CN104359286B - A kind of remove the method for sour gas in natural gas - Google Patents
A kind of remove the method for sour gas in natural gas Download PDFInfo
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- CN104359286B CN104359286B CN201410632404.2A CN201410632404A CN104359286B CN 104359286 B CN104359286 B CN 104359286B CN 201410632404 A CN201410632404 A CN 201410632404A CN 104359286 B CN104359286 B CN 104359286B
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Abstract
A kind of utilize the method for sour gas in water absorption method removing natural gas efficiently.Its equipment, including raw natural gas feed pipe, decompressor and braking blower, compressor bank, knockout drum, absorption tower, stripping tower, flash tank, water pump, exsiccator.The feed pipe of described decompressor is connected with the gas discharge pipe of flash tank, 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 present invention is to draw materials conveniently by the method for high-load sour gas in water absorption method efficient removal natural gas, and recycles, saving water resource, and environmental protection, three-waste free discharge.This method flowage structure is simple, and energy consumption is low, low cost.
Description
Technical field
The present invention relates to the correlative technology field of a kind of refining natural gas, a kind of remove the method for sour gas in natural gas.
Background technology
It is known that natural gas is a kind of clean energy resource.In recent years, plant construction quantity was the trend of cumulative year after year.It is no matter pipeline gas or vehicle-mounted natural gas or by natural gas liquefaction, it is necessary to by the carbon dioxide (CO in natural gas2) and hydrogen sulfide (H2S) removing, they are also referred to as " acid " material, can aggravate outside the corrosion in gas pipeline, the commercial requirements of the acidic materials Cmin in also relevant in region law or involved gas product.Therefore, reaching the quality index of commercial natural gas, the energy expenditure reducing each link is the most important ring of design-build gas plant.
At present, market having been developed for relevant absorption method and is dehydrated the feeding gas coming artesian well source or storage reservoir, the gas stream to dehydration processes the acidic materials wherein contained with removing the most again；The method wherein commonly used depends on various molecular sieve and physics and subcooled liquid is respectively provided with side effect, and the heavier Hydrocarbon i.e. contained in liquid can be removed with acidic materials, and this Hydrocarbon making it difficult to reclaim will substantially increase cost recovery.
Summary of the invention
It is an object of the invention to provide and a kind of remove the method for sour gas in natural gas.
The object of the present invention is achieved like this: a kind of removes the method for sour gas in natural gas, the method is carried out in following system, this system includes knockout drum before compressor, compressor bank, absorption tower, flash tank, braking blower, stripping tower, water pump, exsiccator, it is characterized in that: be connected with the feed pipe of decompressor at flash tank gas discharge pipe, 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, the feed pipe of the braking blower of described decompressor is connected with air；The feed pipe of described 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 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 exsiccator, the liquid-phase outlet pipe on described absorption tower is connected with the feed pipe of flash tank, equipped with choke valve between described absorption tower and flash tank；Natural gas inlet condition is that mol ratio is: methane fuel gas content 45 ~ 98%, carbon dioxide and acid hydrogen sulfide gas 2 ~ 55%；Temperature example-20 DEG C ~ 40 DEG C；Admission pressure normal pressure-0.3MPa；Product atmospheric pressure: 0.4 ~ 7MPa；Purification precision: mol ratio carbon dioxide 30ppm ~ 3%.
Present invention additionally comprises: the liquid outlet tube of described flash tank is connected with the liquid feed pipe of stripping tower, be also equipped with choke valve between described flash tank and stripping tower, the liquid outlet tube of described stripping tower is connected with unit fixed on water pump suction.
Beneficial effects of the present invention:
1. the method that decompressor is applied to water absorption method removing sour gas, achieves many things at one stroke dexterously.Patent application decompressor of the present invention has the effect of three aspects: be on the one hand that the braking blower of decompressor is replaced traditional aerator；As made carrier gas with air, the input of traditional stripping tower carrier gas necessarily has the help of aerator；The brake of traditional decompressor, as braked with blower fan, is scarcely reclaimed, and is vented；The method of this invention, decompressor externally expands work and recycles the carrier gas source of the gas as stripping tower, and saves the power consumption of former aerator.On the other hand being that decompressor provides the cold natural gas to reclaiming, the natural gas of recovery mixes with natural gas makes press inlet temperature reduce, and reduces press energy consumption.It is also an advantage that be, while gas temperature reduces, to produce gas-liquid two-phase, knockout drum can be isolated a part of moisture content in advance, reduce the air-intake load of press, the most 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 the use for decompressor provides source of the gas, and isolates a part of carbon dioxide and hydrogen sulfide before stripping tower, alleviates the load of stripping tower.In absorption tower, natural gas is with water generation physical absorption process, and 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 so that the rich solution of blood pressure lowering seethes with excitement rapidly vaporization in flash tank, and carries out two-phase laminated flow.Rich in methane and carbon dioxide in the gas separated, press entrance need to be returned to and reenter absorption tower recovery.The liquid separated uses air stripping, the carbon dioxide dissolved in water with removing and hydrogen sulfide in stripping tower.Can be used with regeneration cycle by water after flash distillation and stripping.
3. the present invention adopts water as 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, low cost.
Though the 4. new boost expander of the present invention, but the not traditional flow process many increases energy consumption of ratio, 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 aerator.It is computed, for the natural gas refining device of a set of daily output 20,000 Nm, though application decompressor ratio uses the many inputs of aerator 50,000 yuan, 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, can save operating cost 235 yuan every day, can be that user saves 7.05 ten thousand yuan every year.In sum, use the equipment of the present invention, the market competitiveness of enterprise can be improve with energy-conservation about 8%.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the present invention is described in further detail.
Fig. 1 is the process structure simplified schematic diagram of the present invention.
The symbol description of accompanying drawing major part: 1 is knockout drum before compressor, 2 is compressor bank, and 3 is absorption tower, and 4 is flash tank, and 5 is knockout drum after decompressor, and 6 is decompressor, and 7 is braking blower, and 8 is stripping tower, and 9 is water pump, and 10 is exsiccator, and 11,12 are choke valve.
Below in conjunction with accompanying drawing and by example, the present invention is described in further detail, but the following example example therein that is only the present invention, not representing the rights protection scope that the present invention is limited, 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 knockout drum before compressor, and 2 is compressor bank, and 3 is absorption tower, and 4 is flash tank；It is 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 natural gas (A in Fig. 1) with the escape pipe of knockout drum after decompressor 5 respectively feed pipe with knockout drum before compressor 1 connect, before described compressor, the escape pipe of 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 exsiccator 10, the liquid-phase outlet pipe on described absorption tower 3 is connected with the feed pipe of flash tank 4, equipped with choke valve 11 between described absorption tower 3 and flash tank 4；The liquid outlet tube of described flash tank 4 is connected with the liquid feed pipe of stripping tower 8, is also equipped with choke valve 12 between described flash tank 4 and stripping tower 8, and the liquid outlet tube of described stripping tower 8 is connected with water pump 9 import.
Natural gas inlet condition is that mol ratio is: the fuel gas content 45 ~ 98% such as methane, and the sour gas such as carbon dioxide and hydrogen sulfide 2 ~ 55%, tolerance does not limits；Temperature example-20 DEG C ~ 40 DEG C；Admission pressure normal pressure-0.3MPa；Product atmospheric pressure: 0.4 ~ 7MPa；Purification precision: mol ratio carbon dioxide 30ppm ~ 3%.
The natural gas feed pipe of the present invention becomes the natural gas of the purification of decarbonization, desulfuration after knockout drum, compressor bank, absorption tower, exsiccator before passing sequentially through compressor；And the gas containing gas component that the source of another road natural gas feed pipe flashes off at flash tank through choke valve blood pressure lowering for rich solution at the bottom of absorption tower is after decompressor blood pressure lowering is lowered the temperature, gas after knockout drum separates a part of water after decompressor and natural gas feed pipe mixed gases, free water is isolated in cooling again, enters compressor bank afterwards.
On the one hand the decompressor of the present invention provides the cold natural gas to reclaiming, and reduces press load, reduces energy consumption, on the other hand external for decompressor work is reclaimed, and consumes in the carrier gas of stripping tower.Kill two birds with one stone.
The present invention be by after natural gas via overcompression machine supercharging from entrance absorption tower, bottom, water from tower body top enter, anti-phase flowing absorb.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 in flash tank, after isolating a part of moisture content, injects in absorption tower, farthest decrease the loss of methane after reentering press inlet compression.High-purity natural gas (C in Fig. 1) after purification is discharged from the top on absorption tower 3, becomes product gas after drying through exsiccator.Rich solution rich in carbon dioxide and hydrogen sulfide enters flash tank through decompression, after isolating most carbon dioxide and hydrogen sulfide, stripping tower blows with air, after carbon dioxide therein and hydrogen sulfide removal, water is re-used in absorption tower removing removing carbon dioxide and hydrogen sulfide after water pump pressurizes.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.The waste gas (B in Fig. 1) that stripping tower top produces be the sour gas removed, and its Main Ingredients and Appearance is air and carbon dioxide and hydrogen sulfide.
In sum, it is achieved that the purpose of the present invention.
Claims (2)
1. one kind removes the method for sour gas in natural gas, the method is carried out in following system, this system includes knockout drum before compressor, compressor bank, absorption tower, flash tank, braking blower, stripping tower, water pump, exsiccator, it is characterized in that: flash tank gas discharge pipe is connected with the feed pipe of decompressor, the discharge nozzle of described decompressor is connected with the feed pipe of knockout drum after decompressor, and 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 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 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 exsiccator, the liquid-phase outlet pipe on described absorption tower is connected with the feed pipe of flash tank, equipped with choke valve between described absorption tower and flash tank；Natural gas inlet condition is that mol ratio is: methane fuel gas content 45 ~ 98%, carbon dioxide and acid hydrogen sulfide gas 2 ~ 55%；Temperature example-20 DEG C ~ 40 DEG C；Admission pressure normal pressure-0.3MPa；Product atmospheric pressure: 0.4 ~ 7MPa；Purification precision: mol ratio carbon dioxide 30ppm ~ 3%.
The method of sour gas in removing natural gas the most 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, being also equipped with choke valve 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 CN104359286A (en) | 2015-02-18 |
| CN104359286B true CN104359286B (en) | 2017-01-04 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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| PB01 | Publication | ||
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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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