CN104359286A - Method for removing acidic gas from natural gas - Google Patents
Method for removing acidic gas from natural gas Download PDFInfo
- Publication number
- CN104359286A CN104359286A CN201410632404.2A CN201410632404A CN104359286A CN 104359286 A CN104359286 A CN 104359286A CN 201410632404 A CN201410632404 A CN 201410632404A CN 104359286 A CN104359286 A CN 104359286A
- Authority
- CN
- China
- Prior art keywords
- gas
- feed pipe
- decompressor
- pipe
- flash tank
- 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.)
- Granted
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 239000007789 gas Substances 0.000 title claims abstract description 42
- 239000003345 natural gas Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000002378 acidificating effect Effects 0.000 title abstract description 6
- 238000010521 absorption reaction Methods 0.000 claims abstract description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 34
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 17
- 239000001569 carbon dioxide Substances 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 13
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 12
- 239000012159 carrier gas Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- 239000002737 fuel gas Substances 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- VZUGBLTVBZJZOE-KRWDZBQOSA-N n-[3-[(4s)-2-amino-1,4-dimethyl-6-oxo-5h-pyrimidin-4-yl]phenyl]-5-chloropyrimidine-2-carboxamide Chemical compound N1=C(N)N(C)C(=O)C[C@@]1(C)C1=CC=CC(NC(=O)C=2N=CC(Cl)=CN=2)=C1 VZUGBLTVBZJZOE-KRWDZBQOSA-N 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 239000000463 material Substances 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 3
- 238000004064 recycling Methods 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000002354 daily effect Effects 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a method for efficiently utilizing a water absorption method to remove acidic gas from natural gas. A device comprises a raw natural gas feeding pipe, an expansion machine, a brake fan, a compressor set, a separating tank, an absorbing tower, an air stripping tower, a flash tank, a water pump and a dryer, wherein a feeding pipe of the expansion machine is connected with a gas discharging pipe of the flash tank; a discharging pipe of the expansion machine is connected with a feeding pipe of the separating tank behind the expansion machine; a discharging pipe of the brake fan of the expansion machine is connected with a gas-loading port of the air stripping tower; a feeding pipe of the brake fan of the expansion machine is connected with atmosphere. The invention provides the method for utilizing the water absorption method to efficiently remove the high-content acidic gas from the natural gas; the method has the advantages of convenience in material taking, recycling, water-saving property, environmental protection and zero three-waste discharge; the method is simple in flow structure, low in energy consumption and low in cost.
Description
Technical field
The present invention relates to a kind of correlative technology field of refining natural gas, specifically a kind of method removing sour gas in natural gas.
Background technology
As everyone knows, natural gas is a kind of clean energy resource.In recent years, plant construction quantity was the trend of cumulative year after year.No matter pipeline gas or vehicle-mounted natural gas or by natural gas liquefaction, all must by the carbon dioxide (CO in raw natural gas
2) and hydrogen sulfide (H
2s) remove, they are also referred to as " acidity " material, can aggravate outside the corrosion in gas pipeline, also have the commercial requirements of the acidic materials Cmin in the law or involved gas product of being correlated with in region.Therefore, reach the quality index of commercial natural gas, the energy ezpenditure reducing each link is the most important ring of design-build gas plant.
At present, market develops relevant absorption method and the feeding gas coming artesian well source or storage reservoir has been dewatered, and then the gas stream of dehydration is processed to remove blue sky and reduces the acidic materials wherein contained; The method wherein generally used depends on various molecular sieve and physics and subcooled liquid and all has side effect, and the heavier hydrocarbon namely contained in liquid can be removed with acidic materials, and this makes the hydrocarbon being difficult to reclaim obviously will increase cost recovery.
Summary of the invention
The object of this invention is to provide a kind of method removing sour gas in natural gas.
The object of the present invention is achieved like this: a kind of method removing sour gas in natural gas, the method includes unstripped gas knockout drum before compressor, feed gas compressor, absorption tower, flash tank, braking blower, stripping tower, water pump, drier, is characterized in that: be connected with the feed pipe of decompressor at flash tank gas discharge pipe, and the discharge nozzle of described decompressor is connected with the feed pipe of knockout drum after decompressor, the discharge nozzle of the braking blower of described decompressor is connected with the carrier gas port of stripping tower, and the feed pipe of the braking blower of described decompressor is connected with air, the feed pipe of described raw natural gas connects with the feed pipe of knockout drum before compressor respectively with the escape pipe of knockout drum after decompressor, before described compressor, the escape pipe of unstripped gas knockout drum is connected with the feed pipe of compressor bank, the discharge nozzle of described compressor bank is connected with the gas feed pipe on absorption tower, the discharge nozzle of described water pump is connected with the liquid phase feeding pipe on absorption tower, the gaseous phase outlet pipe on described absorption tower is connected with the feed pipe of drier, the liquid-phase outlet pipe on described absorption tower is connected with the feed pipe of flash tank, between described absorption tower and flash tank, choke valve is housed, raw natural gas inlet condition is mol ratio: the fuel gas content 45-98% such as methane, the sour gas such as carbon dioxide and hydrogen sulfide 2-55%, temperature example-20 DEG C is to 40 DEG C, admission pressure normal pressure-0.3MPa, gas product pressure: 0.4-7MPa, purification precision: mol ratio carbon dioxide 30ppm-3%.
The present invention also comprises: the liquid outlet tube of described flash tank is connected with the liquid feed pipe of stripping tower, also choke valve is housed between described flash tank and stripping tower, and the liquid outlet tube of described stripping tower is connected with unit fixed on water pump suction.
Beneficial effect of the present invention:
1. decompressor is applied to the method that water absorption method removes sour gas, achieves many things at one stroke dexterously.Patent application decompressor of the present invention has the effect of three aspects: be that the braking blower of decompressor is replaced traditional air blast on the one hand; As done carrier gas with air, the input of traditional stripping tower carrier gas necessarily has the help of air blast; The brake of traditional decompressor, as with blower fan braking, scarcely reclaims, and by emptying; The method of this invention, decompressor externally expansion work recycles the carrier gas source of the gas as stripping tower, and saves the power consumption of former air blast.Be that decompressor provides cold to the natural gas reclaimed on the other hand, the natural gas of recovery mixes with raw natural gas makes press inlet temperature reduce, and reduces press energy consumption.The while of also having a benefit to be gas temperature reduction, produce gas-liquid two-phase, a part of moisture content can be isolated in advance in knockout drum, reduce the air-intake load of press, also just save the energy consumption of natural gas compressor.Because the cold that decompressor provides, gas has twice temperature to reduce, and after decompressor, before knockout drum and compressor, a part of moisture content respectively isolated by knockout drum respectively.
2. the present invention is provided with flash tank farthest to reduce the loss of methane, and provides source of the gas for the use of decompressor, and before stripping tower, isolate a part of carbon dioxide and hydrogen sulfide, alleviates the load of stripping tower.In absorption tower in natural gas and water generation physical absorption process, not only carbon dioxide and hydrogen sulfide are removed, and a small amount of methane also can be dissolved in water.In order to reclaim this portion of methane, this method arranges choke valve and flash tank behind absorption tower, the rich solution of step-down is seethed with excitement rapidly vaporization in flash tank, and carries out two-phase laminated flow.Be rich in methane and carbon dioxide in the gas be separated, press entrance need be turned back to and reenter absorption tower recovery.The liquid be separated uses air stripping in stripping tower, to remove the carbon dioxide and hydrogen sulfide that dissolve in water.Can regeneration cycle be used by water after flash distillation and stripping.
3. the present invention adopts water to be absorbent, draws materials conveniently, and recycles, saving water resource, and environmental protection, three-waste free discharge.This method flowage structure is simple, and energy consumption is low, cost is low.
Though the 4. new boost expander of the present invention, not than traditional flow process many increases energy consumption, instead because the reduction of intake air temperature and isolate a part of moisture content, reduce the energy consumption of press, and also a saving the energy consumption of former air blast.As calculated, for the natural gas refining device of a set of daily output 20,000 Nm3, though application decompressor input 5 ten thousand yuan more than use air blast, but press can be saved and run power consumption 14 kilowatt hour, the electricity charge calculate according to 0.7 yuan of every kilowatt hour, operating cost 235 yuan can be saved every day, can be user every year and save 7.05 ten thousand yuan.In sum, adopt equipment of the present invention, can energy-conservation about 8%, improve the market competitiveness of enterprise.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the present invention is described in further detail.
Fig. 1 is process structure simplified schematic diagram of the present invention.
The symbol description of accompanying drawing major part: 1 is unstripped gas knockout drum before compressor, and 2 is feed gas compressor, and 3 is absorption tower, and 4 is flash tank, 5 is knockout drum after decompressor, and 6 is decompressor, and 7 is braking blower, and 8 is stripping tower, 9 is water pump, and 10 is drier, and 11,12 are choke valve.
Be described in further detail the present invention by example below in conjunction with accompanying drawing, but following example is only the present invention's example wherein, do not represent the rights protection scope that the present invention limits, the scope of the present invention is as the criterion with claim.
Detailed description of the invention
embodiment 1:
As shown in Figure 1,1 in figure is unstripped gas knockout drum before compressor, and 2 be feed gas compressor 3 is absorption tower, and 4 is flash tank; Be connected with the feed pipe of decompressor 6 at flash tank 4 gas discharge pipe, the discharge nozzle of described decompressor 6 is connected with the feed pipe of knockout drum after decompressor 5, the discharge nozzle of the braking blower 7 of described decompressor is connected with the carrier gas port of stripping tower 8, and the feed pipe of the braking blower 7 of described decompressor is connected with air; The feed pipe of described raw natural gas (A in Fig. 1) connects with the feed pipe of knockout drum before compressor 1 respectively with the escape pipe of knockout drum after decompressor 5, before described compressor, the escape pipe of unstripped gas knockout drum 1 is connected with the feed pipe of compressor bank 2, and the discharge nozzle of described compressor bank 2 is connected with the gas feed pipe on absorption tower 3; The discharge nozzle of described water pump 9 is connected with the liquid phase feeding pipe on absorption tower 3, the gaseous phase outlet pipe on described absorption tower 3 is connected with the feed pipe of drier 10, the liquid-phase outlet pipe on described absorption tower 3 is connected with the feed pipe of flash tank 4, between described absorption tower 3 and flash tank 4, choke valve 11 is housed; The liquid outlet tube of described flash tank 4 is connected with the liquid feed pipe of stripping tower 8, between described flash tank 4 and stripping tower 8, choke valve 12 is also housed, and the liquid outlet tube of described stripping tower 8 is connected with water pump 9 import.
Raw natural gas inlet condition is mol ratio: the fuel gas content 45-98% such as methane, the sour gas such as carbon dioxide and hydrogen sulfide 2-55%, and tolerance is not limit; Temperature example-20 DEG C is to 40 DEG C; Admission pressure normal pressure-0.3MPa; Gas product pressure: 0.4-7MPa; Purification precision: mol ratio carbon dioxide 30ppm-3%.
Natural gas feed pipe of the present invention is successively by becoming the natural gas of the purification of decarbonization, desulfuration after knockout drum, compressor bank, absorption tower, drier before compressor; And the source of another road natural gas feed pipe gas containing gas component that to be rich solution at the bottom of absorption tower flash off at flash tank through choke valve step-down is after decompressor step-down cooling, knockout drum after decompressor is separated the gas after a part of water and natural gas feed pipe mixed gases, again cooling isolate free water, after enter compressor bank.
Decompressor of the present invention provides cold to the natural gas reclaimed on the one hand, reduces press load, reduces energy consumption, external for decompressor work reclaimed on the other hand, consume in the carrier gas of stripping tower.Kill two birds with one stone.
The present invention enters absorption tower by after the supercharging of natural gas via overcompression machine from bottom, and water enters from tower body top, and anti-phase flowing absorbs.In this physical absorption process, not only carbon dioxide and hydrogen sulfide are removed, and a small amount of methane also can be dissolved in water.This sub-fraction methane reclaims and through decompressor decrease temperature and pressure, after isolating a part of moisture content, injects in absorption tower after reentering press inlet compression, farthest decrease the loss of methane in flash tank.High-purity natural gas (C in Fig. 1) after purification is discharged from the top on absorption tower 10, after drier drying, become gas product.The rich solution being rich in carbon dioxide and hydrogen sulfide enters flash tank through decompression, after isolating most carbon dioxide and hydrogen sulfide, blow with air in stripping tower, after carbon dioxide wherein and hydrogen sulfide removal, water through water pump pressurization after again for absorption tower in remove carbon dioxide and hydrogen sulfide.The carrier gas source of the gas of stripping tower is air, is the source of the gas of the supporting unit braking blower of decompressor.Decompressor work is utilized.Waste gas (B in Fig. 1) sour gas for removing that stripping tower top produces, its Main Ingredients and Appearance is air and carbon dioxide and hydrogen sulfide.
In sum, object of the present invention is achieved.
Claims (2)
1. one kind removes the method for sour gas in natural gas, the method includes unstripped gas knockout drum before compressor, feed gas compressor, absorption tower, flash tank, braking blower, stripping tower, water pump, drier, is characterized in that: be connected with the feed pipe of decompressor at flash tank gas discharge pipe, and the discharge nozzle of described decompressor is connected with the feed pipe of knockout drum after decompressor, the discharge nozzle of the braking blower of described decompressor is connected with the carrier gas port of stripping tower, and the feed pipe of the braking blower of described decompressor is connected with air, the feed pipe of described raw natural gas connects with the feed pipe of knockout drum before compressor respectively with the escape pipe of knockout drum after decompressor, before described compressor, the escape pipe of unstripped gas knockout drum is connected with the feed pipe of compressor bank, the discharge nozzle of described compressor bank is connected with the gas feed pipe on absorption tower, the discharge nozzle of described water pump is connected with the liquid phase feeding pipe on absorption tower, the gaseous phase outlet pipe on described absorption tower is connected with the feed pipe of drier, the liquid-phase outlet pipe on described absorption tower is connected with the feed pipe of flash tank, between described absorption tower and flash tank, choke valve is housed, raw natural gas inlet condition is mol ratio: the fuel gas content 45-98% such as methane, the sour gas such as carbon dioxide and hydrogen sulfide 2-55%, temperature example-20 DEG C is to 40 DEG C, admission pressure normal pressure-0.3MPa, gas product pressure: 0.4-7MPa, purification precision: mol ratio carbon dioxide 30ppm-3%.
2. the method removing sour gas in natural gas according to claim 1, it is characterized in that: the liquid outlet tube of described flash tank is connected with the liquid feed pipe of stripping tower, also choke valve is housed between described flash tank and stripping tower, the liquid outlet tube of described stripping tower is connected with unit fixed on water pump suction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410632404.2A CN104359286B (en) | 2014-11-12 | A kind of remove the method for sour gas in natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410632404.2A CN104359286B (en) | 2014-11-12 | A kind of remove the method for sour gas in natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104359286A true CN104359286A (en) | 2015-02-18 |
| CN104359286B CN104359286B (en) | 2017-01-04 |
Family
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107381503A (en) * | 2017-08-28 | 2017-11-24 | 崔静思 | A kind of system and method for sulfide hydrogen conversion gas purification |
| CN113355142A (en) * | 2020-03-03 | 2021-09-07 | 中国石油化工股份有限公司 | Natural gas dechlorinating device and process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54103777A (en) * | 1978-02-01 | 1979-08-15 | Hitachi Ltd | Pretreatment of air separator |
| US6230518B1 (en) * | 1998-09-23 | 2001-05-15 | Linde Aktiengesellschaft | Process and liquefier for the production of liquid air |
| CN1952569A (en) * | 2006-04-18 | 2007-04-25 | 北京科瑞赛斯气体液化技术有限公司 | Process and equipment for liquefying air-containing coal-bed gas |
| CN102538398A (en) * | 2012-02-09 | 2012-07-04 | 杭州杭氧股份有限公司 | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) |
| CN103175379A (en) * | 2013-03-18 | 2013-06-26 | 上海交通大学 | Device for preparing liquefied natural gas with pipeline pressure energy and application method thereof |
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54103777A (en) * | 1978-02-01 | 1979-08-15 | Hitachi Ltd | Pretreatment of air separator |
| US6230518B1 (en) * | 1998-09-23 | 2001-05-15 | Linde Aktiengesellschaft | Process and liquefier for the production of liquid air |
| CN1952569A (en) * | 2006-04-18 | 2007-04-25 | 北京科瑞赛斯气体液化技术有限公司 | Process and equipment for liquefying air-containing coal-bed gas |
| CN102538398A (en) * | 2012-02-09 | 2012-07-04 | 杭州杭氧股份有限公司 | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) |
| CN103175379A (en) * | 2013-03-18 | 2013-06-26 | 上海交通大学 | Device for preparing liquefied natural gas with pipeline pressure energy and application method thereof |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107381503A (en) * | 2017-08-28 | 2017-11-24 | 崔静思 | A kind of system and method for sulfide hydrogen conversion gas purification |
| CN113355142A (en) * | 2020-03-03 | 2021-09-07 | 中国石油化工股份有限公司 | Natural gas dechlorinating device and process |
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| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 112300 Liaoning city of Tieling province Kaiyuan city Kaiyuan Economic Development Zone No. 1 North Street, a scientific research Applicant after: LIAONING CIMC HASHENLENG GAS LIQUEFACTION EQUIPMENT CO., LTD. Address before: 112300 No. 1, North Street, Kaiyuan economic and Technological Development Zone, Liaoning, Tieling Applicant before: Liaoning Harbin Shenleng Gas Liquefaction Equipment Co., Ltd. |
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