CN201377962Y - Equipment producing compressed natural gas from mixed gas containing methane - Google Patents
Equipment producing compressed natural gas from mixed gas containing methane Download PDFInfo
- Publication number
- CN201377962Y CN201377962Y CN200920107339U CN200920107339U CN201377962Y CN 201377962 Y CN201377962 Y CN 201377962Y CN 200920107339 U CN200920107339 U CN 200920107339U CN 200920107339 U CN200920107339 U CN 200920107339U CN 201377962 Y CN201377962 Y CN 201377962Y
- Authority
- CN
- China
- Prior art keywords
- gas
- natural gas
- heat exchanger
- liquefied natural
- high pressure
- 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 - Lifetime
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 239000007789 gas Substances 0.000 title claims abstract description 70
- 239000003345 natural gas Substances 0.000 title claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 30
- 238000005057 refrigeration Methods 0.000 claims abstract description 19
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000012530 fluid Substances 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000011049 filling Methods 0.000 abstract description 2
- 238000002309 gasification Methods 0.000 abstract description 2
- 238000010792 warming Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 12
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- -1 n-formyl sarcolysine alkane Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000013526 supercooled liquid Substances 0.000 description 1
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses equipment producing compressed natural gas from mixed gas containing methane, comprising a refrigeration device, a mixed gas containing methane separation device, a cryogenic liquid pump and a high-pressure heat exchanger. Mixed gas containing methane becomes liquefied natural gas after sequentially entering the refrigeration device and the mixed gas containing methane separation device, and then enters the cryogenic liquid pump for pressurization to become high-pressure liquefied natural gas. After entering the high-pressure heat exchanger for re-warming gasification, the high-pressure liquefied natural gas directly becomes a compressed natural gas product for storage and filling, so a complex device using a compressor to compress and cool low-pressure natural gas into the compressed natural gas is saved. The purity of the compressed natural gas product obtained by the equipment can reach over 99.8%, the whole set equipment is simple, and the operation is easy.
Description
Technical field
The utility model relates to the separation equipment that is particularly useful for containing methane blended gas.
Background technology
CNG (Compressed Natural Gas, i.e. compressed natural gas) is natural gas pressurization (general pressure surpasses 16MPa) and is stored in the pressure vessel with gaseous form.CNG can be used as the motor vehicle fuel utilization.In various alternative fuel for cars, natural gas is the desirable clean fuel of automobile, and it has the advantage on resource, environmental protection, economy and safety.The present ratio maximum that accounts for the CNG automobile of gas-fueled vehicles in the world, its technology is also ripe, and environment and economic benefit are all good.In addition, CNG also can be used as natural gas peak-shaving, is using the CNG peak regulation very steady with the gas peak, and the pressure of pipe network can be guaranteed.Because China is in processes such as industrial production and energy extraction, can produce quantity very huge contain methane blended gas, as coke-stove gas, Device in Gas (coalbed methane containing oxygen) etc., wherein most of conduct " waste gas " is discharged or directly burns, with the coke-stove gas is example, and annual China will burn two " West-east Gas at least.If can utilize composition from these " waste gas ", to extract in methane etc. and be used, then can effectively solve the dual problem of energy supply safety, ecological environmental protection, play a significant role for realizing sustainable development economic and society.
Chinese patent ZL200620115881.2 discloses a kind of liquefaction device that contains the air coal bed gas, comprise the compression cleaning equipment, refrigeration plant and liquefaction separation equipment, carry out operations such as dedusting, compression, dehydration by the compression cleaning equipment, enter refrigeration plant then and freeze, enter the liquefaction separation equipment at last and fractionate out liquefied natural gas.It can produce liquefied natural gas from coal bed gas, but can not directly produce CNG.
The utility model content
The purpose of this utility model provides a kind of separation equipment, and it can directly produce CNG from contain methane blended gas.
To achieve these goals, basic design of the present utility model is, adopt the method for low-temperature liquefaction rectifying, methane liquefied from promptly contain methane blended gas separate, with cryogenic liquid pump liquefied natural gas (LNG) is forced into 6 to more than the 30MPa again, become highly pressurised liquid, becoming gases at high pressure after the highly pressurised liquid re-heat is the CNG product, enters high-pressure bottle and stores for use.
Technical scheme as realizing that the present invention conceives substantially provides a kind of equipment of producing compressed natural gas from contain methane blended gas, comprising: refrigerating plant, and the described methane blended gas that contains is cooled in described refrigerating plant and produces gas-liquid mixture; What comprise fractionating column contains the methane blended air separation, described fractionating column is used for isolating liquefied natural gas from described gas-liquid mixture, and has the inlet of the described gas-liquid mixture of input and the bottom liquid outlet that top gas exported and be used to discharge liquefied natural gas; The described equipment of producing compressed natural gas also comprises the cryogenic liquid pump and the high pressure heat exchanger of the inlet that has outlet and link to each other with the outlet of the bottom liquid of described fractionating column, and described cryogenic liquid pump will be from the liquefied natural gas pressurized delivered of described fractionating column described high pressure heat exchanger extremely.
As another preferred version of technique scheme, also comprise the reboiler between the inlet of the bottom liquid outlet that is arranged on described fractionating column and described cryogenic liquid pump, be used to heat inflow liquefied natural gas wherein, so that the purity of raising liquefied natural gas.
As another preferred version of technique scheme, also comprise the subcooler between the inlet of the outlet that is arranged on described reboiler and described cryogenic liquid pump, be used to cool off inflow liquefied natural gas wherein.
As another preferred version of technique scheme, also comprise the condenser between the top gas outlet that is arranged on described fractionating column and the described subcooler, be used for the condensation inflow wherein contain methane blended gas.
As another preferred version of technique scheme, described refrigerating plant comprises gas swell refrigeration device or mixed working fluid refrigerating plant, and wherein gas swell refrigeration device comprises heat exchanger.
As another preferred version of technique scheme, tail gas discharged is by the heat exchanger of described refrigerating plant, for described heat exchanger provides cold from described subcooler.
As another preferred version of technique scheme, described high pressure heat exchanger with contain the methane blended gas phase and be communicated with, for described high pressure heat exchanger provides hot fluid.
As another preferred version of technique scheme, described high pressure heat exchanger is communicated with the refrigeration gas phase, for described high pressure heat exchanger provides hot fluid.
The obtained beneficial effect of the utility model is: supercharging becomes high pressure LNG through cryogenic pump the method that adopts low-temperature liquefaction to separate is separated methane from contain methane blended gas after; High pressure LNG enters high pressure heat exchanger rewarming gasification back just directly becomes the CNG product, can be for storing and filling usefulness, save with compressor with the low pressure natural gas compression and be cooled to the complex appts of CNG.The CNG product purity of using this equipment to obtain can reach more than 99.8%, and complete equipment is simple, easy to operate.
Description of drawings
Below in conjunction with the drawings and specific embodiments the utility model is described in further detail.
Fig. 1 is a schematic flow sheet of producing CNG among the utility model embodiment.
The specific embodiment
Equipment of the present utility model mainly comprises refrigerating plant, unstripped gas (promptly containing methane blended gas) separator, LNG supercharging equipment and high pressure heat exchanger.Described refrigerating plant comprises two kinds of gas (nitrogen or n-formyl sarcolysine alkane gaseous mixture) swell refrigeration device and mixed working fluid refrigerating plants, wherein simple to operate, the small investment of gas swell refrigeration device, energy consumption are moderate, mainly comprise units such as refrigerant gas compressor, multi-channel heat exchanger, high pressure heat exchanger, booster expansion turbine; The mixed working fluid refrigerating plant is simple to operate, energy consumption is low, investment is moderate, mainly comprises units such as mixed working fluid compressor, gas-liquid separator, multi-channel heat exchanger, high pressure heat exchanger, cryogenic throttle valve.The described methane blended air separation that contains mainly comprises fractionating column, fractionation tower bottom reboiler, also can be according to actual conditions choosing dress overhead condenser.Described LNG supercharging equipment is a special low temperature liquid pump, as required LNG is pressurized to more than 6～30Mpa.
In the utility model, containing methane blended gas is the mist of methane content (percent by volume) between 10%～95%.The gaseous mixture that exceeds this scope is as if this equipment of employing, or economy is not good, or is not suitable for this equipment.
Contain methane blended gas for through the clean gas after the purified treatment and be applicable to low temperature environment in the utility model.Purification process comprises dehydration, takes off CO
2, desulfurization, demercuration, take off benzene and aromatic hydrocarbon, take off naphthalene and remove other high-boiling-point impurity component or the like.
Refrigerating plant adopts gas swell refrigeration device in the present embodiment, to containing the separation of liquefying of methane blended gas.Technological process is as follows:
Consult the schematic flow sheet that compressed natural gas CNG is produced in the circulation of gas swell refrigeration among Fig. 1, the methane blended gas A that contains after the purification enters heat exchanger 1,2 heat-shifts successively, cooled off by cold fluid, temperature reduces step by step, after coming out from heat exchanger 2, contain the methane liquefy substantially in the methane blended gas this moment.Enter fractionating column 3 then, liquid flows from top to bottom, and gas flows from bottom to top.More down, the methane content in the liquid is high more, and more up, the methane content in the gas is low more.After liquid flows at the bottom of the tower, enter the reboiler 5 at the bottom of the tower, and the low boiling component of trace in the liquid (relevant with feed gas composition, as O
2, N
2, CO, H
2Deng) be heated further flash distillation and come out, make the liquefied natural gas LNG purity of coming out further improve from fractionating column, can reach more than 99.8%.Enter subcooler 6 afterwards, the gas that is come out from cat head further cools off, and becomes supercooled liquid natural gas LNG.The liquefied natural gas LNG that crosses after cold enters cryogenic liquid pump 7, is pressurized to 6 to more than the 30MPa.The high-pressure liquefaction natural gas enters high pressure heat exchanger 8, with the hot fluid heat-shift, becomes gases at high pressure, i.e. compressed natural gas CNG product stores after going out system.From subcooler 6 rewarming tail gas discharged B, enter heat exchanger 2,1 successively, for system provides cold, go out system at last.
The gas that comes out from a column plate (or filler top) topmost can directly go out fractionating column and enter subcooler 6 rewarmings.Also can enter overhead condenser 4 as shown in Figure 1, further liquefaction, liquid is back to fractionating column 3 and makes phegma, and gas (tail gas) removes subcooler 6 after going out condenser 4.So, trace methane can be got off by further condensation in the gas, improved the recovery rate of methane, but energy consumption can increase to some extent.
Hot fluid with the high-pressure liquefaction heat exchange gas in heat exchanger 8 can be a refrigeration gas, also can be unstripped gas, can be according to the requirements of process adjustment, and in this example, hot fluid is refrigeration gas.As shown in Figure 1, after refrigeration gas C (as nitrogen) cools off through compressor 9 compressions, aftercooler 10, enter the 11 further superchargings of turbo-expander pressurized end then, through aftercooler 12 coolings, be divided into two-way then: the one tunnel enters high pressure heat exchanger 8 and LNG heat-shift; One the tunnel enters heat exchanger 1 and cold fluid heat exchange.Converge after the air cooling of two-way refrigeration but goes out heat exchanger, enter the expanding end 13 of turbo-expander then, become the gas of low-temp low-pressure after the expansion.Enter the cold junction of heat exchanger 2,1 afterwards successively, come out after cold is provided, enter compressor 9 compressions, supercharging, cooling, expansion, refrigeration again, so circulation for system.
Of particular note: schematic flow sheet shown in Figure 1 is not a fixed mode, can adjust with cold proportioning situation according to actual needs.As whether the fractionation cat head being added in the condenser, high pressure heat exchanger 8 the hot fluids gas of walking to freeze still is whether subcooler etc. to be set before unstripped gas, the cryogenic liquid pump make up arbitrarily.
Claims (8)
1. equipment of producing compressed natural gas from contain methane blended gas comprises:
Refrigerating plant, the described methane blended gas that contains is cooled in described refrigerating plant and produces gas-liquid mixture;
What comprise fractionating column contains the methane blended air separation, described fractionating column is used for isolating liquefied natural gas from described gas-liquid mixture, and has the inlet of the described gas-liquid mixture of input and the bottom liquid outlet that top gas exported and be used to discharge liquefied natural gas;
It is characterized in that, described equipment also comprises the cryogenic liquid pump and the high pressure heat exchanger of the inlet that has outlet and link to each other with the outlet of the bottom liquid of described fractionating column, and described cryogenic liquid pump will be from the liquefied natural gas pressurized delivered of described fractionating column described high pressure heat exchanger extremely.
2. equipment according to claim 1, it is characterized in that, also comprise the reboiler between the inlet of the bottom liquid outlet that is arranged on described fractionating column and described cryogenic liquid pump, be used to heat inflow liquefied natural gas wherein, so that the purity of raising liquefied natural gas.
3. equipment according to claim 2 is characterized in that, also comprises the subcooler between the inlet of the outlet that is arranged on described reboiler and described cryogenic liquid pump, is used to cool off inflow liquefied natural gas wherein.
4. equipment according to claim 3 is characterized in that, also comprises the condenser between the top gas outlet that is arranged on described fractionating column and the described subcooler, be used for the condensation inflow wherein contain methane blended gas.
5. equipment according to claim 4 is characterized in that, described refrigerating plant comprises gas swell refrigeration device or mixed working fluid refrigerating plant, and wherein gas swell refrigeration device comprises heat exchanger.
6. equipment according to claim 5 is characterized in that, tail gas discharged is by the heat exchanger of described refrigerating plant, for described heat exchanger provides cold from described subcooler.
7. equipment according to claim 6 is characterized in that, described high pressure heat exchanger with contain the methane blended gas phase and be communicated with, for described high pressure heat exchanger provides hot fluid.
8. equipment according to claim 6 is characterized in that, described high pressure heat exchanger is communicated with the refrigeration gas phase, for described high pressure heat exchanger provides hot fluid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200920107339U CN201377962Y (en) | 2009-04-14 | 2009-04-14 | Equipment producing compressed natural gas from mixed gas containing methane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200920107339U CN201377962Y (en) | 2009-04-14 | 2009-04-14 | Equipment producing compressed natural gas from mixed gas containing methane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201377962Y true CN201377962Y (en) | 2010-01-06 |
Family
ID=41518077
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200920107339U Expired - Lifetime CN201377962Y (en) | 2009-04-14 | 2009-04-14 | Equipment producing compressed natural gas from mixed gas containing methane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201377962Y (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102141317A (en) * | 2011-03-16 | 2011-08-03 | 浙江大学 | Rectification-type self-overlaying gas liquefying system |
| CN103033025A (en) * | 2011-09-30 | 2013-04-10 | 新地能源工程技术有限公司 | Industrial arts for dehydrogenation and denitrogen and de-carbon monoxide from high methane gas and liquefied natural gas production |
| CN105627693A (en) * | 2016-03-11 | 2016-06-01 | 重庆耐德能源装备集成有限公司 | Natural gas treatment device and method |
| CN105987579A (en) * | 2015-02-02 | 2016-10-05 | 上海宝钢气体有限公司 | Method for simultaneously preparing compressed natural gas and liquefied natural gas from methane mixed gas |
-
2009
- 2009-04-14 CN CN200920107339U patent/CN201377962Y/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102141317A (en) * | 2011-03-16 | 2011-08-03 | 浙江大学 | Rectification-type self-overlaying gas liquefying system |
| CN102141317B (en) * | 2011-03-16 | 2012-07-25 | 浙江大学 | Rectification-type self-overlaying gas liquefying system |
| CN103033025A (en) * | 2011-09-30 | 2013-04-10 | 新地能源工程技术有限公司 | Industrial arts for dehydrogenation and denitrogen and de-carbon monoxide from high methane gas and liquefied natural gas production |
| CN103033025B (en) * | 2011-09-30 | 2015-02-18 | 新地能源工程技术有限公司 | Industrial arts for dehydrogenation and denitrogen and de-carbon monoxide from high methane gas and liquefied natural gas production |
| CN105987579A (en) * | 2015-02-02 | 2016-10-05 | 上海宝钢气体有限公司 | Method for simultaneously preparing compressed natural gas and liquefied natural gas from methane mixed gas |
| CN105987579B (en) * | 2015-02-02 | 2018-09-04 | 上海宝钢气体有限公司 | The method for producing compressed natural gas and liquefied natural gas simultaneously from methane mixed gas |
| CN105627693A (en) * | 2016-03-11 | 2016-06-01 | 重庆耐德能源装备集成有限公司 | Natural gas treatment device and method |
| CN105627693B (en) * | 2016-03-11 | 2019-03-01 | 重庆耐德能源装备集成有限公司 | A kind of processing unit and method of natural gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102115684B (en) | Method for producing liquefied natural gas by using coke oven gas | |
| CN102538398B (en) | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) | |
| CA2836628C (en) | Process for liquefaction of natural gas | |
| CN101033910B (en) | System for integrating air separation with cool capacity recovery of liquefied natural gas | |
| CN101968298B (en) | Separation and recovery device and method for argon and methane in synthetic ammonia relief gas | |
| CN102374754B (en) | The Apparatus and method for of liquified natural gas and carbon monoxide is produced from coke-stove gas | |
| CN103175381B (en) | Low concentration coal-bed gas produces LNG technique containing oxygen cryogenic liquefying | |
| CN104528647A (en) | Method and device for preparing hydrogen and high-purity carbon monoxide by separating synthetic gas | |
| CN101688753B (en) | Method and device for separating mixture of hydrogen, methane and carbon monoxide by cryogenic distillation | |
| CN101899342B (en) | Process for producing liquefied natural gas by coal bed gas in mine coal | |
| CN201377962Y (en) | Equipment producing compressed natural gas from mixed gas containing methane | |
| CN102435045A (en) | Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof | |
| CN101709238A (en) | Method for preparing liquefied natural gas by using coke-oven gas | |
| CN103175380B (en) | Low concentration coal-bed gas produces LNG device containing oxygen cryogenic liquefying | |
| CN105135820A (en) | Method and system for manufacturing LNG through gas containing air | |
| CN202382518U (en) | Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas) | |
| CN204702504U (en) | A kind of synthetic gas is separated hydrogen making and high-purity CO device | |
| CN101709237B (en) | Method for preparing liquefied natural gas by using coke-oven gas | |
| CN105157348B (en) | The liquid nitrogen washing device and its method of a kind of recovery LNG | |
| CN212538461U (en) | Take multistage separation to be applicable to propane recovery unit of super rich gas | |
| CN202470622U (en) | Purifying, separating and liquefying system for nitrogen-oxygen-containing coal-mine gas | |
| CN114165987A (en) | Liquid carbon dioxide production device and production method thereof | |
| CN108036585B (en) | Heat pump air separation system for LNG cold energy utilization | |
| CN111763131A (en) | Method and device for producing ethane by cold dry gas reflux | |
| CN204944041U (en) | Utilize the system producing LNG containing air gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190402 Address after: 100094 Beijing Haidian District Fenghui Middle Road No. 7 New Material Pioneering Building 2 Floor 202 Patentee after: ZHONGKE RUIAO ENERGY TECHNOLOGY CO.,LTD. Address before: 100190 Beijing Haidian District Zhongguancun North No. 2 Patentee before: Technical Institute of Physics and Chemistry Chinese Academy of Sciences |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100106 |