CN105727697A - Solar photovoltaic refrigeration assisted hydrate method carbon capture system - Google Patents
Solar photovoltaic refrigeration assisted hydrate method carbon capture system Download PDFInfo
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- CN105727697A CN105727697A CN201610169512.XA CN201610169512A CN105727697A CN 105727697 A CN105727697 A CN 105727697A CN 201610169512 A CN201610169512 A CN 201610169512A CN 105727697 A CN105727697 A CN 105727697A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B21/00—Machines, plants or systems, using electric or magnetic effects
- F25B21/02—Machines, plants or systems, using electric or magnetic effects using Peltier effect; using Nernst-Ettinghausen effect
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/002—Machines, plants or systems, using particular sources of energy using solar energy
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/002—Machines, plants or systems, using particular sources of energy using solar energy
- F25B27/007—Machines, plants or systems, using particular sources of energy using solar energy in sorption type systems
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
Abstract
The invention discloses a solar photovoltaic refrigeration assisted hydrate method carbon capture system. A solar power generation device is connected with a thermoelectricity refrigeration device and an inverter, and the other end of the inverter is connected with an absorption-type refrigerating machine and various levels of compressors; after exchanging heat with the thermoelectricity refrigeration device and the adsorption-type refrigerating machine, a refrigerating medium exchanges heat with various levels of coolers and various levels of reaction kettles; and mixed gas such as industrial smoke CO2, N2 and the like successively passes through the absorption-type refrigerating machine, a primary hydrate method carbon capture system and a secondary hydrate method carbon capture system. By utilizing the solar photovoltaic refrigeration assisted hydrate method carbon capture system, the gradient utilization of energy is realized, the solar power generation is used for providing power to the thermoelectricity refrigerating device, the absorption-type refrigerating machine and various levels of compressors, so as to provide a low-temperature high-pressure environment for generating a hydrate; and by adopting the hydrate two-level separation method, CO2 is captured, the process flow is simple, raw materials are cheap, and the separation efficiency is improved; and the solar power generation system, the thermoelectricity refrigerating system and the hydrate method CO2 capture system are used for separating the industrial gas, so that the pollution to the environment is small, and the energy utilization efficiency is high.
Description
Technical field
The present invention relates to a kind of solar energy auxiliary carbon trapping technique, be specifically related to a kind of solar photoelectric refrigeration auxiliary hydrate and carry out the system of collecting carbonic anhydride.
Background technology
Since entering 21 century, CO2The problems such as the global warming that isothermal chamber gas causes are increasingly severe.CO in air2Concentration quickly raises and is mainly derived from the gas that commercial production is discharged, for instance the waste gas that coal-burning boiler, incinerator, steel mill etc. are discharged all contains the CO of higher concentration2.Therefore, to the CO in industrial smoke2It is easily separated trapping and becomes the emphasis place of reduction of greenhouse gas discharge.
As a kind of emerging technology, hydrate CO2Trapping technique had both had equipment is corrosion-free, environmentally safe feature, can realize again trapping and save as one, therefore being thought the CCS technology of most potentiality by many scholars.Chinese patent CN201110278132.7 discloses a kind of circular carbon dioxide capture device with hydrate method, to solve hydrate CO2The problems such as the speed in trapping process is slow, efficiency is low, easy generation obstruction.CN201410166253.6 discloses a kind of bubble type hydrate trapping carbon dioxide system, and this trapping system can be accurately controlled for CO2The separating medium temperature of trapping, simultaneously to CO in bubble tower2In trapping process hydrate formation and decompose all can carry out quantitative analysis.But both technology all only achieve single-stage and separate, and still there is CO2The response rate is low and reclaims products C O2The problems such as concentration is not high.
Also a lot of two grades of even multi-stage separation devices are occurred in that in recent years, for instance Chinese patent CN201410165156.5 discloses and a kind of traps CO based on hydrate2Recirculating fluidized bed furnace system.This system is in conjunction with fluidizing theory, and design has two-stage reactor, to improve utilization of materials.This patent is pointed out, recirculating fluidized bed furnace system can be trap CO based on hydrate2Technology provide one and can realize industrialized device.But the reactor played a major role needs to rely on extra power to maintain the environment of cryogenic high pressure, thus forming hydrate.And this system is not carried out cascaded utilization of energy, efficiency of energy utilization is relatively low, and operating cost is too high, and this also becomes and realizes one of industrialized bottleneck.
Additionally, energy consumption remains high, it is existing CO2The common drawback of trapping technique.Therefore also having Many researchers to attempt combining regenerative resource with CCS, the patent if publication number is CN201410394352.X proposes the integrated system of the trapping of a kind of solar energy auxiliary carbon dioxide and heat supply, and adopting solar energy heating subsystem is CO2Trapping energy supply, and the heat in system is comprehensively utilized by thermograde, to realize the raising of system overall thermal efficiency.But the capture method proposed in this patent is ethanolamine (MEA) solution absorption method, and MEA solution is relatively costly, has certain corrosivity, and easily by the SO in flue gas2And O2Aoxidized.Comparatively speaking, hydrate is to use the water being readily available as raw material, and equipment is corrosion-free, and not easily oxidized, if can combine with regenerative resource, will effectively reduce operating cost, while having superior environmental-protecting performance, promote economy, be advantageously implemented heavy industrialization.
Summary of the invention
It is an object of the invention to the cascade utilization by solar energy, design a kind of solar photoelectric refrigeration auxiliary hydrate carbon trapping system, use present system to make inlet flue gas after sequentially passing through three grades of heat exchange of air cooler, First Heat Exchanger, the second heat exchanger and the first cooler and the second cooler, pass into generation hydrate in the first reactor and the second reactor and realize step heat exchange, and reclaim CO2Gas.
In order to solve above-mentioned technical problem, a kind of solar photoelectric refrigeration auxiliary hydrate carbon trapping system that the present invention proposes, including solar generator refrigeration subsystem, solar powered pressure control subsystem, refrigerating medium cycle subsystem, collecting carbonic anhydride subsystem, described collecting carbonic anhydride subsystem is hydrate two-stage carbon dioxide trapping subsystem；Described solar generator refrigeration subsystem includes the thermoelectric cooling unit being connected with device of solar generating one end, described thermoelectric cooling unit includes the first hot junction being sequentially connected in series, cold end and the second hot junction, and one end of described device of solar generating connects into primary Ioops with described first hot junction and the second hot junction；Described solar powered pressure control subsystem includes the inverter being connected with the device of solar generating other end, the Absorption Refrigerator in parallel with the described inverter other end, first order compressor, high stage compressor, air cooler and third level compressor；Described refrigerating medium cycle subsystem includes refrigerating medium heat exchanger, Absorption Refrigerator and refrigerating medium loop, and described Absorption Refrigerator includes vaporizer, condenser, generator and absorber；Described hydrate two-stage carbon dioxide trapping subsystem includes First Heat Exchanger, the first cooler, first order reactor, the second heat exchanger, the second cooler and described second level reactor；The entrance of described first order compressor is connected to the generator thermal source outlet of Absorption Refrigerator；Described First Heat Exchanger is connected between first order compressor and described air cooler；Described high stage compressor is connected with described air cooler, and described first cooler and first order reactor are connected in turn between described air cooler and described third level compressor；The gas outlet of described first order reactor is connected to the gas approach of described First Heat Exchanger, and the connecting line between described first order reactor and described First Heat Exchanger is provided with valve；The outlet of described third level compressor is connected with the second heat exchanger, the second cooler and described second level reactor successively；The gas outlet of described second level reactor is connected to the gas approach of the second heat exchanger, and the connecting line between described second level reactor and described second heat exchanger is provided with valve；Described first order reactor and described second level reactor are provided with Pressure gauge and thermometer respectively；The entrance point of the zone of heat liberation of described refrigerating medium heat exchanger is connected to the first extraction pipeline, the port of export of the zone of heat liberation of described refrigerating medium heat exchanger is connected to the second extraction pipeline, the arrival end of described first cooler, the cooling device import of described first order reactor, the arrival end of described second cooler and the cooling device import of described second level reactor are connected to described first by each independent refrigerating medium branch road respectively and draw on pipeline, the port of export of described first cooler, the cooling device outlet of described first order reactor, the arrival end of described second cooler and the cooling device outlet of described second level reactor are connected to described second by each independent refrigerating medium loop respectively and draw on pipeline；Interconnective first draws pipeline, refrigerating medium branch road, refrigerating medium loop and the second extraction pipeline constitutes described refrigerating medium loop；Described Absorption Refrigerator vaporizer and described refrigerating medium loop carry out heat exchange, and described Absorption Refrigerator is positioned at the entrance point side of the zone of heat liberation of described refrigerating medium heat exchanger, and the vaporizer of described Absorption Refrigerator is drawn pipeline with described first and is connected；The port of export side of the described second zone of heat liberation drawn on pipeline and be positioned at described refrigerating medium heat exchanger is provided with a circulating pump.
Compared with prior art, the invention has the beneficial effects as follows:
(1) realizing the cascade utilization of energy, utilize solar electrical energy generation, provide electric energy to thermoelectric cooling unit, compressor at different levels and Absorption Refrigerator, high-temperature flue gas is as Absorption Refrigerator thermal source.Thermoelectric cooling unit and Absorption Refrigerator provide cold to need low temperature environment to maintain hydrate generation, and compressors at different levels provide hydrate to generate required environment under high pressure；
(2) hydrate two-stage separation method is adopted to realize CO2Trapping, technological process is simple, raw material economics, and two-stage separation efficiency separates high than single-stage.
(3) inlet flue gas sequentially passes through Absorption Refrigerator, air cooler, residual gas heat exchanger and cooler, passes into generation hydrate in reactor, it is achieved step heat exchange, improve capacity usage ratio after level Four heat exchange.
(4) this system adopts solar electrical energy generation, thermoelectric cooling, hydrate CO2The systems such as trapping realize the separation of factory smoke, and environmental pollution is little.
Accompanying drawing explanation
Fig. 1 is that solar photoelectric of the present invention refrigeration auxiliary hydrate carbon trapping system constitutes schematic diagram.
In figure；
1-device of solar generating 2-unidirectional current electric wire 31,32-thermoelectric cooling unit hot junction
The cold end 4-refrigerating medium heat exchanger 5-Absorption Refrigerator of 33-thermoelectric cooling unit
6-circulating pump 7-refrigerating medium loop 8-inverter
9-alternating current electric wire 10-first order compressor 11-First Heat Exchanger
12-high stage compressor 13-air cooler 14-the first cooler
15-first order reactor 16-third level compressor 17-the second heat exchanger
18-the second cooler 19-second level reactor 20～25-valve
26,27～Pressure gauge 28,29-thermometer
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, technical solution of the present invention being described in further detail, the present invention is only explained by described specific embodiment, not in order to limit the present invention.
As it is shown in figure 1, one solar photoelectric of the present invention refrigeration auxiliary hydrate carbon trapping system, including solar generator refrigeration subsystem, solar powered pressure control subsystem, refrigerating medium cycle subsystem, collecting carbonic anhydride subsystem.
Described collecting carbonic anhydride subsystem is hydrate two-stage carbon dioxide trapping subsystem；
Described solar generator refrigeration subsystem includes the thermoelectric cooling unit being connected with device of solar generating 1 one end, described thermoelectric cooling unit includes the first hot junction 31 being sequentially connected in series, cold end 33 and the second hot junction 32, and one end of described device of solar generating 1 connects into primary Ioops with described first hot junction 31 and the second hot junction 32.
Described solar powered pressure control subsystem includes the inverter 8 being connected with device of solar generating 1 other end, the Absorption Refrigerator 5 in parallel with described inverter 8 other end, first order compressor 10, high stage compressor 12, air cooler 13 and third level compressor 16.
Described refrigerating medium cycle subsystem includes refrigerating medium heat exchanger 4, Absorption Refrigerator 5 and refrigerating medium loop 7, and described Absorption Refrigerator 5 includes vaporizer, condenser, generator and absorber.
Described hydrate two-stage carbon dioxide trapping subsystem includes First Heat Exchanger the 11, first cooler 14, first order reactor the 15, second heat exchanger the 17, second cooler 18 and described second level reactor 19.
The entrance of described first order compressor 10 is connected to the generator thermal source outlet of Absorption Refrigerator 5；Described First Heat Exchanger 11 is connected between first order compressor 10 and described air cooler 13；Described high stage compressor 12 is connected with described air cooler 13, and described first cooler 14 and first order reactor 15 are connected in turn between described air cooler 13 and described third level compressor 16；The gas outlet of described first order reactor 15 is connected to the gas approach of described First Heat Exchanger 11, and the connecting line between described first order reactor 15 and described First Heat Exchanger 11 is provided with valve 24；The outlet of described third level compressor 16 is connected with second heat exchanger the 17, second cooler 18 and described second level reactor 19 successively；The gas outlet of described second level reactor 19 is connected to the gas approach of the second heat exchanger 17, and the connecting line between described second level reactor 19 and described second heat exchanger 17 is provided with valve 25；Described first order reactor 15 and described second level reactor 19 are provided with Pressure gauge and thermometer respectively.
The entrance point of the zone of heat liberation of described refrigerating medium heat exchanger 4 is connected to the first extraction pipeline 71, the port of export of the zone of heat liberation of described refrigerating medium heat exchanger 4 is connected to the second extraction pipeline 72, the arrival end of described first cooler 14, the cooling device import of described first order reactor 15, the arrival end of described second cooler 18 and the cooling device import of described second level reactor 19 are connected to described first by each independent refrigerating medium branch road respectively and draw on pipeline, the port of export of described first cooler 14, the cooling device outlet of described first order reactor 15, the arrival end of described second cooler 18 and the cooling device outlet of described second level reactor 19 are connected to described second by each independent refrigerating medium loop respectively and draw on pipeline 72；Interconnective first draws pipeline 71, refrigerating medium branch road, refrigerating medium loop and the second extraction pipeline 72 constitutes described refrigerating medium loop 7；Described Absorption Refrigerator 5 vaporizer and described refrigerating medium loop 7 carry out heat exchange, described Absorption Refrigerator 5 is positioned at the entrance point side of the zone of heat liberation of described refrigerating medium heat exchanger 4, and the vaporizer of described Absorption Refrigerator 5 is drawn pipeline 71 with described first and is connected；The port of export side of the described second zone of heat liberation drawn on pipeline 72 and be positioned at described refrigerating medium heat exchanger 4 is provided with a circulating pump 6.
Solar generator refrigeration subsystem is coupled together by refrigerating medium heat exchanger 4 and Absorption Refrigerator 5 with refrigerating medium cycle subsystem, under the effect of the circulating pump 6 of refrigerating medium loop head connection, refrigerating medium ethylene glycol solution in refrigerating medium heat exchanger 4 with cold end 3 heat exchange of thermoelectric cooling unit, afterwards, valve 20 on refrigerating medium branch road respectively after refrigerating medium and the cold end 4 of thermoelectric cooling unit and Absorption Refrigerator 5 heat exchange, valve 21, valve 22, valve 23 is to the first cooler 14, first order reactor 15, second cooler 18, second level reactor 19 device such as grade freezes, industrial smoke CO2、N2Mixing gas passes sequentially through Absorption Refrigerator 5 through pipeline, first order compressor 10, First Heat Exchanger 11, high stage compressor 12, air cooler 13, first cooler 14, first order reactor 15, the residual gas not generating hydrate after first order reactor 15 passes sequentially through valve 24, First Heat Exchanger 11, with heat transfer of mixture gas, the gas that decomposition of hydrate produces passes sequentially through first order reactor 15, third level compressor 16, second heat exchanger 17, second cooler 18, second level reactor 19, the gas of hydrate is not generated by valve 25 through second level reactor 19, second heat exchanger 17, heat exchange is carried out with the mixing gas of one-level decomposition of hydrate.
Through refrigerating medium heat exchanger 4 and Absorption Refrigerator 5, refrigerating medium ethylene glycol solution in refrigerating medium loop 7 passes sequentially through circulating pump 6, valve the 20, first cooler 14, valve 21, first order reactor 15, valve the 22, second cooler 18, valve 23, second level reactor 19 through pipeline, thus constituting refrigerating medium cycle subsystem；
Industrial smoke CO2、N2Absorption Refrigerator 5 is passed sequentially through through pipeline Deng mixing gas, first order compressor 10, First Heat Exchanger 11, high stage compressor 12, air cooler 13, first cooler 14, first order reactor 15, the residual gas not generating hydrate passes sequentially through valve 24 through pipeline, First Heat Exchanger 11, the gas that decomposition of hydrate produces passes sequentially through third level compressor 16 through pipeline, second heat exchanger 17, second cooler 18, second level reactor 19, the gas not generating hydrate passes sequentially through second level reactor 19, valve 25, second heat exchanger 17, constitute hydrate two-stage carbon dioxide trapping system.
Solar generator refrigeration subsystem is coupled together by refrigerating medium heat exchanger 4 with refrigerating medium cycle subsystem, it is connected to circulating pump 6 at refrigerating medium loop head, under the effect of circulating pump 6, ethylene glycol solution in refrigerating medium heat exchanger 4 with cold end 31 and 32 heat exchange of thermoelectric cooling unit, afterwards by pipeline respectively through valve 20, valve 21, valve 22, valve 23 is to the first cooler 14, first order reactor 15, second cooler 18, second level reactor 19 device such as grade freezes, refrigerating medium cycle subsystem is connected with hydrate two-stage carbon dioxide trapping system herein.The refrigerating medium flow in each separate Zhi Huilu can be controlled by controlling the aperture of each valve, the aperture size of each valve is controlled by the monitor signal of the thermometer 28 and 29 on the first reactor 15 and the second reactor 19, to provide suitable cold to generate required temperature environment to maintain hydrate, every one-level hydration reaction of formation still design temperature is 4.5 DEG C, and decomposition of hydrate temperature is 25 DEG C.
Solar powered pressure control subsystem is coupled together by Absorption Refrigerator 5, first order compressor 10, high stage compressor 12, air cooler 13, third level compressor 16 with hydrate two-stage carbon dioxide trapping system.By compressors at different levels, mixing gas being pressurizeed maintain hydrate and generate required pressure environment, first order hydration reaction of formation still operation pressure is 2.50MPa, and two grades of hydrate reaction of formation still operation pressure are 0.90MPa.
The workflow of hydrate two-stage carbon dioxide trapping system is: industrial smoke CO2、N2nullIt is introduced into Absorption Refrigerator 5 as high temperature heat source Deng mixing gas，It is compressed to 0.5MPa by 0.1MPa then through first order compressor 10，The residual gas that flue gas is discharged with first order reactor 15 top after being compressed by first order compressor 10 is by First Heat Exchanger 11 heat exchange，It is compressed to 2.5MPa by high stage compressor 12 by 0.5MPa after heat exchange，Then through air cooler 13、First cooler 14 is cooled to 4.5 DEG C，Pass into generation hydrate in reactor 15，According to the monitoring of Pressure gauge 26 and thermometer 28 in first order reactor 15，When pressure stability 2.5MPa and temperature stabilization 4.5 DEG C，Stop passing into gas，Carrying out along with hydrate reaction of formation，In reactor, pressure reduces，Show that reaction of formation terminates when detecting when pressure no longer changes，Now open reactor top valve 24 and discharge residual gas，Close valve 24、20、21，First order reactor 15 temperature raises the decomposition reaction carrying out hydrate，Reactor exit is determined by gas chromatograph no longer has gas release to show to decompose completely，Then valve 24 is opened、21、20.The gas decomposited is compressed to 0.9MPa through third level compressor 16, the residual gas discharged with second level reactor 19 top after being compressed by third level compressor 16 is by the second heat exchanger 17 heat exchange, it is cooled to 4.5 DEG C then through the second cooler 18 and passes into generation hydrate in reactor 19, according to the monitoring of Pressure gauge 27 and thermometer 29 in second level reactor 19, when pressure stability 0.9MPa and temperature stabilization 4.5 DEG C, open reactor top valve 25 and discharge residual gas, close valve 25, 22, 23, second level reactor 19 temperature raises the decomposition reaction carrying out hydrate, reactor exit is determined by gas chromatograph no longer has gas release to show to decompose completely, then valve 25 is opened, 22, 23.Finally reclaim CO2Gas, hydrate generates required water and is recycled by the water after decomposition of hydrate.
The total system of the present invention is made up of four subsystems, it may be assumed that solar generator refrigeration subsystem, refrigerating medium cycle subsystem, solar powered pressure control subsystem, hydrate two-stage carbon dioxide trapping system.By heat exchanger 4 ', the cold of the cold end of thermoelectric cooling unit passes to refrigerating medium, solar generator refrigeration subsystem and refrigerating medium cycle subsystem is coupled together；By the first cooler 14, first order reactor the 15, second cooler 18, second level reactor 19, the cold of refrigerating medium passes to flue gas, reaches the purpose of cooled flue gas, refrigerating medium cycle subsystem is connected with hydrate two-stage carbon dioxide trapping system.Solar powered pressure control subsystem and hydrate two-stage carbon dioxide trapping system are connected by multiple-stage adiabatic compressor and Absorption Refrigerator.By the above-mentioned system and device connecting and composing whole collecting carbonic anhydride.
For ensureing the continuous operation of system, it is possible to a whole set of hydrate two-stage carbon dioxide trapping subsystem in parallel.While one subsystem carries out one-level decomposition of hydrate, two grades of hydrate formations, another set of system carries out the catabolic process of the generation of one-level hydrate, two grades of hydrates.
Hydrate is generated by quaternary ammonium salt tetrabutyl ammonium bromide (TBAB), tetrabutyl ammonium fluoride (TBAF), tetrabutylammonium chloride (TBAC) facilitation, better through the facilitation effect of experimentation TBAF, additionally oxolane (THF) also can reduce hydrate generation pressure, but human and environment is very harmful, dangerous in commercial Application.The present invention adopts TBAF as additive, reduces the generation pressure of hydrate, improves hydration reaction efficiency, reduces compression energy consumption.
TABA and the contrast of TBAF hydrate formation rate constants during 1,4.5 DEG C of table
Using present system, flue gas is compressed to hydrate by adiabatic compressor and generates pressure 2.5MPa, is divided into two stages of compression, and the first order is compressed to 0.5MPa by 0.1MPa, and the second level is compressed to 2.5MPa by 0.5MPa.Every one-level hydration reaction of formation temperature is set as 4.5 DEG C, and decomposition of hydrate temperature is set as room temperature 25 DEG C.
To sum up, present system utilizes solar electrical energy generation, provides electric energy to thermoelectric cooling unit, compressor at different levels and air cooler.Thermoelectric cooling unit provides cold to need low temperature environment to maintain hydrate generation, and compressors at different levels provide hydrate to generate required environment under high pressure, and needed for carbon trapping, energy is all provided by regenerative resource.Hydrate two-stage separation method is adopted to realize CO2Trapping, technological process is simple, raw material economics, and two-stage separation efficiency separates high than single-stage, adopts TBAF (4-butyl ammonium fluoride trihydrate) as additive, reduces the generation pressure of hydrate, improve hydration reaction efficiency, reduces compression energy consumption.Inlet flue gas sequentially passes through air cooler, residual gas heat exchanger and cooler, passes into generation hydrate in reactor, it is achieved step heat exchange, improve capacity usage ratio after three grades of heat exchange.
Although above in conjunction with accompanying drawing, invention has been described; but the invention is not limited in above-mentioned detailed description of the invention; above-mentioned detailed description of the invention is merely schematic; rather than it is restrictive; those of ordinary skill in the art is under the enlightenment of the present invention; without deviating from the spirit of the invention, it is also possible to make many variations, these belong within the protection of the present invention.
Claims (1)
1. a solar photoelectric refrigeration auxiliary hydrate carbon trapping system, including solar generator refrigeration subsystem, solar powered pressure control subsystem, refrigerating medium cycle subsystem, collecting carbonic anhydride subsystem, it is characterized in that, described collecting carbonic anhydride subsystem is hydrate two-stage carbon dioxide trapping subsystem；
Described solar generator refrigeration subsystem includes the thermoelectric cooling unit being connected with device of solar generating (1) one end, described thermoelectric cooling unit includes the first hot junction (31) being sequentially connected in series, cold end (33) and the second hot junction (32), one end of described device of solar generating (1) and described first hot junction (31) and the second hot junction (32) connect into primary Ioops；
Described solar powered pressure control subsystem includes the inverter (8) being connected with device of solar generating (1) other end, the Absorption Refrigerator (5) in parallel with described inverter (8) other end, first order compressor (10), high stage compressor (12), air cooler (13) and third level compressor (16)；
Described refrigerating medium cycle subsystem includes refrigerating medium heat exchanger (4), Absorption Refrigerator (5) and refrigerating medium loop (7), and described Absorption Refrigerator (5) includes vaporizer, condenser, generator and absorber；
Described hydrate two-stage carbon dioxide trapping subsystem includes First Heat Exchanger (11), the first cooler (14), first order reactor (15), the second heat exchanger (17), the second cooler (18) and described second level reactor (19)；
The entrance of described first order compressor (10) is connected to the generator thermal source outlet of Absorption Refrigerator (5)；
Described First Heat Exchanger (11) is connected between first order compressor (10) and described air cooler (13)；
Described high stage compressor (12) is connected with described air cooler (13), and described first cooler (14) and first order reactor (15) are connected in turn between described air cooler (13) and described third level compressor (16)；
The gas outlet of described first order reactor (15) is connected to the gas approach of described First Heat Exchanger (11), and the connecting line between described first order reactor (15) and described First Heat Exchanger (11) is provided with valve (24)；
The outlet of described third level compressor (16) is connected with the second heat exchanger (17), the second cooler (18) and described second level reactor (19) successively；The gas outlet of described second level reactor (19) is connected to the gas approach of the second heat exchanger (17), and the connecting line between described second level reactor (19) and described second heat exchanger (17) is provided with valve (25)；
Described first order reactor (15) and described second level reactor (19) are provided with Pressure gauge and thermometer respectively；
The entrance point of the zone of heat liberation of described refrigerating medium heat exchanger (4) is connected to the first extraction pipeline (71), the port of export of the zone of heat liberation of described refrigerating medium heat exchanger (4) is connected to the second extraction pipeline (72)
The arrival end of described first cooler (14), the cooling device import of described first order reactor (15), the arrival end of described second cooler (18) and the cooling device import of described second level reactor (19) are connected to described first by each independent refrigerating medium branch road respectively and draw on pipeline (71)；The port of export of described first cooler (14), the cooling device outlet of described first order reactor (15), the port of export of described second cooler (18) and the cooling device outlet of described second level reactor (19) are connected to described second by each independent refrigerating medium loop respectively and draw on pipeline (72)；
Interconnective first draws pipeline (71), refrigerating medium branch road, refrigerating medium loop and the second extraction pipeline (72) constitutes described refrigerating medium loop (7)；
Described Absorption Refrigerator (5) vaporizer and described refrigerating medium loop (7) carry out heat exchange, described Absorption Refrigerator (5) is positioned at the entrance point side of the zone of heat liberation of described refrigerating medium heat exchanger (4), and the vaporizer of described Absorption Refrigerator (5) is drawn pipeline (71) with described first and is connected；The port of export side of the described second zone of heat liberation drawn on pipeline (72) and be positioned at described refrigerating medium heat exchanger (4) is provided with a circulating pump (6).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113465222A (en) * | 2021-07-07 | 2021-10-01 | 寒地黑土能源科技有限公司 | Solar remote control absorption refrigeration system |
| CN114247270A (en) * | 2021-12-14 | 2022-03-29 | 西安热工研究院有限公司 | Carbon dioxide circulating electric adsorption capturing and sealing system |
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| CN202052455U (en) * | 2011-04-26 | 2011-11-30 | 华北电力大学 | Solar auxiliary extraction flue gas decarburization and refrigeration combination system with liquid absorbent |
| US8641812B2 (en) * | 2010-05-17 | 2014-02-04 | General Electric Company | Gas treatment and solar thermal collection system |
| CN204563877U (en) * | 2015-01-13 | 2015-08-19 | 宁波瑞信能源科技有限公司 | Solar energy cascade phase-transition heat-storage indirect steam auxiliary carbon dioxide trapping system |
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| US8641812B2 (en) * | 2010-05-17 | 2014-02-04 | General Electric Company | Gas treatment and solar thermal collection system |
| CN102258927A (en) * | 2010-05-26 | 2011-11-30 | 李溪 | Device for capturing flue gas CO2 of coal-fired power plant |
| CN202052455U (en) * | 2011-04-26 | 2011-11-30 | 华北电力大学 | Solar auxiliary extraction flue gas decarburization and refrigeration combination system with liquid absorbent |
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| CN113465222A (en) * | 2021-07-07 | 2021-10-01 | 寒地黑土能源科技有限公司 | Solar remote control absorption refrigeration system |
| CN114247270A (en) * | 2021-12-14 | 2022-03-29 | 西安热工研究院有限公司 | Carbon dioxide circulating electric adsorption capturing and sealing system |
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