CN1414067A - Recovery method of light hydrocarbon in natural gas - Google Patents
Recovery method of light hydrocarbon in natural gas Download PDFInfo
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- CN1414067A CN1414067A CN 02132979 CN02132979A CN1414067A CN 1414067 A CN1414067 A CN 1414067A CN 02132979 CN02132979 CN 02132979 CN 02132979 A CN02132979 A CN 02132979A CN 1414067 A CN1414067 A CN 1414067A
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Abstract
A process for recovering light hydrocarbon from natural gas includes such steps as cooling natural gas, gas-liquid separation in separating tower, introducing gas to absorption tower, gas-liquid exchange with absorbent to generate C3 and C4 components for recovering, mixing the liquid with light hydrocarbon in the separator, introducing the mixture to desorption tower to release methane and ethane, introducing the generated desorption liquid to analyzing tower to obtain C3 and C4 components for recovering, pressurizing the heavy hydrocarbon in the analyzing tower by 1.35-1.55 MPa, and cooling to 38-42 deg.C, to generate light hydrocarbon for recovering. Its advantage is high recovery rate.
Description
Technical field: the present invention relates to a kind of after the shallow cold technology of Sweet natural gas grafting oil absorption technique, thereby improve the method for the hydrocarbon hydrocarbon rate of recovery.
Background technology: Natural Gas Shallow Freezing Unit is to reclaim C
3The chemical plant installations of above heavy component condensed liquid, its main processes is: adopt freezing method (20～-25 ℃) to separate liquid hydrocarbon (C after the natural gas via compressor boost
3 +) as ethene and other industrial chemicals export trade.The subject matter of the shallow cold existence of Sweet natural gas at present is: 1, light hydrocarbon yield is low: C in the Sweet natural gas
1Content adopts shallow cold technology lighter hydrocarbons resource (C at 75～90% (molar percentages)
2More than) rate of recovery has only 45～60%.2, the component yield is low: above-mentioned Sweet natural gas is formed the shallow cold technology of employing, key ingredient propane (C
3) yield has only 20～50%.
Summary of the invention: the present invention is grafting oil absorption technique after shallow cold technology, and utilizing and resolving the back heavy hydrocarbon is natural gas and oil C
5 +Absorption agent as the absorption tower, suction is taken off in employing, process of analysis carries out fractionation to absorption of light hydrocarbon and produces the liquefied gas product, form shallow cold-oil absorption-smart fractionated methods of light hydrocarbon recovery, this method is according to the gas-liquid phase equilibrium principle, utilize absorption agent that shallow cold dry gas is absorbed, further reclaim the C in the Sweet natural gas
3, C
4Component improves light hydrocarbon yield; Hydrocarbon mixture is carried out fractionation, produce liquefied gas and single-component hydrocarbon, the heavy hydrocarbon part after the fractionation is as the absorption agent recycling on absorption tower, and another part is defeated outward as product.The object of the present invention is to provide a kind of rate of recovery that can improve lighter hydrocarbons in the Sweet natural gas, increase the recovery method of lighter hydrocarbons in the Sweet natural gas of lighter hydrocarbons output.The recovery method of lighter hydrocarbons enters gains after the shallow cold technology of Sweet natural gas to carry out gas-liquid separation in the secondary triphase separator 1 exactly in the Sweet natural gas, makes gas enter the bottom on absorption tower 2 and the absorption agent in the absorption tower 2 and carries out the gas-liquid exchange and generate C
3, C
4Reclaim behind the component; Enter after lighter hydrocarbons in liquid and the secondary triphase separator 1 mix and deviate from methane and ethane in the desorption tower 4, make the imbibition of taking off of formation enter Analytic Tower 6 and cut out C
3, C
4Reclaim behind the component, also have gas and heavy hydrocarbon in the Analytic Tower 6, the heavy hydrocarbon in the Analytic Tower 6 is forced into 1.35～1.55Mpa, be cooled to 38 ℃～42 ℃, reclaim behind the formation lighter hydrocarbons.Send behind gas cooling to 28～32 in the Analytic Tower 6 ℃ into return tank 8, make the one partial reflux to Analytic Tower 6, another part is failed outward as civil liquefied gas.Absorption agent in the described absorption tower 2 is natural gas and oil C
5 +The invention has the advantages that: it can improve the rate of recovery of lighter hydrocarbons, and making incomparably, the light hydrocarbon recovery rate of Sweet natural gas improves 30～50%, C
3The rate of recovery brings up to 70～87% by original 20～50%; Can cut down the consumption of energy, use this method can fully reclaim surplus cold, the overbottom pressure of original device, waste heat, rely on former general facilities and manpower, reduce running cost, wherein shallow cold grafting oil absorption technique and single shallow cold comparing, ton hydrocarbon energy consumption descends 30%, compares with independent construction liquefied gas device, ton liquefied gas energy consumption descends more than 38%, saves manpower 30～50%.Can increase economic efficiency, can improve 6 times by Sweet natural gas liquefy hydrocarbon benefit; Hydrocarbon mixture is become liquefied gas can rise in value 20%.After adopting this method, handling incomparably, the gas economic benefit can improve about 1890 yuan.With Daqing oil field Sa Zhong district 300,000 sides/sky ammonia refrigeration shallow cooling device is example, after oily absorption of light hydrocarbon recombining process is used, and C
3Yield brings up to 75.0% by 23.72%, and light hydrocarbon yield is by 1.415t/10
4Nm
3Bring up to 2.144t/10
4Nm
3, 8000 tons of year volume increase lighter hydrocarbons, unit consumption of product descends 34%, save operation cost 45%, 1.5 ten thousand tons of year production liquefied gas.
Description of drawings: Fig. 1 is a process principle figure of the present invention.
Embodiment one: carry out freezing from entering shallow cooling system after compressed machine 20 superchargings of the oil field gas of oil recovery factory, water cooler 21 precoolings, 22 separation of one-level triphase separator, after the shallow cold technology of Sweet natural gas gains are entered and carry out gas-liquid separation in the secondary triphase separator 1, the bottom and the absorption agent in the absorption tower 2 that make gas enter absorption tower 2 carry out gas-liquid exchange generation C
3, C
4Reclaim behind the component, the gas of absorption tower 2 cats head goes outside 19 meterings of tank field defeated after rich or poor interchanger 3 heat exchange; Enter after isolated lighter hydrocarbons mix in liquid and the secondary triphase separator 1 at the bottom of the tower and deviate from methane and ethane in the desorption tower 4, after 5 heat exchange of Analytic Tower feed heater, enter Analytic Tower 6 and cut out C in the imbibition of taking off that forms at the bottom of desorption tower 4 towers
3, C
4Reclaim behind the component, also have gas and heavy hydrocarbon in the Analytic Tower 6, overhead gas in the Analytic Tower 6 is sent into return tank 8 after overhead condenser 7 is cooled to 28～32 ℃, make the one partial reflux to Analytic Tower 6 inner control tower top temperatures, it is outer defeated that another part is delivered to tank field 9 as civil liquefied gas, with the heavy hydrocarbon at the bottom of the towers in the Analytic Tower 6 through desorption tower column bottoms pump 10 be forced into 1.35～1.55Mpa, heavy hydrocarbon water cooler 11 is cooled to 38～42 ℃, reclaim after forming lighter hydrocarbons, a part can be entered absorption tower 2 as absorption agent, another part goes tank field 12 meterings outer defeated as light hydrocarbon product.Absorption agent in the described absorption tower is natural gas and oil C
5 +
Embodiment two: what present embodiment and embodiment one were different is, overhead gas in the Analytic Tower 6 is sent into return tank 8 after overhead condenser 7 is cooled to 30 ℃, make the one partial reflux to Analytic Tower 6 inner control tower top temperatures, it is outer defeated that another part is delivered to tank field 9 as civil liquefied gas, with the heavy hydrocarbon at the bottom of the towers in the Analytic Tower 6 through desorption tower column bottoms pump 10 be forced into 1.45Mpa, heavy hydrocarbon water cooler 11 is cooled to 40 ℃, reclaim after forming lighter hydrocarbons, a part can be entered absorption tower 2 as absorption agent, another part goes tank field 12 meterings outer defeated as light hydrocarbon product.Absorption agent in the described absorption tower is natural gas and oil C
5 +
Embodiment three: present embodiment and embodiment one, two different are, when producing motor liquified gas, the charging of gas in the Analytic Tower 6 as debutanizing tower 13 is transported in the debutanizing tower 13, liquid at the bottom of formation overhead gas and the tower, the overhead gas of debutanizing tower 13 is sent into return tank 15 after overhead condenser 14 is cooled to 38～42 ℃, after debutanizing tower reflux pump 16 is forced into 1.23～1.27Mpa, a part is back in the debutanizing tower 13, another part is delivered to tank field 17 as motor liquified gas and is stored, liquid mixes the back and goes tank field 12 meterings outer defeated as light hydrocarbon product after interchanger 18 is cooled to 38～42 ℃ at the bottom of the tower of debutanizing tower 13 with heavy hydrocarbon at the bottom of the tower in the Analytic Tower 6.
Embodiment four: what present embodiment and embodiment three were different is, when producing motor liquified gas, the charging of gas in the Analytic Tower 6 as debutanizing tower 13 is transported in the debutanizing tower 13, liquid at the bottom of formation overhead gas and the tower, the overhead gas of debutanizing tower 13 is sent into return tank 15 after overhead condenser 14 is cooled to 40 ℃, after debutanizing tower reflux pump 16 is forced into 1.25Mpa, a part is back in the debutanizing tower 13, another part is delivered to tank field 17 as motor liquified gas and is stored, liquid mixes the back and goes tank field 12 meterings outer defeated as light hydrocarbon product after interchanger 18 is cooled to 40 ℃ at the bottom of the tower of debutanizing tower 13 with heavy hydrocarbon at the bottom of the tower in the Analytic Tower 6.
Claims (5)
1, the recovery method of lighter hydrocarbons in a kind of Sweet natural gas, it is characterized in that after the shallow cold technology of Sweet natural gas gains being entered in the secondary triphase separator (1) carries out gas-liquid separation, the bottom and the absorption agent in absorption tower (2) that make gas enter absorption tower (2) carry out gas-liquid exchange generation C
3, C
4Reclaim behind the component; Enter in the desorption tower (4) after lighter hydrocarbons in liquid and the secondary triphase separator (1) mix and deviate from methane and ethane, make the imbibition of taking off of formation enter Analytic Tower (6) and cut out C
3, C
4Reclaim behind the component, also have gas and heavy hydrocarbon in the Analytic Tower (6), the heavy hydrocarbon in the Analytic Tower (6) is forced into 1.35～1.55Mpa, be cooled to 38 ℃～42 ℃, reclaim behind the formation lighter hydrocarbons.
2, the recovery method of lighter hydrocarbons in the Sweet natural gas according to claim 1, it is characterized in that sending behind gas cooling to 28～32 in the Analytic Tower (6) ℃ into return tank (8), make the one partial reflux to Analytic Tower (6), another part is defeated outward as civil liquefied gas.
3, the recovery method of lighter hydrocarbons in the Sweet natural gas according to claim 1, it is characterized in that the charging of the gas in the Analytic Tower (6) as debutanizing tower (13) is transported in the debutanizing tower (13), liquid at the bottom of formation overhead gas and the tower, the overhead gas of debutanizing tower (13) is sent into return tank (15) after overhead condenser (14) is cooled to 38～42 ℃, after debutanizing tower reflux pump (16) is forced into 1.23～1.27Mpa, a part is back in the debutanizing tower (13), another part is delivered to tank field (17) as motor liquified gas and is stored, liquid mixes the back and goes tank field (12) metering outer defeated as light hydrocarbon product after interchanger (18) is cooled to 38～42 ℃ at the bottom of the tower of debutanizing tower (13) with heavy hydrocarbon at the bottom of the interior tower of Analytic Tower (6).
4, the recovery method of lighter hydrocarbons in the Sweet natural gas according to claim 3, it is characterized in that the charging of the gas in the Analytic Tower (6) as debutanizing tower (13) is transported in the debutanizing tower (13), liquid at the bottom of formation overhead gas and the tower, the overhead gas of debutanizing tower (13) is sent into return tank (15) after overhead condenser (14) is cooled to 40 ℃, after debutanizing tower reflux pump (16) is forced into 1.25Mpa, a part is back in the debutanizing tower (13), another part is delivered to tank field (17) as motor liquified gas and is stored, liquid mixes the back and goes tank field (12) metering outer defeated as light hydrocarbon product after interchanger (18) is cooled to 40 ℃ at the bottom of the tower of debutanizing tower (13) with heavy hydrocarbon at the bottom of the interior tower of Analytic Tower (6).
5,, it is characterized in that the absorption agent in the described absorption tower (2) is natural gas and oil C according to the recovery method of lighter hydrocarbons in claim 1,2, the 3 or 4 described Sweet natural gases
5 +
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02132979 CN1414067A (en) | 2002-09-17 | 2002-09-17 | Recovery method of light hydrocarbon in natural gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02132979 CN1414067A (en) | 2002-09-17 | 2002-09-17 | Recovery method of light hydrocarbon in natural gas |
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|---|---|
| CN1414067A true CN1414067A (en) | 2003-04-30 |
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ID=4747006
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|---|---|---|---|
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320096C (en) * | 2004-10-13 | 2007-06-06 | 姜国文 | Brewing equipment for preparing lightweight alkane from heavy hydrocarbon and process thereof |
| CN100347272C (en) * | 2006-01-20 | 2007-11-07 | 华南理工大学 | Light hydrocarbon separating method for liquefied natural gas with peak regulating function |
| CN100354393C (en) * | 2004-12-22 | 2007-12-12 | 三菱电机株式会社 | Apparatus and method for treating and recovering gaseous hydrocarbons |
| CN100365101C (en) * | 2005-09-23 | 2008-01-30 | 河南中原绿能高科有限责任公司 | Method for removing heavy hydrocarbon in natural gas by heavy hydrocarbon absorption |
| CN102453599A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Composite calcium sulfonate-based tetrapolyurea lubricating grease and preparation method thereof |
| CN103351895A (en) * | 2013-06-07 | 2013-10-16 | 新地能源工程技术有限公司 | Method and device for removing water and heavy hydrocarbons from shale gas |
| CN103822438A (en) * | 2012-11-16 | 2014-05-28 | 中国石油天然气股份有限公司 | Shallow-cooling light hydrocarbon recovery process method |
| CN113755198A (en) * | 2020-06-03 | 2021-12-07 | 中国石油化工股份有限公司 | Method for recovering carbon dioxide and heavier components in refinery dry gas, system and application thereof |
| CN113755201A (en) * | 2020-06-03 | 2021-12-07 | 中国石油化工股份有限公司 | Method for concentrating carbon dioxide and components in dry gas of light and heavy refinery, device and application thereof |
-
2002
- 2002-09-17 CN CN 02132979 patent/CN1414067A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320096C (en) * | 2004-10-13 | 2007-06-06 | 姜国文 | Brewing equipment for preparing lightweight alkane from heavy hydrocarbon and process thereof |
| CN100354393C (en) * | 2004-12-22 | 2007-12-12 | 三菱电机株式会社 | Apparatus and method for treating and recovering gaseous hydrocarbons |
| CN100365101C (en) * | 2005-09-23 | 2008-01-30 | 河南中原绿能高科有限责任公司 | Method for removing heavy hydrocarbon in natural gas by heavy hydrocarbon absorption |
| CN100347272C (en) * | 2006-01-20 | 2007-11-07 | 华南理工大学 | Light hydrocarbon separating method for liquefied natural gas with peak regulating function |
| CN102453599A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Composite calcium sulfonate-based tetrapolyurea lubricating grease and preparation method thereof |
| CN102453599B (en) * | 2010-10-22 | 2014-10-01 | 中国石油化工股份有限公司 | Composite calcium-sulfonate-based tetrapolyurea lubricating grease and preparation method thereof |
| CN103822438A (en) * | 2012-11-16 | 2014-05-28 | 中国石油天然气股份有限公司 | Shallow-cooling light hydrocarbon recovery process method |
| CN103822438B (en) * | 2012-11-16 | 2016-08-03 | 中国石油天然气股份有限公司 | Shallow-cooling light hydrocarbon recovery process method |
| CN103351895A (en) * | 2013-06-07 | 2013-10-16 | 新地能源工程技术有限公司 | Method and device for removing water and heavy hydrocarbons from shale gas |
| CN103351895B (en) * | 2013-06-07 | 2015-05-06 | 新地能源工程技术有限公司 | Method and device for removing water and heavy hydrocarbons from shale gas |
| CN113755198A (en) * | 2020-06-03 | 2021-12-07 | 中国石油化工股份有限公司 | Method for recovering carbon dioxide and heavier components in refinery dry gas, system and application thereof |
| CN113755201A (en) * | 2020-06-03 | 2021-12-07 | 中国石油化工股份有限公司 | Method for concentrating carbon dioxide and components in dry gas of light and heavy refinery, device and application thereof |
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