic gas and the condensed second synthetic gas, inputting the separated raw materials into the fuel storage tank for storage, inputting the separated synthetic gas into the cold-hot electric output subsystem for combustion work, and inputting the redundant synthetic gas into the synthetic gas storage tank for storage.
According to an embodiment of the present disclosure, the fuel pretreatment subsystem further comprises a first valve, a second valve, and a third valve, wherein: the first valve is used for adjusting the proportion of the fuel working medium input into the solar thermal chemical subsystem and the flue gas thermochemical heat regeneration subsystem by the fuel preheater; the second valve is used for adjusting the proportion of the first synthesis gas input into the condenser by the solar thermal chemical subsystem and the second synthesis gas input into the condenser by the flue gas thermochemical heat recovery subsystem; the third valve is used for controlling the amount of raw materials input into the cold-hot electric output subsystem by the fuel storage tank.
According to an embodiment of the present disclosure, a solar thermal chemical subsystem includes a trough solar concentrating collector, a solar thermochemical reactor, a high temperature heat transfer oil pump, a low temperature heat transfer oil pump, a high temperature heat transfer oil thermal storage tank, a low temperature heat transfer oil thermal storage tank, wherein: the low-temperature heat conduction oil heat storage tank is used for storing low-temperature heat conduction oil; the low-temperature heat conduction oil pump is used for conveying the low-temperature heat conduction oil to the solar thermochemical reactor; the groove type solar concentrating collector is used for heating low-temperature heat conduction oil in the solar thermochemical reactor by utilizing focused solar energy, and exchanging heat between the high-temperature heat conduction oil after heat absorption and a fuel working medium to enable the fuel working medium to undergo thermochemical reaction under the action of a catalyst to generate first synthesis gas; the high-temperature heat conduction oil pump is used for conveying the high-temperature heat conduction oil subjected to heat exchange with the fuel working medium to the high-temperature heat conduction oil heat storage tank for storage, and conveying the high-temperature heat conduction oil to the solar thermochemical reactor to provide heat required by thermochemical reaction under the condition of insufficient solar radiation.
According to an embodiment of the present disclosure, the solar thermal chemical subsystem further comprises a fourth valve, a fifth valve, and a sixth valve, wherein: the fourth valve is arranged on a pipeline between the high-temperature heat conduction oil pump and the high-temperature heat conduction oil heat storage tank and is used for controlling the flow direction of the high-temperature heat conduction oil; the sixth valve is arranged between the low-temperature heat conduction oil pump and the low-temperature heat conduction oil heat storage tank and is used for controlling the flow direction of the low-temperature heat conduction oil; the fifth valve is arranged between the high-temperature heat conduction oil heat storage tank and the low-temperature heat conduction oil heat storage tank and is used for supplementing heat conduction oil when one of the high-temperature heat conduction oil heat storage tank and the low-temperature heat conduction oil heat storage tank is insufficient in heat conduction oil.
According to an embodiment of the present disclosure, a flue gas thermochemical regeneration subsystem comprises a primary flue gas thermochemical reactor, a secondary flue gas thermochemical reactor, a palladium membrane tube, a purge gas device, and a hydrogen storage tank, wherein: the first-stage flue gas thermochemical reactor is used for utilizing the heat exchange between the high-temperature flue gas output by the cold-hot electric output subsystem after power generation and the fuel working medium input by the fuel preheater to enable the fuel working medium to be heated to generate a thermochemical reaction to generate third synthetic gas; the palladium membrane tube is used for separating hydrogen in the third synthesis gas; the purge gas device is used for introducing the separated hydrogen into the hydrogen storage tank for storage; the secondary flue gas thermochemical reactor is used for generating second synthesis gas by continuously carrying out thermochemical reaction by using the third synthesis gas from which the hydrogen is separated.
According to an embodiment of the present disclosure, the flue gas thermochemical regeneration subsystem further comprises a seventh valve and an eighth valve, wherein: the eighth valve is used for adjusting the proportion of the high-temperature smoke which is input into the primary smoke thermochemical reactor by the cold-heat electric output subsystem and the high-temperature smoke which is used for providing cold-heat output for users; the seventh valve is used for adjusting the proportion of the medium-temperature flue gas input into the fuel preheater by the secondary flue gas thermochemical reactor and the medium-temperature flue gas used for providing cold and heat output for users.
According to an embodiment of the present disclosure, a cold and hot electrical output subsystem includes a gas turbine, an absorption chiller unit, and a flue gas heat exchanger, wherein: the gas turbine is used for generating power by using the combustion work of the synthesis gas input by the separator or the synthesis gas storage tank and the raw materials input by the fuel storage tank to generate high-temperature flue gas, and the high-temperature flue gas is input into the primary flue gas thermochemical reactor to exchange heat with the fuel working medium; the absorption refrigerating unit is used for refrigerating a user by utilizing high-temperature flue gas input by the gas turbine and/or medium-temperature flue gas input by the secondary flue gas thermochemical reactor; the flue gas heat exchanger is used for supplying heat for users by utilizing high-temperature flue gas input by the gas turbine and/or medium-temperature flue gas input by the secondary flue gas thermochemical reactor and/or flue gas after being utilized by the absorption refrigerating unit.
According to an embodiment of the present disclosure, the cold and hot electric output subsystem further comprises a ninth valve and a tenth valve, wherein: the ninth valve is used for adjusting the proportion of the synthesis gas input into the synthesis gas storage tank and the synthesis gas input into the gas turbine by the separator; the tenth valve is used for adjusting the proportion of the high-temperature flue gas and/or the medium-temperature flue gas input into the absorption refrigerating unit and the high-temperature flue gas and/or the medium-temperature flue gas input into the flue gas heat exchanger.
According to the embodiment of the disclosure, the composite parabolic trough type solar reactor with the heat storage interlayer is of a structure that a sleeve layer is arranged on the outer side of a metal pipe and is used for introducing heat conduction oil; and a disturbance structure is also arranged in the casing layer and used for disturbing the heat conduction oil introduced into the casing layer.
According to the thermochemical combined heat and power generation system based on the composite solar reactor, provided by the embodiment of the disclosure, the thermochemical combined heat and power generation system at least comprises the following beneficial effects:
the solar energy is converted into chemical energy through the solar thermal chemical subsystem, so that the cold and heat output subsystem is used for providing cold and heat output for users through combustion work, the solar heat collection technology and the thermochemical reaction of fuel are organically integrated, the solar energy is converted into chemical energy, the inherent characteristics of discontinuous and unstable solar energy are overcome, and the full utilization of the solar energy is realized.
Further, a solar thermochemical reactor of the solar thermal chemical subsystem adopts a composite parabolic trough type solar reactor with a heat storage interlayer, a layer of sleeve is arranged on the outer side of a metal pipe to form a double-layer sleeve structure, a disturbance structure is arranged between the double-layer sleeves, and heat conduction oil is introduced into the interlayer between the two pipes to provide a high-temperature heat source for thermochemical reaction of fuel; through the structure optimization mode, the temperature difference of the catalytic bed layer along the circumferential direction is reduced, the mixing effect of the heat conduction oil is further improved, the matching relation between the temperature distribution and the heat required by the reaction is improved, and the thermochemical reaction of the fuel working medium is fully generated under the action of the catalyst.
Furthermore, the heat-conducting oil heat storage tank is used for storing heat of high-temperature heat-conducting oil, and the heat-conducting oil is utilized under the condition of insufficient solar radiation intensity, so that continuous and stable performance of fuel thermochemical reaction when the solar radiation is insufficient is ensured.
Further, based on the energy utilization principle of 'temperature opposite port and cascade utilization', the full recovery of the waste heat of the flue gas is realized through the thermochemical reaction of the fuel before the high-temperature flue gas is directly used for refrigerating/heating, the heat exchange temperature difference between the high-temperature flue gas and the refrigerating/heating process is reduced, and the energy cascade utilization conversion process of the cold-heat poly-generation system is optimized.
Further, the flue gas thermochemical heat regeneration subsystem adopts a two-stage fuel thermochemical reactor, and adopts a palladium membrane tube with a separation function to separate and store hydrogen in the synthesis gas in a hydrogen storage tank, and the rest synthesis gas after separation is introduced into a next-stage fuel thermochemical reactor for reaction, so that the thermochemical reaction depth of the fuel can be improved, and the yield of the synthesis gas is increased.
And further, the solar energy and the flue gas waste heat are stored in the form of synthetic gas fuel through an integrated energy storage technology, and different energy storage and supply strategies are implemented according to the requirements of a user side, so that the energy grade of the solar energy and the flue gas waste heat is improved, the energy structure of the system is optimized, and the regulation and control flexibility of the system is improved, so that the requirements of the user are better met.
Drawings
The above and other objects, features and advantages of the present disclosure will become more apparent from the following description of embodiments thereof with reference to the accompanying drawings in which:
fig. 1 schematically illustrates a block diagram of a thermochemical cogeneration system based on a composite solar reactor provided by an embodiment of the disclosure.
FIG. 2 schematically illustrates a block diagram of various subsystems in a composite solar reactor-based thermochemical cogeneration system provided by embodiments of the disclosure.
Fig. 3A schematically illustrates a cross-sectional view of a solar reactor structure provided by an embodiment of the present disclosure.
Fig. 3B schematically illustrates a top view of a solar reactor structure provided by an embodiment of the present disclosure.
Fig. 3C schematically illustrates a position structure diagram of a perturbation structure in a solar reactor provided by embodiments of the present disclosure.
[ reference numerals ]
The system comprises an A-fuel pretreatment subsystem, a B-solar thermal chemical subsystem, a C-flue gas thermochemical heat regeneration subsystem and a D-cold-heat-electricity output subsystem;
1-fuel storage tank, 2-working medium pump, 3-fuel preheater, 4-condenser, 5-separator, 6-synthetic gas storage tank, 7-trough type solar concentrating collector, 8-solar thermochemical reactor, 9-high temperature heat conduction oil pump, 10-low temperature heat conduction oil pump, 11-high temperature heat conduction oil heat storage tank, 12-low temperature heat conduction oil heat storage tank, 13-first stage smoke thermochemical reactor, 14-second stage smoke thermochemical reactor, 15-palladium membrane tube, 16-purge gas device, 17-hydrogen storage tank, 18-gas turbine, 19-absorption refrigerator set, 20-smoke heat exchanger;
v1-first valve, V2-second valve, V3-third valve, V4-fourth valve, V5-fifth valve, V6-sixth valve, V7-seventh valve, V8-eighth valve, V9-ninth valve, V10-tenth valve;
s1-raw material, S2-fuel working medium, S3-low temperature heat conduction oil, S4-first synthesis gas, S5-high temperature flue gas, S6-second synthesis gas, S7-high temperature heat conduction oil, S8-separated synthesis gas, S9-third synthesis gas, S10-purge gas, S11-hydrogen, S12-medium temperature flue gas and S13-separated raw material.
Detailed Description
For the purposes of promoting an understanding of the principles and advantages of the disclosure, reference will now be made to the embodiments illustrated in the drawings and specific language will be used to describe the same. It will be apparent that the described embodiments are some, but not all, of the embodiments of the present disclosure. Based on the embodiments in this disclosure, all other embodiments that a person of ordinary skill in the art would obtain without making any inventive effort are within the scope of protection of this disclosure.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the disclosure. The terms "comprises," "comprising," and/or the like, as used herein, specify the presence of stated features, steps, operations, and/or components, but do not preclude the presence or addition of one or more other features, steps, operations, or components.
In the present disclosure, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; may be mechanically connected, may be electrically connected or may communicate with each other; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the terms in this disclosure will be understood by those of ordinary skill in the art as the case may be.
In the description of the present disclosure, it should be understood that the terms "longitudinal," "length," "circumferential," "front," "rear," "left," "right," "top," "bottom," "inner," "outer," and the like indicate an orientation or a positional relationship based on that shown in the drawings, merely to facilitate description of the present disclosure and to simplify the description, and do not indicate or imply that the subsystem or element being referred to must have a particular orientation, be configured and operated in a particular orientation, and thus should not be construed as limiting the present disclosure.
Like elements are denoted by like or similar reference numerals throughout the drawings. Conventional structures or constructions will be omitted when they may obscure the understanding of this disclosure. And the shape, size and position relation of each component in the figure do not reflect the actual size, proportion and actual position relation. In addition, in the claims, any reference signs placed between parentheses shall not be construed as limiting the claim.
Similarly, in the foregoing description of exemplary embodiments of the disclosure, various features of the disclosure are sometimes grouped together in a single embodiment, figure, or description thereof for the purpose of streamlining the disclosure and aiding in the understanding of one or more of the various disclosed aspects. The description of the reference to the terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present disclosure, the meaning of "a plurality" is at least two, such as two, three, etc., unless explicitly specified otherwise.
In carrying out the disclosed concept, the inventors found that: the solar heat collection technology is combined with the fuel thermochemical reaction, and the high-efficiency conversion and utilization of solar energy are realized by a mode that solar energy provides a high-temperature heat source for the fuel thermochemical reaction. In this way, on the one hand, the utilization of renewable energy sources can be realized, and the consumption of fossil fuels is reduced; on the other hand, the solar energy is converted into chemical energy in the fuel, so that the energy density of the solar energy is improved, the storage and conversion of the solar energy are realized, the problems of discontinuous and unstable solar energy are solved, the energy grade of the solar energy is effectively improved, and the method has a good development prospect. In view of this, embodiments of the present disclosure provide a thermochemical cogeneration system based on a composite solar reactor.
Fig. 1 schematically illustrates a block diagram of a thermochemical cogeneration system based on a composite solar reactor provided by an embodiment of the disclosure.
As shown in fig. 1, the thermochemical combined heat and power generation system based on the composite solar reactor comprises a fuel pretreatment subsystem A, a solar thermal chemical subsystem B, a flue gas thermochemical heat regeneration subsystem C and a cold-heat-power output subsystem D.
The fuel pretreatment subsystem A is used for preheating raw materials to obtain fuel working media by utilizing medium-temperature flue gas after thermochemical reaction of the flue gas thermochemical heat recovery subsystem C, and conveying the fuel working media to the solar thermal chemical subsystem B and the flue gas thermochemical heat recovery subsystem C.
The solar thermal chemical subsystem B is used for absorbing solar energy by utilizing low-temperature heat conduction oil, and exchanging heat between the high-temperature heat conduction oil after heat absorption and the fuel working medium to enable the fuel working medium to undergo thermal chemical reaction under the action of a catalyst to generate first synthesis gas. The solar thermochemical reactor 8 of the solar thermal chemical subsystem B adopts a compound parabolic trough solar reactor with a heat accumulating interlayer.
And the smoke thermochemical heat recovery subsystem C is used for exchanging heat between the high-temperature smoke output by the cold-heat-electricity output subsystem D after power generation and the fuel working medium, so that the fuel working medium generates thermochemical reaction to generate second synthesis gas.
The cold-heat electric output subsystem D is used for generating power by utilizing combustion work of raw materials or first synthetic gas or second synthetic gas, inputting generated high-temperature flue gas into the flue gas thermochemical heat regeneration subsystem C for thermochemical reaction of fuel working media to provide heat or utilizing the high-temperature flue gas for providing cold and heat output for users.
FIG. 2 schematically illustrates a block diagram of various subsystems in a composite solar reactor-based thermochemical cogeneration system provided by embodiments of the disclosure.
As shown in fig. 2, the fuel pretreatment subsystem a may include a fuel storage tank 1, a working fluid pump 2, a fuel preheater 3, a condenser 4, a separator 5, and a syngas storage tank 6.
A fuel tank 1 for storing a raw material S1.
And the working medium pump 2 is used for pumping the raw material S1 from the fuel storage tank 1 to the fuel preheater 3 so that the fuel preheater 3 preheats the raw material S1 by utilizing the medium-temperature flue gas S12 conveyed by the flue gas thermochemical heat recovery subsystem C to obtain the fuel working medium S2.
And the condenser 4 is used for condensing the first synthesis gas S4 generated by the solar thermal chemical subsystem B or the second synthesis gas S6 generated by the flue gas thermochemical heat recovery subsystem C.
And the separator 5 is used for separating raw materials from the condensed first synthesis gas S4 or second synthesis gas S6, inputting the separated raw materials S13 into the fuel storage tank 1 for storage, inputting the separated synthesis gas S8 into the cold-hot electric output subsystem D for combustion work, and inputting the redundant synthesis gas S8 into the synthesis gas storage tank 6 for storage.
Further, the fuel pre-treatment subsystem a also includes a first valve V1, a second valve V2, and a third valve V3. The first valve V1 is arranged on a pipeline between the fuel preheater 3 and the solar thermal chemical subsystem B and the flue gas thermochemical heat recovery subsystem C and is used for adjusting the proportion of the fuel preheater 3 to the fuel working medium S2 of the solar thermal chemical subsystem B and the flue gas thermochemical heat recovery subsystem C. The second valve V2 is arranged on a pipeline between the solar thermal chemical subsystem B and the flue gas thermochemical heat recovery subsystem C and the condenser 4 and is used for adjusting the proportion of the first synthesis gas S4 and the second synthesis gas S6 which are input into the condenser 4 by the solar thermal chemical subsystem B and the flue gas thermochemical heat recovery subsystem C. A third valve V3 is provided on the pipeline between the fuel tank 1 and the cold-hot electric output subsystem D for controlling the amount of raw material S1 input to the cold-hot electric output subsystem D.
The solar thermal chemical subsystem B may include a trough solar concentrating collector 7, a solar thermochemical reactor 8, a high temperature heat transfer oil pump 9, a low temperature heat transfer oil pump 10, a high temperature heat transfer oil thermal storage tank 11, and a low temperature heat transfer oil thermal storage tank 12.
The low-temperature conduction oil heat storage tank 12 is used for storing low-temperature conduction oil S3.
The low-temperature heat conduction oil pump 10 is used for sending the low-temperature heat conduction oil S3 to the solar thermochemical reactor 8.
The trough solar concentrating collector 7 is configured to heat the low-temperature heat conduction oil S3 in the solar thermochemical reactor 8 by using focused solar energy, and exchange heat between the high-temperature heat conduction oil S7 after heat absorption and the fuel working medium S2, so that the fuel working medium S2 undergoes a thermochemical reaction under the action of a catalyst to generate the first synthesis gas S4. Wherein, the catalyst can adopt Cu/Zn/Al 2 O 3 The catalysts, in particular, the disclosure is not limited.
The high-temperature heat conduction oil pump 9 is used for pumping the high-temperature heat conduction oil S7 subjected to heat exchange with the fuel working medium S2 to the high-temperature heat conduction oil heat storage tank 11 for storage, and conveying the high-temperature heat conduction oil S7 in the high-temperature heat conduction oil heat storage tank 11 to the solar thermochemical reactor 8 under the condition of insufficient solar radiation so as to provide heat required by thermochemical reaction.
Further, the solar thermal subsystem B further includes a fourth valve V4, a fifth valve V5, and a sixth valve V6, where the fourth valve V4 is disposed on a pipeline between the high-temperature heat conduction oil pump 9 and the high-temperature heat conduction oil heat storage tank 11, and is used to control the flow direction of the high-temperature heat conduction oil S7. The sixth valve V6 is disposed between the low-temperature heat conduction oil pump 10 and the low-temperature heat conduction oil heat storage tank 12, and is used for controlling the flow direction of the low-temperature heat conduction oil S3. The fifth valve V5 is disposed between the high-temperature heat-conducting oil heat-storage tank 11 and the low-temperature heat-conducting oil heat-storage tank 12, and is used for supplementing heat-conducting oil when one of the high-temperature heat-conducting oil heat-storage tank 11 and the low-temperature heat-conducting oil heat-storage tank 12 is insufficient.
The flue gas thermochemical heat recovery subsystem C can comprise a primary flue gas thermochemical reactor 13, a secondary flue gas thermochemical reactor 14, a palladium membrane tube 15, a purge gas device 16 and a hydrogen storage tank 17.
The primary flue gas thermochemical reactor 13 is used for utilizing the high-temperature flue gas S5 output after the cold-hot electricity output subsystem D performs work and power generation to exchange heat with the fuel working medium S2 input by the fuel preheater 3 so that the fuel working medium S2 is heated to perform thermochemical reaction to generate third synthetic gas S9.
A palladium membrane tube 15 for separating hydrogen S11 from the third synthesis gas S9;
purge gas device 16 for introducing separated hydrogen gas S11 into hydrogen storage tank 17 by purge gas S10.
A secondary flue gas thermochemical reactor 14 for generating a second synthesis gas S6 by continuing the thermochemical reaction of the third synthesis gas S9 after separation of the hydrogen S11.
Further, the flue gas thermochemical heat recovery subsystem C further comprises a seventh valve V7 and an eighth valve V8. The eighth valve V8 is disposed on a pipeline between the cold-hot electric output subsystem D and the primary flue gas thermochemical reactor 13, and is used for adjusting a ratio of the high-temperature flue gas S5 input into the primary flue gas thermochemical reactor 13 by the cold-hot electric output subsystem D to the high-temperature flue gas S5 used for providing cold and heat output for a user. The seventh valve V7 is arranged on a pipeline between the secondary flue gas thermochemical reactor 14 and the fuel preheater 3 and is used for adjusting the proportion of the medium-temperature flue gas S12 input into the fuel preheater 3 by the secondary flue gas thermochemical reactor 14 and the medium-temperature flue gas S12 for providing cold and heat output for a user.
The cold and hot electrical output subsystem D may include a gas turbine 18, an absorption chiller unit 19, and a flue gas heat exchanger 20. The gas turbine 18 is used for generating high-temperature flue gas S5 by utilizing combustion work of the synthesis gas S8 input by the separator 5 or the synthesis gas storage tank 6 or the raw material S1 input by the fuel storage tank 1, and inputting part of the high-temperature flue gas S5 into the primary flue gas thermochemical reactor 13 to exchange heat with fuel working media.
The absorption refrigeration unit 19 is used for refrigerating the user by utilizing the high-temperature flue gas S5 input by the gas turbine 18 and/or the medium-temperature flue gas S12 input by the secondary flue gas thermochemical reactor 14.
The flue gas heat exchanger 20 is used for supplying heat to a user by utilizing the high-temperature flue gas S5 input by the gas turbine 18 and/or the medium-temperature flue gas S12 input by the secondary flue gas thermochemical reactor 14 and/or the flue gas after being utilized by the absorption refrigerating unit 19.
Further, the cold-hot electric output subsystem D further includes a ninth valve V9 and a tenth valve V10. The ninth valve V9 is disposed on a pipeline between the separator 5 and the gas turbine 18, and three ports of the ninth valve V9 are respectively connected to the separator 5, the gas turbine 18 and the synthesis gas storage tank 6, and are used for adjusting a ratio of the synthesis gas S8 input into the synthesis gas storage tank 6 and the synthesis gas S8 input into the gas turbine 18 by the separator 5. The tenth valve V10 is arranged on an inlet pipeline of the absorption refrigerating unit 19, and four ports of the tenth valve V10 are respectively connected with the seventh valve V7, the eighth valve V8, the absorption refrigerating unit 19 and the flue gas heat exchanger 20, and is used for adjusting the proportion of the high-temperature flue gas S5 or the medium-temperature flue gas S12 input into the absorption refrigerating unit 19 and the high-temperature flue gas S5 or the medium-temperature flue gas S12 input into the flue gas heat exchanger 20.
On the basis of the embodiment, the solar thermochemical reactor 8 is a composite parabolic trough solar reactor with a heat storage interlayer, and a disturbance structure is further arranged in the sleeve layer and used for disturbing the heat conduction oil introduced into the sleeve layer.
Fig. 3A schematically illustrates a cross-sectional view of a solar reactor structure provided by an embodiment of the present disclosure, fig. 3B schematically illustrates a top view of a solar reactor structure provided by an embodiment of the present disclosure, and fig. 3C schematically illustrates a position structure diagram of a disturbance structure in a solar reactor provided by an embodiment of the present disclosure.
As shown in fig. 3A to 3C, the solar thermochemical reactor 8 has the structure: and a layer of sleeve is added to the outer side of the metal pipe to form a double-layer sleeve structure, namely a structure of the metal pipe 2-heat conduction oil-metal pipe 1-vacuum layer-glass pipe, a disturbance structure is arranged between the double-layer sleeves, and heat conduction oil is introduced into an interlayer between the two pipes to provide a high-temperature heat source for thermochemical reaction of fuel. Through the structure optimization mode, the temperature difference of the catalytic bed layer along the circumferential direction is reduced, the mixing effect of the heat conduction oil is further improved, and the matching relation between the temperature distribution and the heat required by the reaction is improved.
By way of example, a specific type of perturbation structure may be a helical fin, perturbing the conduction oil passing between the double-layer bushings by rotation of the helical fin. It should be understood that the type of the disturbing structure is not limited to helical fins, and can disturb the heat transfer oil introduced between the double-layer bushings, and the present disclosure is not limited thereto.
According to an embodiment of the present disclosure, the specific workflow of the thermochemical cogeneration system based on the composite solar reactor set forth above is:
the raw material S1 in the fuel storage tank 1 is conveyed into the fuel preheater 3 by the working medium pump 2 to exchange heat with the medium-temperature flue gas S12. The preheated fuel working substance S2 is sent into the solar thermal chemical reactor 8 and the primary flue gas thermal chemical reactor 13. The solar radiation energy with high heat flux density is obtained by focusing the groove type solar concentrating collector 7 to heat the heat conduction oil, and the heat conduction oil provides high-temperature reaction heat for the thermochemical reaction of the fuel in the solar thermochemical reactor 8 to generate the first synthesis gas S4. When the solar radiation is insufficient at night, the high-temperature conduction oil S7 in the high-temperature conduction oil heat storage tank 11 is introduced into the solar thermochemical reactor 8 by changing the flow direction of the conduction oil, and heat required by the fuel thermochemical reaction is provided, so that the continuous and stable performance of the fuel thermochemical reaction in the solar thermochemical reactor 8 is ensured.
The fuel working medium S2 fed into the first-stage flue gas thermochemical reactor 13 is driven by the waste heat of the high-temperature flue gas S5 of the gas turbine 18 to generate a third synthetic gas S9 through chemical reaction, hydrogen S11 in the third synthetic gas S9 is separated through a palladium membrane tube 15 and stored in a hydrogen storage tank 17, and the rest of the third synthetic gas S9 is fed into the next-stage fuel thermochemical reactor to continue to react, so that a second synthetic gas S6 is generated. The first synthesis gas S4 generated by the solar thermochemical reactor 8 and the second synthesis gas S6 generated by the flue gas thermochemical reactor are sent into the condenser 4 together for condensation, and the gas-liquid separation of the mixed fuel is realized under the action of the separator 5. The separated residual raw material S13 is sent into the fuel storage tank 1, the separated synthesis gas S8 is regulated and separated into two gas flows through a ninth valve V9, one gas flow can be directly fed into the gas turbine 18 for combustion work, after meeting the work requirement of the gas turbine 18, the other surplus synthesis gas flow is fed into the synthesis gas storage tank 6, so that the storage of the synthesis gas is realized, the synthesis gas in the storage tank can be fed into the gas turbine 18 for power generation or used as cold and hot supplementary fuel at the user side, the synthesis gas S8 in the synthesis gas storage tank 6 is firstly consumed according to the actual cold, hot and electric load requirements at the user side, and when the stored synthesis gas cannot meet the load requirements at the user side, the synthesis gas is continuously fed into the synthesis gas storage tank 6 for combustion work.
The absorption refrigeration unit 19 and the flue gas heat exchanger 20 can directly utilize the high-temperature flue gas S5 from the gas turbine 18 or utilize the medium-temperature flue gas S12 after the flue gas thermochemical reaction to provide refrigeration and heating for users. The ratio of the fuel thermochemical reaction and the refrigerating/heating flue gas can be changed by adjusting the seventh valve V7 and the eighth valve V8, so that the adjustment and the distribution of the cold and hot capacity output of a user are realized.
In summary, according to the thermochemical combined heat and power generation system based on the composite solar reactor provided by the embodiment of the disclosure, the solar heat collection technology and the thermochemical reaction of fuel are organically integrated, so that the full utilization of solar energy is realized, the solar energy is converted into chemical energy in the fuel, and the inherent characteristics of discontinuous and unstable solar energy are overcome; the composite parabolic trough type solar reactor with the heat storage interlayer is introduced, and a disturbance structure is arranged in the reactor, so that the mixing effect of heat conduction oil is improved, and the matching relation between the temperature distribution and the heat required by the reaction is improved; the high-temperature heat conduction oil is stored through the heat storage tank, and the high-temperature heat conduction oil in the heat storage tank is utilized to drive the fuel thermochemical reaction to be carried out when the solar radiation is insufficient. In addition, the low-grade flue gas waste heat is used for fuel thermochemical reaction, so that the flue gas waste heat is fully recovered, and the energy cascade high-efficiency conversion process of the combined cooling, heating and power system is further optimized.
While the foregoing embodiments have been described in some detail for purposes of clarity of understanding, it will be understood that the foregoing embodiments are merely illustrative of the invention and are not intended to limit the invention, and that any modifications, equivalents, improvements, etc. that fall within the spirit and principles of the present disclosure are intended to be included within the scope of the present disclosure.
Claims (7)
1. The thermochemical combined heat and power generation system based on the composite solar reactor is characterized by comprising a fuel pretreatment subsystem (A), a solar thermal chemical subsystem (B), a flue gas thermochemical heat regeneration subsystem (C) and a cold-heat-power output subsystem (D), wherein:
the fuel pretreatment subsystem (A) is used for preheating raw materials to obtain fuel working media by utilizing medium-temperature flue gas after thermochemical reaction of the flue gas thermochemical heat recovery subsystem (C), and conveying the fuel working media to the solar thermal chemical subsystem (B) and the flue gas thermochemical heat recovery subsystem (C); the fuel pretreatment subsystem (A) comprises a fuel storage tank (1), a working medium pump (2), a fuel preheater (3), a condenser (4), a separator (5) and a synthesis gas storage tank (6), wherein: -the fuel tank (1) is used for storing the raw material; the working medium pump (2) is used for conveying the raw materials from the fuel storage tank (1) to the fuel preheater (3) so that the fuel preheater (3) preheats the raw materials by utilizing medium-temperature flue gas conveyed by the flue gas thermochemical heat regeneration subsystem (C) to obtain a fuel working medium; the condenser (4) is used for condensing the first synthesis gas or the second synthesis gas; the separator (5) is used for separating raw materials from the condensed first synthesis gas or second synthesis gas, inputting the separated raw materials into the fuel storage tank (1) for storage, inputting the separated synthesis gas into the cold-hot electric output subsystem (D) for combustion work, and inputting the redundant synthesis gas into the synthesis gas storage tank (6) for storage;
the solar thermal chemical subsystem (B) is used for absorbing solar energy by utilizing low-temperature heat conduction oil, the fuel working medium exchanges heat with the high-temperature heat conduction oil after heat absorption, and the fuel working medium generates a thermochemical reaction to generate first synthesis gas under the action of a catalyst, wherein the solar thermal chemical subsystem (B) comprises a groove type solar concentrating collector (7), a solar thermochemical reactor (8), a high-temperature heat conduction oil pump (9), a low-temperature heat conduction oil pump (10), a high-temperature heat conduction oil heat storage tank (11) and a low-temperature heat conduction oil heat storage tank (12), wherein: the low-temperature heat conduction oil heat storage tank (12) is used for storing low-temperature heat conduction oil; the low-temperature heat conduction oil pump (10) is used for conveying the low-temperature heat conduction oil to the solar thermochemical reactor (8); the groove type solar concentrating collector (7) is used for heating low-temperature heat conduction oil in the solar thermochemical reactor (8) by utilizing focused solar energy, and heat exchange is carried out between the high-temperature heat conduction oil after heat absorption and the fuel working medium so that the fuel working medium is subjected to thermochemical reaction under the action of a catalyst to generate first synthesis gas; the high-temperature heat conduction oil pump (9) is used for conveying the high-temperature heat conduction oil subjected to heat exchange with the fuel working medium to the high-temperature heat conduction oil heat storage tank (11) for storage, and conveying the high-temperature heat conduction oil to the solar thermochemical reactor (8) to provide heat required by thermochemical reaction of the fuel working medium under the condition of insufficient solar radiation; the solar thermochemical reactor (8) adopts a composite parabolic trough type solar reactor with a heat storage interlayer, the composite parabolic trough type solar reactor with the heat storage interlayer is of a structure that a sleeve layer is arranged on the outer side of a metal pipe, and the sleeve layer is used for introducing heat conduction oil; a disturbance structure is further arranged in the casing layer and used for disturbing the heat conduction oil introduced into the casing layer;
the flue gas thermochemical heat recovery subsystem (C) is used for exchanging heat between the fuel working medium and high-temperature flue gas output after the cold-heat electric output subsystem (D) performs work generation so as to enable the fuel working medium to perform thermochemical reaction to generate second synthesis gas;
the cold-hot electric output subsystem (D) is used for generating power by utilizing combustion work of the raw materials or the first synthetic gas and the second synthetic gas, and inputting generated high-temperature flue gas into the flue gas thermochemical heat regeneration subsystem (C) to exchange heat with a fuel working medium or provide cold and heat output for a user by utilizing the high-temperature flue gas.
2. The composite solar reactor-based thermochemical cogeneration system of claim 1, wherein the fuel pretreatment subsystem (a) further comprises a first valve (V1), a second valve (V2), and a third valve (V3), wherein:
the first valve (V1) is used for adjusting the proportion of the fuel working medium input into the solar thermal chemical subsystem (B) and the flue gas thermochemical heat recovery subsystem (C) by the fuel preheater (3);
the second valve (V2) is used for adjusting the ratio of the first synthesis gas input to the condenser (4) by the solar thermal chemical subsystem (B) and the second synthesis gas input to the condenser (4) by the flue gas thermochemical regeneration subsystem (C);
the third valve (V3) is used for controlling the amount of the raw materials input into the cold-hot electric output subsystem (D) by the fuel storage tank (1).
3. The thermochemical cogeneration system based on a compound solar reactor of claim 1, wherein the solar thermal subsystem (B) further comprises a fourth valve (V4), a fifth valve (V5) and a sixth valve (V6), wherein:
the fourth valve (V4) is arranged on a pipeline between the high-temperature heat conduction oil pump (9) and the high-temperature heat conduction oil heat storage tank (11) and is used for controlling the flow direction of high-temperature heat conduction oil;
the sixth valve (V6) is arranged between the low-temperature heat conduction oil pump (10) and the low-temperature heat conduction oil heat storage tank (12) and is used for controlling the flow direction of the low-temperature heat conduction oil;
the fifth valve (V5) is arranged between the high-temperature heat conduction oil heat storage tank (11) and the low-temperature heat conduction oil heat storage tank (12) and is used for supplementing heat conduction oil when one of the high-temperature heat conduction oil heat storage tank (11) and the low-temperature heat conduction oil heat storage tank (12) is insufficient.
4. The composite solar reactor-based thermochemical cogeneration system of claim 1, wherein the flue gas thermochemical regenerator system (C) comprises a primary flue gas thermochemical reactor (13), a secondary flue gas thermochemical reactor (14), a palladium membrane tube (15), a purge gas device (16) and a hydrogen storage tank (17), wherein:
the primary flue gas thermochemical reactor (13) is used for utilizing the high-temperature flue gas output by the cold-heat-electricity output subsystem (D) after power generation and the fuel working medium input by the fuel preheater (3) to exchange heat so that the fuel working medium is heated to generate a thermochemical reaction to generate third synthetic gas;
the palladium membrane tube (15) is used for separating hydrogen in the third synthesis gas;
the purge gas device (16) is used for introducing the separated hydrogen into the hydrogen storage tank (17) for storage;
the secondary flue gas thermochemical reactor (14) is used for generating the second synthesis gas by continuously carrying out thermochemical reaction by using the third synthesis gas from which the hydrogen is separated.
5. The composite solar reactor-based thermochemical cogeneration system of claim 4, wherein the flue gas thermochemical regenerator system (C) further comprises a seventh valve (V7) and an eighth valve (V8), wherein:
the eighth valve (V8) is used for adjusting the ratio of the high-temperature flue gas input into the primary flue gas thermochemical reactor (13) by the cold-heat electric output subsystem (D) to the high-temperature flue gas used for providing cold and heat output for a user;
the seventh valve (V7) is used for adjusting the proportion of the medium-temperature flue gas input into the fuel preheater (3) by the secondary flue gas thermochemical reactor (14) and the medium-temperature flue gas used for providing cold and heat output for users.
6. The thermochemical combined heat and power generation system based on a composite solar reactor according to claim 4, wherein the cold heat and power output subsystem (D) comprises a gas turbine (18), an absorption refrigeration unit (19) and a flue gas heat exchanger (20), wherein:
the gas turbine (18) is used for generating electricity by utilizing combustion work of the synthesis gas input by the separator (5) or the synthesis gas storage tank (6) and the raw materials input by the fuel storage tank (1), and inputting the generated high-temperature flue gas into the primary flue gas thermochemical reactor (13) and the absorption refrigerating unit (19) and/or the flue gas heat exchanger (20);
the absorption refrigerating unit (19) is used for refrigerating a user by utilizing high-temperature flue gas input by the gas turbine (18) and/or medium-temperature flue gas input by the secondary flue gas thermochemical reactor (14);
the flue gas heat exchanger (20) is used for supplying heat for users by utilizing high-temperature flue gas input by the gas turbine (18) and/or medium-temperature flue gas input by the secondary flue gas thermochemical reactor (14) and/or flue gas after being utilized by the absorption refrigerating unit (19).
7. The composite solar reactor-based thermochemical cogeneration system of claim 6, wherein the cold-heat-power output subsystem (D) further comprises a ninth valve (V9) and a tenth valve (V10), wherein:
-the ninth valve (V9) is used to adjust the ratio of the synthesis gas fed to the synthesis gas tank (6) by the separator (5) and the synthesis gas fed to the gas turbine (18);
the tenth valve (V10) is used for adjusting the proportion of the high-temperature flue gas and/or the medium-temperature flue gas input into the absorption refrigerating unit (19) and the high-temperature flue gas and/or the medium-temperature flue gas input into the flue gas heat exchanger (20).
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