CN101888194B - Solar energy and methanol fuel chemical-looping combustion power generation system and method - Google Patents
Solar energy and methanol fuel chemical-looping combustion power generation system and method Download PDFInfo
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- CN101888194B CN101888194B CN 200910084034 CN200910084034A CN101888194B CN 101888194 B CN101888194 B CN 101888194B CN 200910084034 CN200910084034 CN 200910084034 CN 200910084034 A CN200910084034 A CN 200910084034A CN 101888194 B CN101888194 B CN 101888194B
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Abstract
The present invention relates to solar energy thermal-power-generating and energy technology field, especially a kind of burning chemistry chains electricity generation system and method that the solar energy of control CO2 discharge is complementary with methanol fuel. The system is the organic coupling of middle low-temperature solar energy thermochemical process and burning chemistry chains power cycle, comprising: solar energy heating-reduction reactor, solar energy heating-decomposition reactor, oxidation reactor, afterburning combustion chamber, combustion gas turbine, steam turbine, waste heat boiler, heat exchanger etc.. Using the present invention, the cascade utilization of different quality energy complementations is realized, can realize that zero energy consumption of CO2 separates by simple condensation, while fuel grade is reduced to the grade of FeO by the combustion system, to reduce combustion process
Loss, improves system
Efficiency; It is chemically reacted by solar heat, realizes the promotion of middle low-temperature solar energy grade; By afterburning, solve the problems, such as that burning chemistry chains dynamical system is low because of combustion gas turbine entrance initial temperature caused by recycled material limitation.
Description
Technical field
The present invention relates to solar energy thermal-power-generating and energy technology field, relate in particular to a kind of control CO
2The solar energy of discharging and burning chemistry chains electricity generation system and the method for methanol fuel complementation.
Background technology
CO
2As the main greenhouse gas that the mankind discharge in the atmosphere, major part derives from the burning of fossil fuels such as coal, oil, natural gas, and wherein 29% comes self power generation.At present, CO
2Reduction of discharging can be by readjusting the energy structure and improving that the energy transforms and utilization ratio realizes.
From the angle of readjusting the energy structure, regenerative resource especially solar energy is placed high hopes.Solar energy makes many developed countries all rise to regenerative resources such as solar energy from the original additional energy status of the strategy alternatives energy with generality, the spatter property of development and use and the advantages such as economy that appear gradually of its reserves " unlimitedness ", existence.Along with the proposition of China's construction resources conservation, friendly environment society's target, the paces of renewable energy utilizations such as solar energy are also obviously accelerated.
Current, the main developing direction of solar utilization technique is that solar photoelectric transforms and the solar energy thermal transition, and wherein the solar thermal power generating of photo-thermal conversion is again the most attractive heliotechnics of following twenty or thirty year.Yet because low, the time discontinuity of energy of solar energy density and the inequality of spatial distribution etc. have caused the solar energy storage difficulty, so for a comparatively long period of time, solar energy substitutes fossil fuel fully and still can't realize.In addition, solar energy to large-scale develop and utilize cost still very high, can't be equal to mutually with the fossil energy of routine economically.
The solar heat chemistry is to utilize solar thermal energy to drive endothermic chemical reaction, and reaction institute calorific requirement is provided, with the conversion of solar energy of disperseing be the energy density height, can store, fuel forms such as transportable synthesis gas or H2 are used.2003, Germany proposed solar energy reformation natural gas association circulating power generation system, and this electricity generation system can make solar energy net heat commentaries on classics effect rate reach 30%.Solar-natural gas-zinc oxide energy environment system has been studied in the energy research center by Switzerland country, its basic ideas are to utilize the high temperature solar thermal energy as thermal source, with gas renormalizing and these two the chemical process organic integration of zinc oxide reduction zinc, realize that simultaneously gas renormalizing is producing of synthesis gas and fuel zinc.Yet, current solar heat chemical reaction temperature concentrates on 900～1200 ℃ the transformation of energy of high temperature solar heat and utilization, need to adopt expensive solar-energy light collector, assemble and be higher than 900 ℃ high-grade solar energy, so that the heat energy of reaction needed to be provided, cause its cost too high, simultaneously the use of material is had higher requirement, be unfavorable for large-scale application.In addition, though the utilization of solar heat chemistry can reduce the use of fossil fuel, reduce CO
2Discharge capacity, but synthesis gas directly burning cause CO
2By N
2Dilution has increased CO
2Separating difficulty, consider CO
2Capture, system effectiveness can reduce significantly.
The energy transforms and the angle of utilization ratio from improving, because human in a short time is that the situation of main energy sources can not change with the fossil energy, especially China, coal is formed into energy-consuming from resource and constitutes and all account for absolute leading position, how to make energy resource system at separation of C O
2The time can also keep the energy resource system utilization ratio not reduce even improve, be control CO
2The main purpose of the energy resource system research of discharging.
Burning chemistry chains is a kind of combustion mode that is different from traditional fuel and the direct catalytic combustion of air, and it, carries out the traditional combustion reaction: reduction reaction, oxidation reaction as the media that transmits oxygen in two steps by metal oxide.Fuel at first is oxidized to steam and CO by metal oxide in reduction reactor
2, metal oxide is reduced to metal simple-substance or metal suboxide simultaneously.Metal simple-substance or metal suboxide after being reduced enter oxidation reactor, and a large amount of heat is emitted in oxidized regeneration, produce high-temperature flue gas.Because the not direct catalytic combustion of fuel and air has been avoided N
2To CO
2Dilution, CO in the reduction reactor tail gas
2The concentration height is not increasing special CO
2Under the separation equipment situation, can realize low energy consumption separation of C O
2, simultaneously because the fuel grade is lowered to the grade of the metal oxide after being reduced, makes and burn
Loss reduces, and has improved the efficient of system.
Burning chemistry chains can be at separation of C O because of it
2The time realize that the raising of system effectiveness causes the attention of many countries.A large amount of contributions have been done to the early stage research of burning chemistry chains by Japan.1994, Japanese scholar Ishida professor and Chinese scholar's golden red light professor took the lead in proposing control CO
2The new system of humid air turbine of the burning chemistry chains of discharging organically combines burning chemistry chains and thermodynamic cycle first in the world, and this is studied in nineteen ninety-five and obtains United States Patent (USP).Subsequently, states such as America and Europe begin to pay attention to the effect of chemical chain burning technology aspect the control greenhouse gas, and the FP5 of European Union framework, FP6 framework are subsidized burning chemistry chains as the important research content.Sweden Cha Ermusi University of Science and Technology has set up the burning chemistry chains circulating fluidized bed experimental bench of international first 10kW, Korea S has set up the demonstration power station of 50kW burning chemistry chains, intend setting up natural gas base 100kW burning chemistry chains power generating demonstration device on the largest scale at present in the BIGCO2 project of the Europe maximum that Norway research committee subsidizes, multinomial research about chemical chain has also been carried out in the subordinate of USDOE national energy technology experiment chamber.
But there is technical problem in burning chemistry chains: the performance of circulating granular is most important to the burning chemistry chains process, and the used carrier of oxygen of current burning chemistry chains mostly is Fe
2O
3, the NiO particle, for guaranteeing the stable of recycled material physical property, its oxidizing reaction temperature is strictly controlled, generally control below 1200 ℃, and current combustion gas turbine entrance initial temperature has reached more than 1400 ℃, and oxidizing reaction temperature can't mate with combustion gas turbine entrance initial temperature, has limited the raising of combustion gas turbine entrance initial temperature, thereby make the raising of system effectiveness be restricted, caused the bottleneck of burning chemistry chains power circulation system.
Summary of the invention
(1) technical problem that will solve
In view of this, the objective of the invention is to propose a kind of control CO
2The solar energy of discharging and burning chemistry chains electricity generation system and the method for methanol fuel complementation, solve the low problem of combustion gas turbine entrance initial temperature that the burning chemistry chains dynamical system causes because of the recycled material restriction, the efficient heat generating of low-temperature solar energy utilizes in realizing simultaneously, reduces CO
2The capture energy consumption.
(2) technical scheme
In order to achieve the above object, the invention provides a kind of control CO
2The solar energy of discharging and the burning chemistry chains round-robin method of methanol fuel complementation, this method comprises:
Methanol fuel reduces Fe under the driving of middle low-temperature solar energy
2O
3Circulating granular, middle low-temperature solar energy is converted into chemical energy to be stored among the reduction product Fe O, FeO continues oxidation by air regeneration, emit big calorimetric and produce high-temperature flue gas, the middle low-temperature solar energy that is stored in simultaneously among the FeO discharges with the form of high temperature heat, and the grade of low-temperature solar energy promotes in the realization; Low-temperature solar energy refers to the solar energy of temperature range between 150 ℃ to 300 ℃ in described;
In the such scheme, this method further comprises: methanol fuel is at reduction Fe
2O
3In the time of circulating granular, under middle low-temperature solar energy drives, be broken down into and comprise H
2Synthesis gas with CO, middle low-temperature solar energy is converted into the chemical energy of synthesis gas, the high-temperature flue gas generation combustion reaction that synthesis gas and circulating granular regenerative process produce, drive the combustion gas turbine acting with further raising flue-gas temperature, the middle low-temperature solar energy that is stored in simultaneously in the synthesis gas discharges with the form of high temperature heat, and the low-temperature solar energy grade is to the lifting of high temperature heat grade in finishing.
In order to achieve the above object, the invention provides a kind of control CO
2The solar energy of discharging and the burning chemistry chains electricity generation system of methanol fuel complementation, this system is made of the chemical chain combustion apparatus of middle low-temperature solar energy driving and the combustion-compensating device of middle low-temperature solar energy driving, wherein:
The chemical chain combustion apparatus that middle low-temperature solar energy drives comprises solar energy heating-reduction reactor 2, oxidation reactor 6, gas- solid heat exchanger 3,5,12,13, shunt 19, cyclone separator 7, preheater 1 and pump 9, wherein:
Solar energy heating-reduction reactor 2 utilizes solar collector, and the solar energy collecting that will hang down energy-flux density in the line focus mode becomes the middle low temperature heat energy of high fluence density, is received from methyl alcohol and the circulating granular Fe of solar energy preheater 1 in order to driving
2O
3Reduction reaction;
Gas- solid heat exchanger 3,5,12,13, heat transmission equipment is used for the exchange heat between the hot and cold logistics of realization;
Cyclone separator 7 is used for gas-solid mixture is carried out gas solid separation;
The combustion-compensating device that middle low-temperature solar energy drives comprises solar energy heating-decomposition reactor 11, afterburning combustion chamber 8, combustion gas turbine 14, waste heat boiler 15, steam turbine 16, condenser 17, preheater 10, pump 18 and compressor 4, wherein:
Solar energy heating-decomposition reactor 11 utilizes solar collector, and the solar energy collecting that will hang down energy-flux density in the line focus mode becomes the middle low temperature heat energy of high fluence density, is received from the methanol decomposition reaction of solar energy preheater 10 in order to driving;
Flue-gas temperature for the synthesis gas after the Methanol Decomposition and the flue gas generation combustion reaction that is received from cyclone separator, is further improved in afterburning combustion chamber 8;
In the such scheme, middle low-temperature solar energy and methanol fuel are according to different complementation, the comprehensive cascade utilizations of carrying out of grade.
In the such scheme, the burning chemistry chains mode that low-temperature solar energy drove during described methanol fuel adopted, the methanol steam after the preheating enters solar energy heating-reduction reactor, under middle low-temperature solar energy drives with circulating granular Fe
2O
3Reduction reaction takes place, and produces solid particle FeO and gaseous state product water steam and CO
2, FeO emits a large amount of heat through compressed air oxidation regeneration in oxidation reactor after the preheating, generates high temperature Fe
2O
3And flue gas, after gas solid separation, high-temperature flue gas enters afterburning combustion chamber, Fe
2O
3Particle enters reduction reactor recirculation behind the heat exchanger recovery waste heat.
In the such scheme, after the preheating of described methanol fuel part, enter solar energy heating-decomposition reactor, under the driving of middle low temperature solar thermal energy, decomposition reaction takes place, produce synthesis gas, act as a fuel after synthesis gas is preheated and enter the afterburning combustion chamber, with the high-temperature flue gas that is received from cyclone separator, combustion reaction takes place, emit a large amount of heat, further improve combustion gas turbine entrance initial temperature, solved because guaranteeing the stability of recycled material physical property, oxidizing reaction temperature is restricted, and causes the low problem of combustion gas turbine entrance initial temperature.
In the such scheme, described solar collector adopts parabolic slot type concentration structure, simple in structure, the solar energy collecting that will hang down energy-flux density in the line focus mode becomes the middle low temperature heat energy of high fluence density, compare with high-temp solar heat collector, its optically focused is than low, and manufacturing and operating cost reduce greatly, are conducive to large-scale promotion and application.
In the such scheme, low-temperature solar energy during this system rationally utilizes is in order to drive methyl alcohol-Fe
2O
3Reduction reaction and methanol decomposition reaction, low-temperature solar energy changes to the chemical energy of FeO and synthesis gas in the realization, and be stored in middle low-temperature solar energy in FeO and the synthesis gas with the chemical energy form, by oxidation reaction and afterburning, form with high temperature heat is emitted, the grade of low-temperature solar energy is to the lifting of high temperature heat grade in finishing, and compares the exothermic heat of reaction amount with direct burning and increase to some extent, increases the amount that part is reaction absorption solar energy.
In the such scheme, low-temperature solar energy during this system utilizes, the use amount of reduction fuel reduces CO
2Discharging, simultaneously owing to adopt burning chemistry chains, the burning of fuel is divided into reduction reaction and two steps of oxidation reaction are carried out the CO that reaction produces
2Not by N
2Dilution, CO
2The concentration height can be removed steam through simple condensation, isolates CO
2, this process does not need special CO
2Separator and extra energy consumption realize CO
2Zero energy consumption separate, have very high economy and environmental benefit.
In the such scheme, under the more weak situation of no solar energy or solar irradiation intensity, reduction reaction institute calorific requirement in this system is provided by the sensible heat that circulating granular carries, and decomposition reactor and methyl alcohol preheating institute calorific requirement are provided by fume afterheat according to each process institute energy requirement taste difference.
In the such scheme, under the more weak situation of no solar energy or solar irradiation intensity, utilize fume afterheat that methyl alcohol preheating and the required reaction heat of decomposition reaction are provided, utilize high temperature Fe
2O
3Sensible heat provide the reduction reaction process required reaction heat, guarantee the continuous operation of system under the more weak condition of no solar energy or solar irradiation intensity.
(3) beneficial effect
From technique scheme as can be seen, the invention has the beneficial effects as follows:
1, the complementation of low-temperature solar energy and methanol fuel in the emphasis, the cascade utilization of realization energy grade;
2, system has overcome the burning chemistry chains dynamical system because of the low problem of combustion gas turbine entrance initial temperature that the recycled material restriction causes by adopting the afterburning mode, has improved combustion gas turbine entrance initial temperature;
3, solar collector adopts parabolic slot type concentration structure, simple in structure, provide 150 ℃ to the heat of 300 ℃ of temperature ranges to raw material preheating, reduction reaction and decomposition reaction, compare with high-temp solar heat collector, manufacturing and operating cost are lower, are conducive to large-scale promotion and application; In addition, this solar collector is the temperature and the needed temperature coupling of reaction of heat energy with conversion of solar energy, has realized the reasonable utilization of middle low-temperature solar energy;
4, in reduction reaction and decomposition reaction process, fuel chemical energy transforms the chemical energy of FeO and synthesis gas, and middle low temperature solar thermal energy also is converted into chemical energy and is stored in FeO and the synthesis gas.From the first law of thermodynamics, native system has increased the energy of product, and the part of increase equals to react the solar thermal energy of absorption; From the second law of thermodynamics, by reduction reaction and decomposition reaction, low-grade solar thermal energy promotes and is high-grade fuel chemical energy;
5, because the present invention adopts solar energy to import the energy as part, reduce the use of fuel, reduced CO
2Discharge capacity, simultaneously reduction reaction produces steam and CO
2, CO
2Can separate by the simple physics condensation method, not need extra power consumption, also not need special CO
2Separator is from producing CO
2The source solved CO
2Control problem, greatly reduce CO
2Separation and capture cost.
Description of drawings
Fig. 1 is control CO provided by the invention
2First embodiment of the solar energy of discharging and the burning chemistry chains dynamical system of methanol fuel complementation;
Fig. 2 is the control CO under no solar energy or the more weak situation of solar irradiation intensity provided by the invention
2Second embodiment of the solar energy of discharging and the burning chemistry chains dynamical system of methanol fuel complementation.
Embodiment
The invention provides two kinds of specific embodiments, the idiographic flow of embodiment 1 is control CO provided by the invention as shown in Figure 1
2The solar energy of discharging and the burning chemistry chains dynamical system of methanol fuel complementation; The idiographic flow of embodiment 2 is the control CO under no solar energy or the more weak situation of solar irradiation intensity provided by the invention as shown in Figure 2
2The solar energy of discharging and the burning chemistry chains dynamical system of methanol fuel complementation.Below these two kinds of embodiment are elaborated.
Embodiment 1:
The present embodiment system is by preheater 1,10, pump 9,18, gas- solid heat exchanger 3,5,12,13, shunt 19, solar energy heating-reduction reactor 2, solar energy heating-decomposition reactor 11, oxidation reactor 6, compressor 4, cyclone separator 7, afterburning combustion chamber 8, combustion gas turbine 14, waste heat boiler 15, steam turbine 16, condenser 17 is formed.Its idiographic flow is:
One methyl alcohol S3 after the middle low temperature solar thermal energy preheating of being assembled by solar collector, enters solar energy heating-decomposition reactor 11 through pump 9 pressurizations in preheater 10 in addition.Part takes place and decomposes in methyl alcohol in decomposition reactor, produce synthesis gas S21, and decomposition reaction institute calorific requirement is provided by the middle low-temperature solar energy that solar collector provides.Synthesis gas S21 enters afterburning combustion chamber 8 after 13 preheatings of gas-solid heat exchanger, and therein with high-temperature flue gas S16 in unreacting oxygen generation combustion reaction, emit a large amount of reaction heat, further improve flue-gas temperature.High-temperature flue gas S18 behind the afterburning enters gas turbine 14 expansion actings, through waste heat boiler 15 recovery waste heats, after the acting of generation steam, enters in the environment.
Embodiment 2:
The present embodiment system is by preheater 1,9, pump 8,17, gas-solid heat exchanger 4,11,12, shunt 18, reduction reactor 2, decomposition reactor 10, oxidation reactor 5, compressor 3, cyclone separator 6, afterburning combustion chamber 7, combustion gas turbine 13, waste heat boiler 14, steam turbine 15, condenser 16 is formed.Its idiographic flow is:
Methyl alcohol S1 splits into two gangs of S2, S3 through shunt 18 and enters system, and wherein methyl alcohol S2 enters reduction reactor 2 after preheater 1 preheating, and the preheating thermal source is fume afterheat.In reduction reactor, methyl alcohol and Fe
2O
3Reduction reaction takes place in circulating granular S7.After the reaction, methyl alcohol is oxidized to gaseous products CO
2With steam S6, Fe
2O
3Be reduced to FeO solid particle S5, react required reaction heat by circulating granular Fe
2O
3Self entrained sensible heat provides.The metal oxide S5 that is reduced by the partial fume preheating of discharging from gas turbine 13, enters oxidation reactor 5 then in gas-solid heat exchanger 11.After the compressed machine 3 of air S8 is compressed to certain pressure, reclaim the circulating granular waste heat in gas-solid heat exchanger 4, the compressed air S10 after being preheated enters oxidation reactor 5.Through pressurization, air S10 after the preheating in oxidation reactor 5 with preheating after FeO particle S12 oxidation reaction takes place, emit a large amount of heat, the oxidized regeneration of circulating granular produces high-temperature flue gas simultaneously.High Temperature Gas solid mixture S13 carries out gas solid separation in cyclone separator 6, gas S14 enters afterburning combustion chamber 7 after discharging from cyclone separator 6 tops, and solid particle S15 is discharged by the bottom.High-temperature solid particle S15 is through gas-solid heat exchanger 12 pre-hot synthesis gas, and gas-solid heat exchanger 4 preheated airs enter reduction reactor 2 and carry out recirculation behind the recovery waste heat.
One methyl alcohol S3 is through pump 8 pressurization in addition, in preheater 9 by smoke pre-heating after, enter decomposition reactor 10.Part takes place and decomposes in methyl alcohol in decomposition reactor, produce synthesis gas S19, and the flue gas of decomposition reaction institute calorific requirement after by preheating FeO solid particle S5 provides.Synthesis gas S19 enters afterburning combustion chamber 7 after 12 preheatings of gas-solid heat exchanger, and therein with high-temperature flue gas S14 in unreacting oxygen generation combustion reaction, emit a large amount of reaction heat, further improve flue-gas temperature.High-temperature flue gas S16 behind the afterburning enters combustion gas turbine 13 expansion actings, through waste heat boiler 14 recovery waste heats, after the acting of generation steam, enters in the environment.
More than each embodiment all adopt ASPEN PLUS software to carry out analog computation, basic parameter and balance condition state parameter and thermodynamic performance see Table 1 to table 5, and adopting under the basic loop parameter condition (seeing Table 1) of embodiment, carried out the comparison of thermal performance aspect in order to ISCC system that end circulating and evaporating section heat is provided and traditional combined cycle system respectively with by high temperature solar thermal energy in assembling.
The circulatory system for embodiment 1, when the methyl alcohol molar flow is 1_mol/s, solar collector is assembled 250 ℃ of solar thermal energy temperature, reduction reaction temperature and decomposition reaction temperature are 200 ℃, 1000 ℃ of oxidizing reaction temperatures, during 1400 ℃/18bar of combustion gas turbine inlet condition, the clean output work of circulation is 447_kW.Because this circulatory system input energy is solar energy and methyl alcohol, is the rational evaluation systematic function, adopts
Efficient, the clean generating efficiency of solar energy compare system.Under the simulated conditions, the circulatory system of embodiment 1
Efficient is 57.1%, and the clean generating efficiency of solar energy is about 30%.Under identical basic loop parameter condition, 450 ℃ of the solar thermal energy temperature that ISCC system solar collector is assembled, 1400 ℃/18bar of gas turbine inlet air parameter,
Efficient is 56.5%, and the clean generating efficiency of solar energy is 23.8%, by comparison, and system of the present invention among the embodiment 1
Efficient exceeds 0.6 percentage point, and the clean generating efficiency of solar energy exceeds 6.2 percentage points; Traditional 1400 ℃/18bar of combined cycle system gas turbine inlet air parameter,
Efficient 55.0%, by comparison, system of the present invention among the embodiment 1
Efficient exceeds 2.1 percentage points.In addition, the present invention is at CO
2Separate with the capture aspect and have clear superiority.Because system input solar energy is used for instead of part methyl alcohol, under identical clean output work condition, native system can be saved 11.8% fuel, CO
2Discharge capacity is reduced to 0.364_kg/kWh by the 0.413_kg/kWh of traditional combined cycle.Adopt chemical absorption method from low pressure, low-temperature flue gas, to reclaim CO
2Energy consumption be about 0.34_kWh/kg CO
2, because 53.2% the CO that native system produces among the embodiment 1
2From reduction reaction, this part CO
2Can realize zero energy consumption separation by the simple physics condensation, therefore adopt the present invention can make CO
2The recovery energy consumption significantly descend, by 0.34kWh/kg CO
2Drop to 0.14kWh/kg CO
2
For the circulatory system of embodiment 2, when the methyl alcohol flow is 1_mol/s, 1000 ℃ of oxidizing reaction temperatures, during 1400 ℃/18bar of combustion gas turbine inlet condition, the clean output work of circulation is 410_kW, the thermal efficiency of cycle of system is 64.4%,
Efficient is 57.2%.Under identical basic loop parameter condition, traditional 1400 ℃/18bar of combined cycle system gas turbine inlet air parameter, thermal efficiency of cycle is 61.6%,
Efficient is 55.0%, and by comparison, system thermal efficiency of the present invention exceeds 2.8 percentage points among the embodiment 2,
Efficient exceeds 2.2 percentage points.In addition, the present invention is at CO
2Separate with the capture aspect and have clear superiority.Under the identical clean output work condition, native system can be saved 3.9% fuel, CO
2Discharge capacity is reduced to 0.397_kg/kWh by the 0.413_kg/kWh of traditional combined cycle.Adopt chemical absorption method from low pressure, low-temperature flue gas, to reclaim CO
2Energy consumption be about 0.34_kWh/kg CO
2, because 55.7% the CO that native system produces among the embodiment 2
2From reduction reaction, this part CO
2Can realize zero energy consumption separation by the simple physics condensation, therefore adopt the present invention can make CO
2The recovery energy consumption significantly descend, by 0.34kWh/kg CO
2Drop to 0.145kWh/kg CO
2
System effectiveness of the present invention, solar energy thermal-power-generating efficient improve and CO
2The basic reason that reclaims the energy consumption reduction is:
1. adopt low-temperature solar energy in the solar collector gathering among solar energy and the complementation of alternative fuel grade, cascade utilization: the embodiment 1, in order to the not high raw material preheating of temperature requirement, reduction reaction and the required heat of decomposition reaction to be provided, realized reasonable, the cascade utilization of middle low-temperature solar energy; Adopt burning chemistry chains, the mode that traditional fuel is directly burnt changes the burning chemistry chains mode into, has reduced the grade of fuel, has reduced burning greatly
Loss; Reclaim high temperature circulation particle sensible heat, be used for pre-hot synthesis gas, compressed air, reduce heat exchange
Loss.
2. adopt afterburning among the raising of gas turbine entrance initial temperature: the embodiment 1, overcome the burning chemistry chains dynamical system because of the low problem of combustion gas turbine entrance initial temperature that the recycled material restriction causes, improved combustion gas turbine entrance initial temperature;
3. the middle low-temperature solar energy that the reduction reaction process absorbs among the lifting of middle low-temperature solar energy grade: the embodiment 1 is stored among the FeO with the chemical energy form, and in oxidation reactor, pass through oxidation reaction, form with high temperature heat is emitted, realized that the grade of middle low-temperature solar energy is to the lifting of high temperature heat grade, and comparing the oxidation reaction thermal discharge with direct burning increases to some extent, increases part and is the amount that reduction reaction absorbs solar energy; The middle low-temperature solar energy that the decomposition reaction process absorbs among the embodiment 1 is stored in the synthesis gas with the chemical energy form, and discharge by the form of afterburning with high temperature heat, the low-grade high-grade to high temperature heat that has realized middle low-temperature solar energy promotes, and comparing its thermal discharge with direct combustion methanol increases to some extent, increases the amount that part is the solar thermal energy of decomposition reaction absorption.
The solar energy utilization and control CO
2Discharge integrated: owing to utilize the solar thermal energy required heat of preheating, reduction reaction and decomposition reaction of supplying raw materials, reduced the use amount of fuel, thereby reduced the CO of system among the embodiment 1
2Discharge capacity; Owing to adopt the indirect burning mode of burning chemistry chains, CO in the reduction reactor
2Concentration height and the condensation of process simple physics can be removed steam, isolate CO
2, do not need special CO
2Separator and extra energy consumption have realized CO
2Zero energy consumption separate, greatly reduce CO
2Separation and capture energy consumption.
The basic loop parameter of table 1 system (being applicable to embodiment 1,2)
| | Embodiment | 1 | |
| Optical efficiency (%) | 65 | - | |
| Reduction reactor absorption efficiency (%) | 80 | - | |
| The solar thermal energy temperature (℃) | 250 | - | |
| Reduction reaction temperature (℃) | 200 | Adiabatic alternating temperature | |
| Gas turbine entrance initial temperature (℃) | 1400 | 1400 | |
| Reduction reactor pressure (bar) | 1 | 1 | |
| The compressor pressure ratio | 18.5 | 18.5 | |
| Burning crushing (%) | 3 | 3 | |
| The compressor isentropic efficiency | 0.88 | 0.88 | |
| The gas turbine isentropic efficiency | 0.91 | 0.91 | |
| The steam turbine isentropic efficiency | 0.88 | 0.88 | |
| High voltage/low voltage steam pressure (bar) | 160/10 | 100/4 | |
| The high voltage/low voltage steam temperature (℃) | 540/300 | 535/260 | |
| The waste heat boiler pinch-point temperature difference (℃) | 10 | 10 |
Table 2 embodiment 1 cyclic balance work condition state parameter
Table 3 is implemented 1 circulation thermodynamic performance
Table 4 embodiment 2 cyclic balance work condition state parameters
| Logistics | T (℃) | P (bar) | G (mol/s) | Logistics | T (℃) | P (bar) | G (mol/s) |
| S1 | 25 | 1 | 1 | S13 | 1000 | 18.5 | 24.64 |
| S2 | 25 | 1 | 0.56 | S14 | 1000 | 18.5 | 22.97 |
| S3 | 25 | 1 | 0.44 | S15 | 1000 | 1 | 1.67 |
| S4 | 150 | 1 | 0.56 | S16 | 1400 | 18 | 23.63 |
| S5 | 159 | 1 | 3.34 | S17 | 26 | 18.5 | 0.44 |
| S6 | 159 | 1 | 1.67 | S18 | 180 | 18.5 | 0.44 |
| S7 | 550 | 1 | 1.67 | S19 | 300 | 18 | 1.29 |
| S8 | 25 | 1 | 27.08 | S20 | 900 | 18 | 1.29 |
| S9 | 449 | 18.5 | 27.08 | S21 | 578.6 | 1.03 | 26.91 |
| S10 | 603.5 | 18.5 | 23.8 | S22 | 395 | 1.03 | 9.96 |
| S11 | 933 | 1 | 1.67 | S23 | 247 | 1.03 | 9.96 |
| S12 | 480 | 1 | 3.34 | S24 | 180 | 1.03 | 9.96 |
Table 5 is implemented 2 circulation thermodynamic performance
Annotate:
Computing formula in table 3, the table 5:
Input heat=methyl alcohol Lower heat value * methyl alcohol flow rate+input solar thermal energy;
The heat efficiency=clean output work/input heat;
Ambient condition is got 25 ℃, 1_bar.
Above-described specific embodiment; purpose of the present invention, technical scheme and beneficial effect are further described; institute is understood that; the above only is specific embodiments of the invention; be not limited to the present invention; within the spirit and principles in the present invention all, any modification of making, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (6)
1. control CO for one kind
2The solar energy of discharging and the burning chemistry chains round-robin method of methanol fuel complementation is characterized in that this method comprises:
One methanol fuel reduces Fe under the driving of middle low-temperature solar energy
2O
3Circulating granular, middle low-temperature solar energy is converted into chemical energy to be stored among the reduction product Fe O, FeO continues oxidation by air regeneration, emit big calorimetric and produce high-temperature flue gas, the middle low-temperature solar energy that is stored in simultaneously among the FeO discharges with the form of high temperature heat, and the grade of low-temperature solar energy promotes in the realization; Low-temperature solar energy refers to the solar energy of temperature range between 150 ℃ to 300 ℃ in described;
At above-mentioned one methanol fuel reduction Fe
2O
3In the time of circulating granular, another strand methanol fuel is broken down under middle low-temperature solar energy drives and comprises H
2Synthesis gas with CO, middle low-temperature solar energy is converted into the chemical energy of synthesis gas, the high-temperature flue gas generation combustion reaction that synthesis gas and circulating granular regenerative process produce, drive the combustion gas turbine acting with further raising flue-gas temperature, the middle low-temperature solar energy that is stored in simultaneously in the synthesis gas discharges with the form of high temperature heat, and the low-temperature solar energy grade is to the lifting of high temperature heat grade in finishing.
2. control CO who be used for to realize the described method of claim 1
2The solar energy of discharging and the burning chemistry chains electricity generation system of methanol fuel complementation is characterized in that, this system is made of the chemical chain combustion apparatus of middle low-temperature solar energy driving and the combustion-compensating device of middle low-temperature solar energy driving, wherein:
The chemical chain combustion apparatus that middle low-temperature solar energy drives, comprise solar energy heating-reduction reactor (2), oxidation reactor (6), gas-solid heat exchanger (3,5,12,13), shunt (19), cyclone separator (7), the first solar energy preheater (1) and first pump (9), wherein:
Solar energy heating-reduction reactor (2) utilizes solar collector, and the solar energy collecting that will hang down energy-flux density in the line focus mode becomes the middle low temperature heat energy of high fluence density, is received from methyl alcohol and the circulating granular Fe of the first solar energy preheater (1) in order to driving
2O
3Reduction reaction;
Oxidation reactor (6) is used for the oxidation reaction that strong heat release takes place for compressed air after the preheating and the circulating granular FeO after the preheating;
Gas-solid heat exchanger (3,5,12,13), heat transmission equipment is used for the exchange heat between the hot and cold logistics of realization;
Shunt (19), part flow arrangement is used for methyl alcohol is carried out the quality shunting;
Cyclone separator (7) is used for the gas-solid mixture that above-mentioned oxidation reaction produces is carried out gas solid separation;
The combustion-compensating device that middle low-temperature solar energy drives, comprise solar energy heating-decomposition reactor (11), afterburning combustion chamber (8), combustion gas turbine (14), waste heat boiler (15), steam turbine (16), condenser (17), the second solar energy preheater (10), second pump (18) and compressor (4), wherein:
Solar energy heating-decomposition reactor (11) utilizes solar collector, and the solar energy collecting that will hang down energy-flux density in the line focus mode becomes the middle low temperature heat energy of high fluence density, is received from the methanol decomposition reaction of the second solar energy preheater (10) in order to driving;
Flue-gas temperature for the synthesis gas after the Methanol Decomposition and the flue gas generation combustion reaction that is received from cyclone separator, is further improved in afterburning combustion chamber (8);
Combustion gas turbine (14) is used for being received from the high-temperature flue gas expansion acting of afterburning combustion chamber;
Waste heat boiler (15) for the fume afterheat of retrieving from the combustion gas turbine, produces high steam or low-pressure steam, enters steam turbine (16) acting then.
3. control CO according to claim 2
2The solar energy of discharging and the burning chemistry chains electricity generation system of methanol fuel complementation, it is characterized in that, the burning chemistry chains mode that low-temperature solar energy drove during described one methanol fuel adopted, methanol steam after the preheating enters solar energy heating-reduction reactor, under middle low-temperature solar energy drives with circulating granular Fe
2O
3Reduction reaction takes place, and produces solid particle FeO and gaseous state product water steam and CO
2, FeO emits a large amount of heat through compressed air oxidation regeneration in oxidation reactor after the preheating, generates high temperature Fe
2O
3And flue gas, after gas solid separation, high-temperature flue gas enters afterburning combustion chamber, Fe
2O
3Particle enters reduction reactor recirculation behind the heat exchanger recovery waste heat.
4. control CO according to claim 2
2The solar energy of discharging and the burning chemistry chains electricity generation system of methanol fuel complementation is characterized in that, at described one methanol fuel reduction Fe
2O
3In the time of circulating granular, after the preheating of described another strand methanol fuel, enter solar energy heating-decomposition reactor, under the driving of middle low temperature solar thermal energy, decomposition reaction takes place, produce synthesis gas, acting as a fuel after synthesis gas is preheated enters the afterburning combustion chamber, with the high-temperature flue gas that is received from cyclone separator, combustion reaction takes place, emit a large amount of heat, further improve combustion gas turbine entrance initial temperature.
5. control CO according to claim 2
2Solar energy and the burning chemistry chains electricity generation system of methanol fuel complementation of discharging is characterized in that, described solar collector employing parabolic slot type concentration structure, and the solar energy collecting that will hang down energy-flux density in the line focus mode becomes the middle low temperature heat energy of high fluence density.
6. control CO according to claim 2
2The solar energy of discharging and the burning chemistry chains electricity generation system of methanol fuel complementation, it is characterized in that, under the more weak situation of no solar energy or solar irradiation intensity, reduction reaction institute calorific requirement in this system is provided by the sensible heat that circulating granular carries, and decomposition reactor and methyl alcohol preheating institute calorific requirement are provided by fume afterheat according to each process institute energy requirement taste difference.
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| 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 |
| CN103807009B (en) * | 2012-11-13 | 2016-01-06 | 中国科学院工程热物理研究所 | The distributed internal-combustion engine cool and thermal power system and method for solar energy and alternative fuel complementation |
| US9200799B2 (en) * | 2013-01-07 | 2015-12-01 | Glasspoint Solar, Inc. | Systems and methods for selectively producing steam from solar collectors and heaters for processes including enhanced oil recovery |
| CN103352814B (en) * | 2013-07-25 | 2015-06-24 | 中国科学院工程热物理研究所 | Parabolic groove type composite power generation system with solar heat collector and chemical heat pump being combined together |
| WO2015048845A1 (en) * | 2013-10-02 | 2015-04-09 | Adelaide Research & Innovation Pty Ltd | A hybrid solar and chemical looping combustion system |
| CN104445060B (en) * | 2014-10-31 | 2017-05-03 | 中国科学院工程热物理研究所 | Comprehensive utilization method for high-temperature energy |
| CN104912607A (en) * | 2015-06-10 | 2015-09-16 | 中国华电工程(集团)有限公司 | Tower type solar optothermal and gas hybrid generation system |
| CN104912757A (en) * | 2015-06-10 | 2015-09-16 | 中国华电工程(集团)有限公司 | Trough-type solar thermal and natural gas combined power generation system |
| CN104912755A (en) * | 2015-06-10 | 2015-09-16 | 中国华电工程(集团)有限公司 | Fresnel type solar photo-thermal and natural gas combined power generating system |
| CN110118160B (en) * | 2018-02-06 | 2020-10-30 | 浙江大学 | Solar supercritical carbon dioxide Brayton cycle system |
| CN108507188B (en) * | 2018-03-13 | 2020-02-21 | 上海理工大学 | Combined heat and power generation system based on solar integrated oxygen-enriched combustion and chemical looping combustion and working method thereof |
| CN109704276A (en) * | 2018-12-19 | 2019-05-03 | 上海电力学院 | A kind of hydrogen production of chemical chain and power generation cycle system of Driven by Solar Energy |
| CN111217330B (en) * | 2020-01-20 | 2022-03-08 | 西安交通大学 | Solar methane chemical-looping reforming reactor and using method thereof |
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