CN204342755U - Methane at low temperature compression decarbonization device - Google Patents
Methane at low temperature compression decarbonization device Download PDFInfo
- Publication number
- CN204342755U CN204342755U CN201420836849.8U CN201420836849U CN204342755U CN 204342755 U CN204342755 U CN 204342755U CN 201420836849 U CN201420836849 U CN 201420836849U CN 204342755 U CN204342755 U CN 204342755U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- interchanger
- outlet
- thermal medium
- methane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The utility model relates to a kind of device sloughing carbon dioxide in methane, particularly relate to a kind of methane at low temperature compression decarbonization device, comprise compressor (1), air-cooled radiator (2), First Heat Exchanger (3), the second interchanger (4), refrigerator (5) and high pressure storage tank (6), described First Heat Exchanger (3) and the second interchanger (4) are equipped with thermal medium entrance, thermal medium outlet, cold medium inlet, cold media outlet four ports.The utility model equipment used comparatively small amt, reduces the operating maintenance cost of each parts; Decarburization effect stability, reliable, need not additional chemical absorption material and physical adsorption material, decrease investment; Floor space is little, and the scale according to the project of operation rationally determines each interchanger, tank body size, the minimizing floor space of energy maximum efficiency.
Description
Technical field
The utility model relates to a kind of device sloughing carbon dioxide in methane, particularly relates to a kind of methane at low temperature compression decarbonization device.
Background technology
Main in prior art exist following several middle decarbonization device:
1, carbon dioxide plant is removed in absorption refining, utilizes By Amine Solutions (primary amine, secondary amine, tertiary amine, sterically hindered amines etc.) and the physical chemistry absorption characteristic of carbonic acid gas to realize.The relative merits of this device: although this kind of device just can be relatively low, easy and simple to handle to very high degree, the disposable input of equipment by the CO 2 refining in gas under not too high pressure.But just no longer there is the characteristic of absorbing carbon dioxide after chemical absorber complete reaction is complete, so the receptivity of chemical absorber is limited.In equipment running process, self thermal losses is relatively high.Need a large amount of purification work water in reaction, after reacting completely, there is liquid waste disposal problem, and conventional absorption agent organic amine also exists toxicity to a certain extent, be unfavorable for the carbonic acid gas recycling absorbed.
2, pressure-variable adsorption removes carbon dioxide plant (PSA), utilize sorbent material (as molecular sieve etc.) to the selective adsorption feature of carbonic acid gas, namely carbonic acid gas has higher separation factor relative to other gaseous components on the sorbent, reaches the object removed carbon dioxide in methane.The relative merits of this device: this kind of device removes carbonic acid gas without the need to additional chemical agent and work water, and reaction process is without the need to the heat energy that works.Equipment self energy consumption is lower, and device structure is mainly based on container-type, and be easy to transport, installment and debugging, system operation reliability is high, is relatively applicable to large-sized biogas purification engineering, and after purifying gas without the need to dry and pressurization.But require relatively high to unstripped gas before purifying, need dewater drying and thoroughly sulphur removal, and in purge process, gas consumption is comparatively large, generally can cause the waste of gas 3%-8%.Need after reacting completely to set up flare system.The disposable input of technical equipment system complex, equipment is high, system cloud gray model expense and maintenance cost high.
3, membrane sepn is purified and is removed carbon dioxide plant, utilize gas with various component to be realized by the difference of membrane permeability effect under pressure-driven, the seepage velocity of normal conditions carbon dioxide is fast, as fast gas to discharge through gas, the seepage velocity of methane is slow, obtains refined product gas as slow gas with saturating residual air form.The relative merits of this device: membrane sepn decarbonization device cost of investment is moderate, film can continue use 3 years, but shows that because atrophy, membrane permeability can reduce 30% after use a year and a half through experience.Due to the many impacts by many factors such as mould material, gas composition, pressure reduction, separation factor and temperature of gas delivery efficiency, and require higher to the degree of cleaning of unstripped gas, unstripped gas needs desulfurization, purification, dedusting before the system of entering.Membrane module is expensive, and the film that uses in membrane separation process needs often to change, and running cost is higher, and therefore gaseous jet simulation method is not generally used alone, the process integration uses such as normal and solvent absorbing, pressure-variable adsorption, low temperature separation process, pervaporation.
4, high-pressure washing device decarbonation is the difference utilizing carbonic acid gas solubleness and methane in water, realizes being separated of carbonic acid gas and methane by physical absorption process.Usual biogas enters after compression bottom absorption column, and water enters from top and carries out Flow Injection Chemiluminescence Method absorption.The relative merits of this device: this kind of device removes carbonic acid gas without the need to using additional chemical agent, without the need to thorough sulphur removal before purifying, without the need to pressurization after purifying, system self consumes energy, thermal losses is lower, the disposable input of equipment is moderate, system cloud gray model expense and maintenance cost moderate, and serviceability is high.But this kind of device absorption process needs large-scale purification process water, for improving the solubleness of carbonic acid gas in water, water washing device decarburization generally adopts elevated pressures, so also needs washing water to pressurize, increases energy consumption.In addition, in the water after reacting completely, H2S concentration is higher, and after purifying, gas need carry out dewater drying and off gas treatment, technical equipment system complex, and the waste water of generation need recycle.
Utility model content
The purpose of this utility model is to provide a kind of methane at low temperature to compress decarbonization device, solves that existing decarbonization device energy consumption is large, complex structure and the high problem of decarburization cost.
For solving the problem, technical solution adopted in the utility model is:
A kind of methane at low temperature compression decarbonization device, comprise compressor, air-cooled radiator, First Heat Exchanger, the second interchanger, refrigerator and high pressure storage tank, described First Heat Exchanger and the second interchanger are equipped with thermal medium entrance, thermal medium outlet, cold medium inlet, cold media outlet four ports, the outlet of described compressor is connected to the entrance of air-cooled radiator, the outlet of air-cooled radiator is connected to the thermal medium entrance of First Heat Exchanger, the cold media outlet of First Heat Exchanger is connected to the transport pipe of gaseous carbon dioxide, the thermal medium outlet of First Heat Exchanger is connected to the thermal medium entrance of the second interchanger, the thermal medium outlet of the second interchanger is connected to the biogas entrance of high pressure storage tank, refrigerator is connected to the cold medium inlet of the second interchanger and cold media outlet by pipeline, high pressure storage tank is provided with gaseous methane outlet and liquid carbon dioxide outlet, wherein the liquid carbon dioxide outlet of high pressure storage tank is connected to the cold medium inlet of First Heat Exchanger by carbonic acid gas transport pipe and reducing valve.
Further technical scheme is, the thermal medium entrance on described First Heat Exchanger and cold media outlet are arranged on the drift angle place, side of First Heat Exchanger, and thermal medium outlet and cold medium inlet are arranged on the opposite side base angle place of First Heat Exchanger; The thermal medium entrance of described second interchanger and cold media outlet are arranged on the drift angle place, side of the second interchanger, and thermal medium outlet and cold medium inlet are arranged on the opposite side base angle place of the second interchanger.
Further technical scheme is, described compressor is A22.5-11 compressor, and described First Heat Exchanger and the second interchanger are M3-M45L type heat exchanger, described refrigerator power 22KW.
The beneficial effect adopting technique scheme to produce is: the utility model equipment used comparatively small amt, reduces the operating maintenance cost of each parts; Decarburization effect stability, reliable, need not additional chemical absorption material and physical adsorption material, decrease investment; Floor space is little, and the scale according to the project of operation rationally determines each interchanger, tank body size, the minimizing floor space of energy maximum efficiency.
Accompanying drawing explanation
Fig. 1 is the connection diagram of the utility model methane at low temperature compression decarbonization device.
Embodiment
In order to make the purpose of this utility model, technical scheme and advantage clearly understand, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein only in order to explain the utility model, and be not used in restriction the utility model.
Fig. 1 shows an embodiment of the utility model methane at low temperature compression decarbonization device: a kind of methane at low temperature compression decarbonization device, comprise compressor 1, air-cooled radiator 2, First Heat Exchanger 3, second interchanger 4, refrigerator 5 and high pressure storage tank 6, described First Heat Exchanger 3 and the second interchanger 4 are equipped with thermal medium entrance a, thermal medium outlet b, cold medium inlet c, cold media outlet d tetra-ports, the outlet of described compressor 1 is connected to the entrance of air-cooled radiator 2, the outlet of air-cooled radiator 2 is connected to the thermal medium entrance of First Heat Exchanger 3, the cold media outlet of First Heat Exchanger 3 is connected to the transport pipe of gaseous carbon dioxide, the thermal medium outlet of First Heat Exchanger 3 is connected to the thermal medium entrance of the second interchanger 4, the thermal medium outlet of the second interchanger 4 is connected to the biogas entrance of high pressure storage tank 6, refrigerator 5 is connected to the cold medium inlet of the second interchanger 4 and cold media outlet by pipeline, high pressure storage tank 6 is provided with gaseous methane outlet and liquid carbon dioxide outlet, wherein the liquid carbon dioxide outlet of high pressure storage tank 6 is connected to the cold medium inlet of First Heat Exchanger 3 by carbonic acid gas transport pipe and reducing valve.
According to a preferred embodiment of the utility model methane at low temperature compression decarbonization device, thermal medium entrance on described First Heat Exchanger 3 and cold media outlet are arranged on the drift angle place, side of First Heat Exchanger 3, and thermal medium outlet and cold medium inlet are arranged on the opposite side base angle place of First Heat Exchanger 3; The thermal medium entrance of described second interchanger 4 and cold media outlet are arranged on the drift angle place, side of the second interchanger 4, and thermal medium outlet and cold medium inlet are arranged on the opposite side base angle place of the second interchanger 4.
For a kind of methane-generating pit of 1200 cubes of patterns of scale, selected model can be, described compressor 1 is A22.5-11 compressor, and described First Heat Exchanger 3 and the second interchanger 4 are M3-M45L type heat exchanger, described refrigerator 5 power 22KW.
Workflow of the present utility model is:
The compressor 1 of biogas after desulfurization through being interconnected becomes high temperature and high pressure gas, be connected with air-cooled radiator 2 and lower the temperature in advance, biogas after pre-cooling enters First Heat Exchanger 3 from the thermal medium entrance of First Heat Exchanger 3, and flow out through the thermal medium outlet of First Heat Exchanger 3, high pressure gas after outflow enter the second interchanger 4 from the thermal medium entrance of the second interchanger 4 by the road, and flow out through the thermal medium outlet of the second interchanger 4, cold medium inlet and the cold media outlet of the second interchanger 4 are all connected to refrigerator 5, biogas in second interchanger 4 is lowered the temperature again, the cryogenic high pressure biogas formed after twice heat exchange enters in high pressure storage tank, gaseous methane is isolated in top, below condenses out liquid carbon dioxide, the liquid carbon dioxide condensed out is back to First Heat Exchanger 3 through reducing valve decompress(ion), and be connected with the cold medium inlet of First Heat Exchanger 3, in First Heat Exchanger 3, heat absorption becomes gaseous carbon dioxide, flow out from cold media outlet.
The utility model equipment used comparatively small amt, only need compressor, scatterer, interchanger, high pressure storage tank, expansion valve, connecting pipeline and control valve, thus reduce the operating maintenance cost of each parts, decarburization effect stability, reliable, need not additional chemical absorption material and physical adsorption material, decrease investment; Floor space is little, and the scale according to the project of operation rationally determines each interchanger, tank body size, the minimizing floor space of energy maximum efficiency.
Although be described the utility model with reference to multiple explanatory embodiment of the present utility model here, but, should be appreciated that, those skilled in the art can design a lot of other amendment and embodiment, these amendments and embodiment will drop within spirit disclosed in the present application and spirit.More particularly, in the scope of, accompanying drawing open in the application and claim, multiple modification and improvement can be carried out to the building block of subject combination layout and/or layout.Except the distortion carried out building block and/or layout and improving, to those skilled in the art, other purposes also will be obvious.
Claims (3)
1. a methane at low temperature compression decarbonization device, it is characterized in that: comprise compressor (1), air-cooled radiator (2), First Heat Exchanger (3), the second interchanger (4), refrigerator (5) and high pressure storage tank (6), described First Heat Exchanger (3) and the second interchanger (4) are equipped with thermal medium entrance, thermal medium outlet, cold medium inlet, cold media outlet four ports, the outlet of described compressor (1) is connected to the entrance of air-cooled radiator (2), the outlet of air-cooled radiator (2) is connected to the thermal medium entrance of First Heat Exchanger (3), the cold media outlet of First Heat Exchanger (3) is connected to the transport pipe of gaseous carbon dioxide, the thermal medium outlet of First Heat Exchanger (3) is connected to the thermal medium entrance of the second interchanger (4), the thermal medium outlet of the second interchanger (4) is connected to the biogas entrance of high pressure storage tank (6), refrigerator (5) is connected to the cold medium inlet of the second interchanger (4) and cold media outlet by pipeline, high pressure storage tank (6) is provided with gaseous methane outlet and liquid carbon dioxide outlet, wherein the liquid carbon dioxide outlet of high pressure storage tank (6) is connected to the cold medium inlet of First Heat Exchanger (3) by carbonic acid gas transport pipe and reducing valve.
2. methane at low temperature compression decarbonization device according to claim 1, it is characterized in that: the thermal medium entrance on described First Heat Exchanger (3) and cold media outlet are arranged on the drift angle place, side of First Heat Exchanger (3), thermal medium outlet and cold medium inlet are arranged on the opposite side base angle place of First Heat Exchanger (3); The thermal medium entrance of described second interchanger (4) and cold media outlet are arranged on the drift angle place, side of the second interchanger (4), and thermal medium outlet and cold medium inlet are arranged on the opposite side base angle place of the second interchanger (4).
3. methane at low temperature compression decarbonization device according to claim 1, it is characterized in that: described compressor (1) is A22.5-11 compressor, described First Heat Exchanger (3) and the second interchanger (4) are M3-M45L type heat exchanger, described refrigerator (5) power 22KW.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420836849.8U CN204342755U (en) | 2014-12-26 | 2014-12-26 | Methane at low temperature compression decarbonization device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420836849.8U CN204342755U (en) | 2014-12-26 | 2014-12-26 | Methane at low temperature compression decarbonization device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204342755U true CN204342755U (en) | 2015-05-20 |
Family
ID=53226039
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420836849.8U Expired - Fee Related CN204342755U (en) | 2014-12-26 | 2014-12-26 | Methane at low temperature compression decarbonization device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204342755U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108151442A (en) * | 2017-12-04 | 2018-06-12 | 中国科学院理化技术研究所 | Low-temperature preparation system for L NG in raw material gas |
-
2014
- 2014-12-26 CN CN201420836849.8U patent/CN204342755U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108151442A (en) * | 2017-12-04 | 2018-06-12 | 中国科学院理化技术研究所 | Low-temperature preparation system for L NG in raw material gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2023061507A1 (en) | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by means of chemical method and psa method | |
| CN101584960A (en) | Separator and separation and purification method of gas-liquid phase absorbing membrane | |
| Liu et al. | Simulation and energy analysis of CO2 capture from CO2-EOR extraction gas using cryogenic fractionation | |
| US20140134695A1 (en) | Integrated hybrid membrane/absorption process for co2 capture and utilization | |
| RU2012130089A (en) | SEPARATION OF AMMONIA AFTER SEPARATION OF CO2 FROM GAS FLOW | |
| CN103357250A (en) | Facility and process for collecting carbon dioxide and/or hydrogen sulfide from gas mixture | |
| Huang et al. | Hybrid physical-chemical absorption process for carbon capture with strategy of high-pressure absorption/medium-pressure desorption | |
| CA2964096A1 (en) | Energy efficient solvent regeneration process for carbon dioxide capture | |
| CN111871171A (en) | Carbon dioxide capture system based on coupling membrane separation method and chemical absorption method | |
| CN201168557Y (en) | Flue gas processing system | |
| CN106731494B (en) | Desorb the process of air lift coupled and pressurizing absorption purification biogas | |
| CN1300635A (en) | Process for removing CO2 and H2S from biological gas | |
| CN204342755U (en) | Methane at low temperature compression decarbonization device | |
| CN105498449B (en) | A kind of CO2Absorbent solution | |
| CN201899968U (en) | Oil gas recovery device combining condensation method with adsorption method | |
| CN206823471U (en) | A kind of MDEA biogas energy-saving decarbonation device | |
| CN103159580B (en) | Method of purifying and extracting methane in waste landfill gas | |
| CN204779511U (en) | Marsh gas desulfurization removes carbon purification natural gas system | |
| CN204891549U (en) | Natural gas desulfurization decarbonization system of coupling sour gas concentration | |
| CN202666657U (en) | Facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture | |
| CN203829859U (en) | Waste gas dust purifying and recovering tower | |
| CN104998517A (en) | Method for increasing concentrations of acid gas hydrogen sulfide and carbonyl sulfide in low-temperature methanol washing process | |
| CN203333608U (en) | Marsh gas purification system | |
| CN211302579U (en) | A waste gas treatment system for VOCs retrieves | |
| CN202297145U (en) | Carbon dioxide purification device integrated with synthetic gas desulfurization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150520 Termination date: 20161226 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |