CN202485229U - Heat-supply system implemented through natural gas combustion - Google Patents
Heat-supply system implemented through natural gas combustion Download PDFInfo
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- CN202485229U CN202485229U CN2012200402472U CN201220040247U CN202485229U CN 202485229 U CN202485229 U CN 202485229U CN 2012200402472 U CN2012200402472 U CN 2012200402472U CN 201220040247 U CN201220040247 U CN 201220040247U CN 202485229 U CN202485229 U CN 202485229U
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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
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The utility model discloses a heat-supply system implemented through natural gas combustion, which comprises a natural gas combustion device and a carbon dioxide capturing device, wherein the natural gas combustion device comprises a first chemical chain combustion reactor, a second chemical chain combustion reactor and a reforming reactor, the first chemical chain combustion reactor and the second chemical chain combustion reactor are connected in parallel with each other, and the reforming reactor is connected to the first chemical chain combustion reactor and the second chemical chain combustion reactor through a first valve; and the carbon dioxide capturing device is connected to the natural gas combustion device, and used for receiving carbon dioxide emitted by the first chemical chain combustion reactor and the second chemical chain combustion reactor. Because the system is provided with two parallelly-connected chemical chain combustion reactors, and the two reactors can alternately carry out redox reaction on oxygen carriers, the whole system can carry out continuous heating. The system is also provided with a carbon dioxide capturing device, so that carbon dioxide generated by the system can be converted into liquid carbon dioxide and then recycled, stored and transported, thereby realizing the great carbon dioxide emission reduction of the whole system.
Description
Technical field
The utility model relates to the combustion technology of energy field, particularly relates to the combustion heat supplying system of hydrocarbons such as a kind of natural gas.
Background technology
Reduce greenhouse gases CO
2Discharge capacity become the focus that the whole world is paid close attention to, CO
2Reduction of discharging can improve the usage ratio (like wind energy, solar energy, geothermal energy etc.) of regenerative resource through improving the conversion and the utilization ratio of the energy.But in the quite a while from now on, fossil feedstock will be the main use energy, if through from the flue gas of routine burning, separating and capture CO
2, can consume lot of energy, cause the energy efficiency of entire system obviously to reduce.Based on this kind situation, (chemical-looping combustion, CLC) technology has geneogenous capture CO to burning chemistry chains
2Function, and do not need extra energy consumption, thereby be a new technology that realizes the raw material efficient clean utilization, have vast potential for future development.But present burning chemistry chains system adopts reaction temperature up to the recirculating fluidized bed more than 900 ℃ more; The sintering deterioration of the sealing problem of system and oxygen carrier is more serious with the wearing and tearing of flowing under the high temperature; Cause problems such as service life is too short, thereby actual application is not arranged so far yet.
Reduce the CO of combustion of fossil fuel
2Discharging mainly contains two approach: the one, improve efficiency of energy utilization, the 2nd, and from combustion product gases, capture CO
2, and be used, store or seal up for safekeeping.At CO
2Remove in the technology, absorb CO with ammonia spray thermal power station boiler exhaust gas flue gas
2, not only can reach CO
2The purpose that reduces discharging can also obtain the high-quality chemical fertilizer.But, because carbonic hydroammonium can be decomposed into ammonia, water and CO under 60 ℃ the environment temperature being higher than
2, cause CO
2Again return atmosphere, so this CO
2The application of discharge-reducing method also needs further research.CO
2Remove the CO that technology also has CaO carbonating-calcination cycle
2Separation (CCR) technology, polymeric membrane remove CO
2, O
2/ CO
2Circulating combustion technology etc.But often the industrializing implementation cost is higher for above-mentioned technology.
Someone proposed to utilize chemical absorption method Separation and Recovery carbon dioxide from the burnt gas in thermal power plant scheme (please reference: clear former positive height, from generating with reclaiming CO the boiler exhaust
2Test, the energy. resource, the energy. the resource science meeting, 1993, the 14th the volume, the 1st its, the 91-97 page or leaf).According to this scheme, although different with the difference of condition, the Separation and Recovery rate of carbon dioxide can reach more than 80%.Yet, adopt the required energy consumption of traditional chemical absorption method Separation and Recovery carbon dioxide from combustion product gases up to 750～900kcal/kg-CO
2, so the operating cost of Separation and Recovery is very high.
And the technology of secondary or three grades of compression condensations is afterwards adopted in the liquefaction of gaseous carbon dioxide usually.Because the compression of carbon dioxide is undertaken by compressor in this technology, thereby power consumption is bigger.In sum, the CO2 in the traditional combustion mode institute smoke discharging is owing to diluted by a large amount of nitrogen, and its concentration only has 8～15%, thereby the energy consumption and the cost of separation and recovery are very high.
On the other hand, in existing combustion of fossil fuel heating system, especially low pressure steam boiler or hot-water boiler, have very high-grade combustion heat and do not obtain rational gradient utilization.Be used for the Gas Hot Water Boiler System of central heating in winter like northern area, obtain 60～90 ℃ hot water with the combustion heat more than 1000 ℃, so high energy grade is not effectively utilized.
The utility model content
The main purpose of the utility model is, overcomes the defective that existing fuel combustion heating system exists, and a kind of new combustion of natural gas heating system is provided; Technical problem to be solved is to reduce the required operating temperature of chemical chain reaction significantly; And then parallel connection is provided with two burning chemistry chains reactors, realizes that continuous heat supply also improves the thermal efficiency, concentrates and captures carbon dioxide simultaneously; Reduce carbon emission, thereby be suitable for practicality more.
The purpose of the utility model and solve its technical problem and adopt following technical scheme to realize.A kind of combustion of natural gas heating system that proposes according to the utility model comprises: the combustion of natural gas device, and it comprises the first burning chemistry chains reactor and the second burning chemistry chains reactor that two parallel connections are provided with; And the collecting carbonic anhydride device, it is connected in above-mentioned combustion of natural gas device, receives the carbon dioxide of the first burning chemistry chains reactor and second burning chemistry chains reactor discharging.
Preferably, aforesaid combustion of natural gas heating system, described combustion of natural gas device also comprises reforming reactor, this reforming reactor is connected in the said first burning chemistry chains reactor and the second burning chemistry chains reactor through first valve; The described first burning chemistry chains reactor is connected in the collecting carbonic anhydride device through second valve, and the described second burning chemistry chains reactor is connected in the collecting carbonic anhydride device through the 3rd valve.
Preferably, aforesaid combustion of natural gas heating system is provided with first heat exchanger between the described first burning chemistry chains reactor and second valve; Be provided with second heat exchanger between described second burning chemistry chains reactor and the 3rd valve; Be provided with the 3rd heat exchanger between the described reforming reactor and first valve.
Preferably, aforesaid combustion of natural gas heating system, described collecting carbonic anhydride device comprises:
Carbon dioxide absorption tower is connected in the described first burning chemistry chains reactor through second valve, is connected in the described second burning chemistry chains reactor through the 3rd valve;
Carbon dioxide absorption liquid regenerator; Be connected in described carbon dioxide absorption tower; Described carbon dioxide absorption tower also includes reboiler, and the required thermal source of reboiler is provided by the reaction heat of the first burning chemistry chains reactor and/or the second burning chemistry chains reactor;
The water vapor condensation heat exchanger is connected in described carbon dioxide absorption liquid regenerator,
Second gas-liquid separator is connected in described water vapor condensation heat exchanger; And
Carbon dioxide storage tank is connected in described second gas-liquid separator.
Preferably, aforesaid combustion of natural gas heating system also comprises the carbon dioxide condensing heat exchanger in the described carbon dioxide storage tank.
Preferably, aforesaid combustion of natural gas heating system, described combustion of natural gas device also comprises burner, is used for to reforming reactor heat being provided; The exhaust outlet at the top of described carbon dioxide absorption tower is connected in this burner.
Preferably, aforesaid combustion of natural gas heating system, described collecting carbonic anhydride device also comprises second gas-liquid separator, is arranged on carbon dioxide absorption tower and the first burning chemistry chains reactor and the pipeline that the second burning chemistry chains reactor is connected.
Preferably; Aforesaid combustion of natural gas heating system; The combustion of natural gas device also comprises the air input channel; This air input channel is provided with the 4th valve, and the 4th valve is connected to the first burning chemistry chains reactor and the second burning chemistry chains reactor, is used for air is delivered to the first burning chemistry chains reactor or the second burning chemistry chains reactor.
Preferably, aforesaid combustion of natural gas heating system, described first valve, second valve, the 3rd valve and the 4th valve are the three-dimensional switch valve or have a valve sets of switching throughput direction by what two or more valves were formed.
Preferably, aforesaid combustion of natural gas heating system, the described first burning chemistry chains reactor and the second burning chemistry chains reactor are respectively the fixed bed reactors that are built-in with heat exchange jacket.
By technique scheme, the utility model combustion of natural gas heating system has advantage at least:
Native system is a raw material with hydrocarbons such as natural gases; It carries out reforming reaction earlier and produces hydrogen and carbon monoxide; And the product of this reforming reaction has extremely strong reproducibility; So the reduction reaction of oxygen carrier can be carried out under 300-500 ℃ lower temperature, can avoid the carbon distribution and the sintering of oxygen carrier, thereby improve the oxygen carrier life-span.
The chemical chain reaction device of native system is the fixed bed reactors that are built-in with heat exchange jacket, not only can avoid the fluidisation wearing and tearing of oxygen carrier, can also eliminate the hot-spot of oxygen carrier, thereby improve the oxygen carrier life-span.
Native system has the burning chemistry chains reactor of two parallel connections, these two reactors redox reaction of oxygen carrier that can hocket, thus make the whole system can continuous heat supply.
Native system carries out collecting carbonic anhydride and supercharging through the reaction heat of the gradient burning chemistry chains that to utilize high-grade combustion of natural gas heat be natural gas reaction.At this, described reaction heat is not used up drains, though but be converted into grade and significantly reduce the water vapor condensation heat that temperature still is higher than required heat supply temperature and reclaim at the water vapor condensation heat exchanger, thereby can realize heat supply to the user in the same old way.That is, can realize in heat supply that the low energy consumption of carbon dioxide or even zero energy consumption capture.
Through in the utility model, adopting the burning chemistry chains mode; Because the steam dew point of the reaction product gas of burning chemistry chains reactor is very high; Thereby the latent heat of the steam of combustion of natural gas generation can obtain reclaiming basically completely; Thereby the heating efficiency of higher calorific value benchmark is reached more than 90%, thereby the fractional energy savings of more traditional gas fired-boiler can reach more than 10%;
Because the burning chemistry chains process is carried out under 300-500 ℃ lower temperature, thereby produces heating power type NOx hardly, thereby can significantly reduce the discharging of atmosphere pollution material;
Because it is very high that the burning chemistry chains reactor is supplied with the gas concentration lwevel of reaction product gas on absorption tower, make CO
2The conversion ratio of chemical absorbent is high, thereby the utility model chemical absorbing solution regenerative process can under high pressure be carried out.Be the CO that the utility model can obtain supercharging
2Gas is through to CO after the supercharging
2Carry out condensation, liquid CO can be provided simultaneously
2Product.Because carbon dioxide supercharging of the present invention is not to adopt electrically driven (operated) compressor to carry out, thereby the not enough conventional liq CO of power consumption
2Preparation method's 30%, therefore, remarkable in economical benefits.
Above-mentioned explanation only is the general introduction of the utility model technical scheme, in order more to know the technological means of understanding the utility model, and can implement according to the content of specification, below with the preferred embodiment of the utility model and conjunction with figs. specify as after.
Description of drawings
Fig. 1 is the schematic flow sheet of the combustion of natural gas heating system of the utility model.
The specific embodiment
For further setting forth the utility model is to reach technological means and the effect that predetermined purpose is taked; Below in conjunction with accompanying drawing and preferred embodiment; To the specific embodiment, structure, characteristic and the effect thereof of the combustion of natural gas heating system that proposes according to the utility model, specify as after.
Seeing also shown in Figure 1ly, is the combustion of natural gas heating system that the utility model proposes, and it comprises combustion of natural gas device A and collecting carbonic anhydride device B.Said fuel burner A is used for combustion of natural gas, and it comprises reforming reactor 100, the first burning chemistry chains reactor 200, the second burning chemistry chains reactor 300 and burner 800.Said collecting carbonic anhydride device B is used to capture and the carbon dioxide of combustion of natural gas device is originated from supercharging, and it comprises first gas-liquid separator 40, carbon dioxide absorption tower 10, carbon dioxide absorption liquid regenerator 20, reboiler 26, water vapor condensation heat exchanger 31, second gas-liquid separator 32 and carbon dioxide storage tank 33.
Described reforming reactor 100 is used for raw natural gas is carried out reforming reaction, and it can adopt prior art to realize.The first burning chemistry chains reactor 200 and the second burning chemistry chains reactor 300; In oxygen carrier is housed; Be used to carry out the reduction reaction of oxygen carrier or the oxidation of oxygen carrier is a regenerative response; Preferable employing is built-in with the fixed bed reactors of heat exchange jacket 201, heat exchange jacket 301, and chemical chain reaction heat offers reboiler 26 or directly offers the user through heat exchange jacket.Described oxygen carrier is preferably cupric oxide.The described first burning chemistry chains reactor 200 and the second burning chemistry chains reactor 300 are parallel connection setting; The outlet material of described reforming reactor 100 is selected one and is got into the first burning chemistry chains reactor 200 or the second burning chemistry chains reactor 300 under the adjusting of first valve 210; That is to say that at synchronization the outlet material of reforming reactor only gets into a burning chemistry chains reactor.This reforming reactor outlet material pipeline is provided with the 3rd heat exchanger 110 and is used to regulate the material temperature that gets into the first burning chemistry chains reactor or the second burning chemistry chains reactor.Also be connected with first heat exchanger 120 at the first burning chemistry chains reactor 200, this first heat exchanger 120 is used for the heat that the outlet material of the first burning chemistry chains reactor is entrained and offers the user.The air input channel is connected to described first burning chemistry chains reactor and the described second burning chemistry chains reactor 300; On this air input channel, be provided with the 4th valve 220, be used for that air is selected one and flow to the first burning chemistry chains reactor 200 or the second burning chemistry chains reactor 300.Also be connected with second heat exchanger 130 at the second burning chemistry chains reactor 300, this second heat exchanger 130 is used for the heat that the outlet material of the second burning chemistry chains reactor is entrained and offers the user.The outlet conduit of said heat exchanger 120 is provided with second valve 230, under the adjusting of this second valve 230 with this heat exchanger exit mass transport to the first gas-liquid separator 40 or nitrogen exhausting pipeline 250.The outlet conduit of said second heat exchanger 130 is provided with the 3rd valve 240, and the outlet material with this second heat exchanger 130 under the adjusting of the 3rd valve 240 is delivered to first gas-liquid separator 40 or the nitrogen exhausting pipeline 250.Said first gas-liquid separator 40; Be used to separate the material that contains carbon dioxide and water, in this first gas-liquid separator 40, form the bottom that aqueous water is deposited in separator from the first burning chemistry chains reactor 200 or the second burning chemistry chains reactor 300.The condensed water of first gas-liquid separator, 40 bottoms is delivered in the reforming reactor 100 as the required reformation agent of reforming reaction through pipeline and delivery pump 900.
Described burner 8 is that raw material burns with fuel gas and air, is used for providing reforming reaction needed heat to reforming reactor, and wherein a part of fuel then is the residual gas that comes from carbon dioxide absorption tower 10.The combustion of natural gas heating system that the foregoing description proposes all adopts pipeline to connect the conveying that is used for material between wherein each the building block.Described first valve 21, the 4th valve 22, second valve 23 and the 3rd valve 24 have material and switch the function of carrying; Promptly can only with the input mass transport to both direction in one of them; It can be the three-dimensional switch valve; The valve sets that also can be made up of two or more valves is used as long as can realize that handoff functionality to the mass transport direction promptly can be by utility model.
The reforming process of in reforming reactor 1, carrying out comprises the CH of reaction equation (1)
4The CO transformationreation of (natural gas) steam reforming reaction and reaction equation (2):
CH
4(g)+H
2O(g)→CO(g)+3H
2(g)ΔH
298 0＝206kJmol
-1 (1)
CO(g)+H
2O(g)→CO
2(g)+H
2(g)ΔH
298 0＝-41kJmol
-1 (2)
The hocket reduction reaction of oxygen carrier of the first above-mentioned burning chemistry chains reactor 200 and the second burning chemistry chains reactor 300; When one of them burning chemistry chains reactor carries out the oxygen carrier reduction reaction, the oxidation reaction of the oxygen carrier after another burning chemistry chains reactor can be reduced.
The reduction reaction equation of oxygen carrier is following:
H
2(g)+CuO(s)→Cu(s)+H
2O(g) ΔH
298°＝-86.6kJmol
-1 (3)
CO(g)+CuO(s)→Cu(s)+CO
2(g) ΔH
298°＝-127.8kJmol
-1 (4)
The oxidation equation formula of the oxygen carrier after being reduced is following:
Cu(s)+1/2O
2(g)→CuO(s) ΔH
298°＝-155.2kJmol
-1 (5)
That is to say; When first valve 210 switches to the first burning chemistry chains reactor 200 with the reforming reactor outlet material; The 4th valve 220 switches to the second burning chemistry chains reactor 300 with air; Simultaneously second valve 230 switches to first gas-liquid separator, 40, the three valves 240 with the first burning chemistry chains reactor outlet material outlet material of the second burning chemistry chains reactor 300 is switched to nitrogen exhausting pipeline 250.
And when first valve 210 switches to the second burning chemistry chains reactor 300 with the reforming reactor outlet material; The 4th valve 220 switches to the first burning chemistry chains reactor 200 with air; Simultaneously second valve 230 switches to first gas-liquid separator, 40, the three valves 240 with the second burning chemistry chains reactor, 300 outlet materials the outlet material of the first burning chemistry chains reactor 200 is switched to nitrogen exhausting pipeline 250.
Described collecting carbonic anhydride device B is used to collect from the carbon dioxide of fuel burner and makes it obtain supercharging and condensation, forms liquid carbon dioxide.This collecting carbonic anhydride device B comprises first gas-liquid separator 40, carbon dioxide absorption tower 10, carbon dioxide absorption liquid regenerator 20, reboiler 26, water vapor condensation heat exchanger 31, gas-liquid separator 32 and carbon dioxide storage tank 33.
Described carbon dioxide absorption tower 10 is used to absorb the carbon dioxide that originates from fuel burner.Described carbon dioxide absorption tower 10 comprises: at the bottom of the tower 11, be used to hold the absorption rich solution, said absorption rich solution is the carbon dioxide absorption liquid that has absorbed carbon dioxide; Packing layer 12 is arranged on the medium position in this carbon dioxide absorption tower 10, its role is to make carbon dioxide absorption liquid and the gas that gets in the tower that bigger contact surface is arranged; Air supply opening 16 is arranged under the above-mentioned packing layer 12, is used in the absorption tower, providing the CO 2 raw material gas that originates from fuel burner body; Exhaust outlet 15 is arranged on the top of carbon dioxide absorption tower 10, is used to discharge the residual gas (mainly be unreacted natural gas and hydrogen, also have a spot of carbon dioxide) after unstripped gas has been absorbed carbon dioxide, and this residual gas is transported to burner 800.Sprinkling equipment 13 is arranged on the above-mentioned packing layer 12, is used for evenly spraying carbon dioxide absorption liquid.In this absorption tower, carbon dioxide absorption liquid drenches in the absorption tower down from top to bottom, and gas flows from bottom to top, and carbon dioxide absorption liquid contacts with unstripped gas in the entering absorption tower, and absorption carbon dioxide wherein.Be provided with heat exchanger 17 at the bottom of the tower of carbon dioxide absorption tower 10, the heat output, the supply user that produce when being used for absorbing carbon dioxide.Described carbon dioxide absorption liquid is the aqueous solution of the mixture of potash, arsenic trioxide, monoethanolamine, diethanol amine, methyl diethanolamine, amion acetic acid, propene carbonate and NHD one of them or above-mentioned each material.
Described carbon dioxide absorption liquid regenerator 20; Be connected with reboiler 26; The required thermal source of reboiler 26 is provided by the reaction heat of the first burning chemistry chains reactor 200 and/or the second burning chemistry chains reactor 300; The top of carbon dioxide absorption liquid regenerator 20 is provided with sprinkling equipment 23, is connected in the absorption rich solution outlet of 10 bottoms, said absorption tower.Middle part at carbon dioxide absorption liquid regenerator 20 is provided with packing layer 22; Be used to make the absorption rich solution fully to regenerate; The bottom of carbon dioxide absorption liquid regenerator is the 21 absorption lean solutions that are used to hold after the regeneration at the bottom of the tower; Carbon dioxide absorption liquid regenerator 20 tops are provided with exhaust outlet 25, and this exhaust outlet 25 is connected in water vapor condensation heat exchanger 31.Through pipeline the absorption rich solution of carbon dioxide absorption tower bottom is delivered to carbon dioxide absorption liquid regenerator and carries out the regeneration of absorption liquid, form gas and liquid two mutually.The main component of this gas is carbon dioxide and steam, is supplied to water vapor condensation heat exchanger 31 from exhaust outlet output.Said liquid is to absorb lean solution, and the gas concentration lwevel that the absorption lean solution contains because process is regenerated is that the conversion ratio of absorbent reduces greatly.21 be connected at the bottom of through pipeline, will absorb lean solution and deliver in the carbon dioxide absorption tower 10, can be used for absorbing carbon dioxide once more tower with sprinkling equipment 13.Reboiler 26 is used at the bottom of the heating tower absorbent solution in 21, is used for gas and carries to produce a large amount of steam, and keep the temperature in the carbon dioxide absorption liquid regenerator 20, thereby make carbon dioxide absorption liquid at high temperature obtain regeneration.Reboiler 26 adopts the thermal source from heat exchange jacket 201 or heat exchange jacket 301 to heat.Like this; The combustion heat that combustion of natural gas produces is finally from cooling coil 311, first heat exchanger 120, second heat exchanger 130, the 3rd heat exchanger 110 and heat exchanger 17 outputs; Though the temperature of quantity of heat given up is lower than burning chemistry chains reaction temperature and the temperature of supplying with the reboiler heat, but still can satisfy like required 60～90 ℃ such as resident's heating.
Preferable; Can be provided with heat exchanger 24; Be used to make the carbon dioxide absorption liquid of output at the bottom of the tower of carbon dioxide absorption liquid regenerator 20 and at the bottom of carbon dioxide absorption tower 10 towers carbon dioxide absorption liquid of 11 outputs carry out heat exchange, thereby reduce heat required when carrying out the regeneration of carbon dioxide absorption liquid.
Said water vapor condensation heat exchanger 31 is used for the mist of cooled carbon dioxide and steam, and making the water vapor condensation in the mist is aqueous water.In the water vapor condensation heat exchanger, be provided with water vapor condensation cooling coil 311 and cooling coil 312, flowing in the coil pipe has heat transferring medium, exports behind the heat of its absorption mist.The refrigerant of two interior different temperatures that flow of cooling coil; Thereby can under different condensation temperatures, reclaim by the latent heat to steam; The cooling coil 311 of its middle and upper reaches is worked under higher condensation temperature; With the condensation heat that reclaims as thermal source to outside heat supply, and the cooling coil 312 in downstream is worked under lower condensation temperature, is used for that steam is carried out the degree of depth and removes.Said gas-liquid separator 32 is connected in described water vapor condensation heat exchanger 31 through pipeline; Be used to separate aqueous water and carbon dioxide from water vapor condensation heat exchanger 31; The aqueous water that forms is stored in this gas-liquid separator, and isolated carbon dioxide is exported.Said carbon dioxide storage tank 33 is connected in the gas delivery port of said second gas-liquid separator 32; Be used to hold carbon dioxide; In carbon dioxide storage tank 33, be provided with carbon dioxide condensing cooling coil 331, flowing in the coil pipe has refrigerant, exports after the condensation heat of its absorption gaseous carbon dioxide.
Because this combustion of natural gas heating system has two burning chemistry chains reactors, can the hocket redox reaction of oxygen carrier of these two reactors therefore can be continuously to user's heat supply.And when a burning chemistry chains reactor carries out the oxygen carrier reduction reaction, the oxidation reaction of the oxygen carrier after another burning chemistry chains reactor can be reduced, thus guarantee that it can carry out reduction reaction once more.Therefore native system possesses the ability of continuous heat supply.Because use fixed bed as the burning chemistry chains reactor, oxygen carrier need not to flow in reactor, so can avoid oxygen carrier wearing and tearing, the service life of improving oxygen carrier.
In addition; Native system also has the function that carbon dioxide is compressed and liquefied; Can directly obtain liquid carbon dioxide at carbon dioxide storage tank 33; Thereby the carbon emission of native system is reduced significantly, help the alleviation of climate warming more, but also by-product valuable liquid carbon dioxide product simultaneously.
The above; It only is the preferred embodiment of the utility model; Not being that the utility model is done any pro forma restriction, though the utility model with the preferred embodiment exposure as above, yet is not in order to limit the utility model; Anyly be familiar with the professional and technical personnel; In not breaking away from the utility model technical scheme scope, make a little change or be modified to the equivalent embodiment of equivalent variations when the technology contents of above-mentioned announcement capable of using, be the content that does not break away from the utility model technical scheme in every case;, all still belong in the scope of the utility model technical scheme any simple modification, equivalent variations and modification that above embodiment did according to the technical spirit of the utility model.
Claims (10)
1. combustion of natural gas heating system is characterized in that comprising:
The combustion of natural gas device, it comprises the first burning chemistry chains reactor and the second burning chemistry chains reactor that two parallel connections are provided with; And
The collecting carbonic anhydride device, it is connected in above-mentioned combustion of natural gas device, receives the carbon dioxide of the first burning chemistry chains reactor and second burning chemistry chains reactor discharging.
2. combustion of natural gas heating system according to claim 1; It is characterized in that described combustion of natural gas device also comprises reforming reactor, this reforming reactor is connected in the said first burning chemistry chains reactor and the second burning chemistry chains reactor through first valve; The described first burning chemistry chains reactor is connected in the collecting carbonic anhydride device through second valve, and the described second burning chemistry chains reactor is connected in the collecting carbonic anhydride device through the 3rd valve.
3. combustion of natural gas heating system according to claim 2 is characterized in that, is provided with first heat exchanger between the described first burning chemistry chains reactor and second valve; Be provided with second heat exchanger between described second burning chemistry chains reactor and the 3rd valve; Be provided with the 3rd heat exchanger between the described reforming reactor and first valve.
4. combustion of natural gas heating system according to claim 2 is characterized in that, described collecting carbonic anhydride device comprises:
Carbon dioxide absorption tower is connected in the described first burning chemistry chains reactor through second valve, is connected in the described second burning chemistry chains reactor through the 3rd valve;
Carbon dioxide absorption liquid regenerator; Be connected in described carbon dioxide absorption tower; Described carbon dioxide absorption tower also includes reboiler, and the required thermal source of reboiler is provided by the reaction heat of the first burning chemistry chains reactor and/or the second burning chemistry chains reactor;
The water vapor condensation heat exchanger is connected in described carbon dioxide absorption liquid regenerator,
Second gas-liquid separator is connected in described water vapor condensation heat exchanger; And
Carbon dioxide storage tank is connected in described second gas-liquid separator.
5. combustion of natural gas heating system according to claim 4 is characterized in that, also comprises the carbon dioxide condensing heat exchanger in the described carbon dioxide storage tank.
6. combustion of natural gas heating system according to claim 4 is characterized in that, described combustion of natural gas device also comprises burner, is used for to reforming reactor heat being provided; The exhaust outlet at the top of described carbon dioxide absorption tower is connected in this burner.
7. combustion of natural gas heating system according to claim 4; It is characterized in that; Described collecting carbonic anhydride device also comprises first gas-liquid separator, is arranged on carbon dioxide absorption tower and the first burning chemistry chains reactor and the pipeline that the second burning chemistry chains reactor is connected.
8. combustion of natural gas heating system according to claim 2; It is characterized in that; Also comprise the air input channel; This air input channel is provided with the 4th valve, and the 4th valve is connected to the first burning chemistry chains reactor and the second burning chemistry chains reactor, is used for air is delivered to the first burning chemistry chains reactor or the second burning chemistry chains reactor.
9. combustion of natural gas heating system according to claim 8; It is characterized in that described first valve, second valve, the 3rd valve and the 4th valve are the three-dimensional switch valve or have a valve sets of switching throughput direction by what two or more valves were formed.
10. according to each described combustion of natural gas heating system of claim 1-9, it is characterized in that the described first burning chemistry chains reactor and the second burning chemistry chains reactor are respectively the fixed bed reactors that are built-in with heat exchange jacket.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105712348A (en) * | 2016-01-19 | 2016-06-29 | 辽宁石油化工大学 | Carbon dioxide recovery method and carbon dioxide recovery device for achieving zero emission of liquified natural gas |
| US9692069B2 (en) | 2013-03-15 | 2017-06-27 | Ziet, Llc | Processes and systems for storing, distributing and dispatching energy on demand using and recycling carbon |
| CN109193009A (en) * | 2018-09-19 | 2019-01-11 | 中国科学院上海高等研究院 | Solid oxide fuel cell composite system and application method |
-
2012
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9692069B2 (en) | 2013-03-15 | 2017-06-27 | Ziet, Llc | Processes and systems for storing, distributing and dispatching energy on demand using and recycling carbon |
| CN105712348A (en) * | 2016-01-19 | 2016-06-29 | 辽宁石油化工大学 | Carbon dioxide recovery method and carbon dioxide recovery device for achieving zero emission of liquified natural gas |
| CN109193009A (en) * | 2018-09-19 | 2019-01-11 | 中国科学院上海高等研究院 | Solid oxide fuel cell composite system and application method |
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