CN101205484A - Three-in-one stable treatment technique for crude oil - Google Patents
Three-in-one stable treatment technique for crude oil Download PDFInfo
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- CN101205484A CN101205484A CNA2007100318476A CN200710031847A CN101205484A CN 101205484 A CN101205484 A CN 101205484A CN A2007100318476 A CNA2007100318476 A CN A2007100318476A CN 200710031847 A CN200710031847 A CN 200710031847A CN 101205484 A CN101205484 A CN 101205484A
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Abstract
The invention provides a triad stabilizing treatment technology for crude oil, which combining crude oil stabilization, light hydrocarbon recovery and liquefied petroleum gas generation as a whole, wherein stabilized crude oil and qualified LPG products are produced by directly treating unstabilized oil flow A. If the light hydrocarbon B which is recovered from natural gas is existed, the light hydrocarbon B can be mixed with the unstabilized oil flow A and treated together. The invention has the advantages of greatly simplifying the technological process, reducing the number of technological treatment equipment, realizing the stabilization of the crude oil without specific arrangement of a crude oil stabilization system, realizing the reutilization of heavy components of the natural gas without specific arrangement of a light hydrocarbon recovering system which has the functions of low pressure air recovery compression, dehydration, refrigeration and condensed liquid separation recovery, canceling the natural gas dewatering equipment and the condensed liquid recovery and separation equipment in a low pressure air compressor, which consume a great deal of energy, decreasing the occupation area of the equipments, saving equipment costs and converting the worthlessly recovered crude oil stabilization flash vapor generated by adopting the conventional light hydrocarbon recovery technology to the valuable recoverable light hydrocarbon, thereby realizing the aim of the energy conservation and the emission reduction.
Description
Technical field
The invention belongs to the stabilization of crude oil treatment process, particularly a kind of three-in-one treatment process that collects stabilization of crude oil, lighter hydrocarbons recovery and production liquefied petroleum gas (LPG).
Background technology
Offshore oil and gas art breading flow process: the oil gas product of offshore platform is via the oil gas treatment system that is provided with on the platform, oil gas handled to reach after outer defeated the requirement respectively through the sea pipe is outer fail.To the Sweet natural gas of unconditional conveying, then on platform, burn or emptying through torch.
On platform,, three kinds of situations are arranged to the treatment scheme of institute's produce oil gas: 1, with institute's producing oil well product on the platform through oil and gas and water from, dehydrating of crude oil and the stable after outer defeated disembarkation of sea pipe, store and sale.This kind flow process generally will be through three, level Four oil gas process treatment process.2, on the platform with well product through preliminary oil and gas and water from after, will be after the sea pipe be carried disembarkation without the moisture and unstabilized crude of thoroughly dehydration, do further processing again and make the moisture of crude oil and stablize qualified back and store and sell.This kind flow process generally only needs the simple oil and gas and water of process one-level or secondary from processing on platform.3, on platform, well product is not done any processing, directly deal with again after the oil and gas multiphase flow disembarkation.The treatment scheme of land terminal: after the unprocessed oil stream disembarkation after qualified, just can make crude oil reach the standard that meets sale at sea through gas-oil separation, dehydrating of crude oil and stable treated process.
In the process of gas-oil separation and stabilization of crude oil, can produce a large amount of low pressure flash gas.Generally terminal can be provided with light hydrocarbon recovery system by land, recycles this part low pressure flash gas.Promptly through with gas recovery compression, dehydration, freezing with process such as separate and reclaim propane and above heavy constituent in the gas, be light hydrocarbon recovery system.
Light hydrocarbon recovery system is reclaimed the lighter hydrocarbons that obtain pass through flash distillation and rectifying processing LPG product again, and obtain byproduct-flash overhead gas (can be used as fuel gas) and stable condensate oil.
1., oil and gas and water is from, dehydration, stabilization of crude oil, storage and sale land art breading flow process comprises three big steps:; 2., the recovery compression of low pressure flash gas, dehydration, the freezing and isolating lighter hydrocarbons recovery process of lime set; 3., the lighter hydrocarbons that recovery is obtained are produced the LPG product through flash distillation and rectifying.
FPSO art breading flow process: marine Floating Production stores and export tanker is called for short FPSO, and the FPSO that uses at China's offshore oilfield has two kinds of different art breading flow processs.1, on FPSO, has only oil and gas and water from, dehydration and flash crude-stabilization treatment scheme.The low pressure flash gas that produces through torch emptying, oil storage chamber is discharged gas by vent valve emptying.2, the art breading flow process on the FPSO be on above-mentioned 1 basis, increased light hydrocarbon recovery system (flow process is with the light hydrocarbon recovery system of land terminal) and LPG production, store and outside communication system.
Because the rising steadily and carry out the national policy of energy-saving and emission-reduction of international oil price, lighter hydrocarbons recovery being set on FPSO and producing the LPG system is sure developing direction.Make that the art breading flow process on the FPSO is consistent with the land terminal treatment scheme.Include light hydrocarbon recovery system and LPG productions, store and outer communication system.
Summary of the invention
The purpose of this invention is to provide a kind of three-in-one stable treatment technique for crude oil, reasonably control phase transition process and operating parameters by simplifying flow process, realized that land terminal or FPSO go up common the needs through stabilization of crude oil, lighter hydrocarbons recovery and three process treatment process of production LPG, be reduced to and only use wherein last production LPG process treatment process, can finish whole treatment process.The direct process for producing of the stream A of stabilize oil is not gone out stable crude and qualified LPG product.Can not mixing if any the lighter hydrocarbons B that reclaims from Sweet natural gas, stabilize oil flows processing together among the A.
The present invention flows through the not stabilize oil of import A and directly sends into heavily boil absorption tower 3 and debutylize rectifying tower thereafter 6 of deethanizing behind the heat temperature raising and handle; What boil heavily that absorption tower 3 cats head discharge from deethanizing is through absorbing the dry gas E after reclaiming lighter hydrocarbons, and discharging what obtain after the heat exchange cooling at the bottom of debutylize rectifying tower 6 towers is that stable crude C and tower top outlet obtain liquefied petroleum gas product D after condensation and pump supercharging; Finish stabilization of crude oil with a set of equipment flow process, from the flashed vapour of stabilization of crude oil, reclaim the three-in-one stable treatment technique for crude oil of lighter hydrocarbons and production liquefied petroleum gas (LPG).
Described for large-scale rectifying tower equipment by pressure regulator valve 1, interchanger 2, deethanizing heavily boil absorption tower 3 and bottom reboiler 3-1, topping-up pump 4, interchanger 5, debutylize rectifying tower 6 and bottom reboiler 6-1 and water cooler 6-3, backflow surge tank 6-4 and reflux pump 6-5, water cooler 7, propane evaporator 8, recycle pump 9, propane evaporator 10, surge tank 11, LPG topping-up pump 12 and molecular sieve 13 are formed, pressure regulator valve 1, interchanger 2 and deethanizing 3 middle parts, absorption tower of heavily boiling communicate, deethanizing 3 tops, absorption tower of heavily boiling have pipe E directly to communicate with dry gas outlet user, and pipe and topping-up pump 4 are arranged at deethanizing 3 bottoms, absorption tower of heavily boiling, interchanger 5 communicates with the middle part of debutylize rectifying tower 6; Large-scale debutylize rectifying tower 6 bottoms communicate with interchanger 5, bottom reboiler 3-1, interchanger 2, water cooler 7; Divide two strands in water cooler 7 back, a stock-traders' know-how propane evaporator 8, recycle pump 9 and deethanizing 3 tops, absorption tower of heavily boiling communicate, and another gang C communicates with the stable crude storage tank; Debutylize rectifying tower 6 tops are through water cooler 6-3, and backflow surge tank 6-4 bottom liquid advances reflux pump 6-5 and the 6 cats head surge tank 6-4 top gas that communicates, refluxes and communicates with outlet D through propane evaporator 10, surge tank 11 and LPG topping-up pump 12.
Described for small-sized rectifying tower equipment by pressure regulator valve 1, interchanger 2, deethanizing heavily boil absorption tower 3 and bottom reboiler 3-1, topping-up pump 4, interchanger 5, debutylize rectifying tower 6 and bottom reboiler 6-1 and cat head fractional distillating tube 6-2, water cooler 7, propane evaporator 8, recycle pump 9 propane evaporators 10, surge tank 11, LPG topping-up pump 12 is formed, pressure regulator valve 1, interchanger 2 and deethanizing 3 middle parts, absorption tower of heavily boiling communicate, deethanizing 3 tops, absorption tower of heavily boiling have pipe E directly to communicate with dry gas outlet user, and pipe and topping-up pump 4 are arranged at deethanizing 3 bottoms, absorption tower of heavily boiling, interchanger 5 communicates with the middle part of debutylize rectifying tower 6; Small-sized debutylize rectifying tower 6 bottoms communicate with interchanger 5, bottom reboiler official 3-1 interchanger 2, water cooler 7, divide two strands in water cooler 7 back, and a stock-traders' know-how propane evaporator 8, recycle pump 9 and deethanizing 3 tops, absorption tower of heavily boiling communicate; Another gang C communicates with the stable crude storage tank; Debutylize rectifying tower 6 tops communicate with propane evaporator 10, surge tank 11 and LPG topping-up pump 12 outlet D through fractional distillating tube 6-2.
The not stabilize oil stream of described import A can be incorporated among the import A if any the lighter hydrocarbons B that reclaims from Sweet natural gas through liquid phase or gas-liquid two-phase hydrocarbon flow after initial gross separation of oil gas water and the dehydration; Increase to force external reflux at deethanizing 3 tops, absorption tower of heavily boiling, take off heavily boil lighter hydrocarbons in the 3 flash overhead vapour of absorption tower of second in order to absorption, forcing the external reflux medium is the stable crude C of debutylize rectifying tower 6 tower bottom outlets.
The reflux condensation mode of described debutylize rectifying tower 6 tower top outlet gases has two kinds of forms: first kind of overhead gas for large-scale rectifying tower adopts two sections condensation coolings, first section phlegma removes trim the top of column through pump, second section backflow surge tank 6-4 top gas is sent to the LPG storage tank stores by LPG topping-up pump 12 after propane evaporator 10 condensations; Second kind for small-sized rectifying tower employing cat head fractional distillating tube 6-2 condensing reflux.
Described propane evaporator 8 and 10 can be to use vaporizer or the interchanger of other cryogens as low-temperature receiver.
Described interchanger 5, bottom reboiler 3-1 and interchanger 2 should at first be connected with debutylize rectifying tower 6 tower bottom outlets.
The present invention makes stabilization of crude oil, and the process of lighter hydrocarbons recovery and production liquefied petroleum gas (LPG) is simplified greatly, and it is many that art breading equipment has been reduced, and realizing does not have ad hoc stabilization of crude oil system, makes stabilization of crude oil.Realization does not have ad hoc low pressure gas to reclaim the light hydrocarbon recovery system of compression, dehydration, freezing and lime set Separation and Recovery, makes that heavy constituent obtain recycling in the Sweet natural gas.Cancelled low pressure gas energy consumption of compressor rich and influential family, gas dehydration equipment, lime set reclaims and separating device.Both can reduce the area occupied of equipment, save the facility investment expense, and make again and adopt the stabilization of crude oil flashed vapour of traditional nugatory recovery of process for recovering light hydrocarbon to become valuable recyclable lighter hydrocarbons, thereby realized the purpose of energy-saving and emission-reduction.
Description of drawings
Fig. 1 is that the present invention is for large-scale rectifying tower equipment flowsheet;
Fig. 2 is that the present invention is for small-sized rectifying tower equipment flowsheet.
Embodiment
As depicted in figs. 1 and 2, the initial gross separation of process oil gas water, the dehydration of oil stream and the not stabilize oil of removing after mechanical impurity is handled flow A, can mix not among the stabilize oil stream A if any the lighter hydrocarbons B that from Sweet natural gas, reclaims, after pressure regulator valve 1 control pressure and interchanger 2 heat exchange heat up, enter the deethanizing absorption tower 3 of heavily boiling.In order to reduce the C among the deethanizing cat head vent gas body E
3And above heavy constituent, increase pressure external reflux absorption at cat head and reclaim lighter hydrocarbons in the cat head flash steam.C in the tower bottom outlet oil stream that requires
2Content can be controlled by the amount of regulating cat head discharge gas.Boost and the laggard debutylize rectifying tower 6 of interchanger 5 heat exchange from the oil of the tower bottom outlet topping-up pump 4 of flowing through.
In debutylize rectifying tower 6, utilize the rectifying principle to remove C in the oil stream
4And following light constituent, make from tower bottom outlet oil stream to reach stable, vapour pressure was divided into two strands less than the stable oil product of 70KpaA. tower bottom outlet again through after interchanger 5, bottom reboiler 3-1 and interchanger 2 heat exchange when standard was 37.8 ℃ after the storing temp that supercooler 7 is cooled to oily stream to require: one C tank stores of deoiling.Another thigh enters propane evaporator 8 cooling after enter the deethanizing absorption tower 3 of heavily boiling from cat head after recycle pump 9 superchargings.
The condensation process of the gas that comes out from debutanizing tower 6 cats head is by two kinds of forms: first kind is cooled off through two sections condensations for large-scale rectifying tower overhead gas, as shown in Figure 1, first section: through water cooler 6-3, backflow surge tank 6-4 sends to deethanizing by reflux pump 6-5 with phlegma and heavily boils 3 tops, absorption tower as absorption agent; Second section: backflow surge tank 6-4 top gas, can be after the laggard propane evaporators 10 of molecular sieve 13 dehydration (will control propane transpiration cooling temperature more than 0 ℃ without dehydration as gas) be liquefied as LPG with condensation of gas, advance surge tank 11 and LPG topping-up pump 12 is sent to the LPG storage tank stores.Second kind for small-sized rectifying tower, and as shown in Figure 2, the gas that cat head comes out is through the thermal backflow of cat head fractional distillating tube 6-2 condensation as cat head, reflux ratio between 1.0～3.0, main condensation C
5 +Above component is as reflux medium.That come out from cat head fractional distillating tube 6-2 mainly is C
3And C
4Gas, through propane evaporator 10, control propane transpiration cooling temperature is more than 0 ℃, also can inject methyl alcohol frostproofer F after, condensation of gas is liquefied as LPG enters surge tank 11, go to store and sell as LPG product D after entering 12 superchargings of LPG topping-up pump again;
Equipment of the present invention is by pressure regulator valve 1, interchanger 2, deethanizing heavily boil absorption tower 3 and bottom reboiler 3-1, topping-up pump 4, interchanger 5, debutylize rectifying tower 6 and bottom reboiler 6-1 and cat head fractional distillating tube 6-2 or water cooler 6-3, and backflow surge tank 6-4 and reflux pump 6-5, water cooler 7, propane evaporator 8, recycle pump 9, propane evaporator 10, surge tank 11, LPG topping-up pump 12 and molecular sieve 13 are formed.To be pressure regulator valve 1, interchanger 2 communicate with deethanizing 3 middle parts, absorption tower of heavily boiling its flow process feature, deethanizing 3 tops, absorption tower of heavily boiling have pipe E directly to communicate with the dry gas user, and deethanizing 3 bottoms, absorption tower of heavily boiling have to manage and communicate with the middle part of debutylize rectifying tower 6 with topping-up pump 4, interchanger 5.Debutylize rectifying tower 6 bottoms communicate with interchanger 5, bottom reboiler 3-1, interchanger 2, water cooler 7.Divide two strands in water cooler 7 back, a stock-traders' know-how propane evaporator 8, recycle pump 9 and deethanizing 3 tops, absorption tower of heavily boiling communicate; Another gang C communicates with the stable crude storage tank.For small-sized debutylize rectifying tower 6, as shown in Figure 1, top gas communicates with propane evaporator 10, surge tank 11 and LPG topping-up pump 12 outlet D after fractional distillating tube 6-2 condensation.For large-scale debutylize rectifying tower 6, as shown in Figure 2, overhead gas cools off through two sections condensations, first section: through water cooler 6-3, backflow surge tank 6-4, reflux pump 6-5 and deethanizing 3 tops, absorption tower of heavily boiling communicate; Second section: backflow surge tank 6-4 top gas, as moisture higher can after molecular sieve 13 dehydrations, communicating with propane evaporator 10, surge tank 11 and LPG topping-up pump 12 outlet D.
The not stabilize oil stream of import A can be incorporated among the import A if any the lighter hydrocarbons B that reclaims from Sweet natural gas through liquid phase or gas-liquid two-phase hydrocarbon flow after initial gross separation of oil gas water and the dehydration.
Increase to force external reflux at deethanizing 3 tops, absorption tower of heavily boiling, take off heavily boil lighter hydrocarbons in the 3 flash overhead gas of absorption tower of second in order to absorption, forcing the external reflux medium is the stable crude C of debutylize rectifying tower 6 tower bottom outlets.
The reflux condensation mode of debutylize rectifying tower 6 tower top outlet gases has two kinds of forms: first kind for small-sized rectifying tower employing cat head fractional distillating tube 6-2 condensing reflux; Second kind is adopted two sections condensations coolings for the overhead gas of large-scale rectifying tower, and first section phlegma removes trim the top of column through pump, second section backflow surge tank 6-4 top gas is sent to the LPG storage tank stores by LPG topping-up pump 12 after propane evaporator 10 condensations.
Interchanger 5, bottom reboiler 3-1 and interchanger 2 should at first use the stable crude of debutylize rectifying tower 6 tower bottom outlets as thermal source, use other external heat sources when not enough.
Claims (7)
1. three-in-one stable treatment technique for crude oil is characterized in that the not stabilize oil of import (A) flowed through and directly sends into heavily boil absorption tower (3) and debutylize rectifying tower (6) thereafter of deethanizing behind the heat temperature raising and handle; What boil heavily that absorption tower (3) cat head discharges from deethanizing is through absorbing the dry gas (E) after reclaiming lighter hydrocarbons, and discharging what obtain after the heat exchange cooling at the bottom of debutylize rectifying tower (6) tower is that stable crude (C) and tower top outlet obtain liquefied petroleum gas product (D) after condensation and pump supercharging; Finish stabilization of crude oil with a set of equipment flow process, from the flashed vapour of stabilization of crude oil, reclaim the three-in-one stable treatment technique for crude oil of lighter hydrocarbons and production liquefied petroleum gas (LPG).
2. according to claim 1 three-in-one stable treatment technique for crude oil, it is characterized in that for large-scale rectifying tower equipment by pressure regulator valve (1), interchanger (2), deethanizing heavily boil absorption tower (3) and bottom reboiler (3-1), topping-up pump (4), interchanger (5), debutylize rectifying tower (6) and bottom reboiler (6-1) and water cooler 6-3, backflow surge tank (6-4) and reflux pump (6-5), water cooler (7), propane evaporator (8), recycle pump (9), propane evaporator (10), surge tank (11), LPG topping-up pump (12) and molecular sieve (13) are formed, pressure regulator valve (1), interchanger (2) and the deethanizing middle part, absorption tower (3) of heavily boiling communicates, the deethanizing top, absorption tower (3) of heavily boiling has pipe (E) directly to communicate with dry gas outlet user, and pipe and topping-up pump (4) are arranged at the deethanizing bottom, absorption tower (3) of heavily boiling, interchanger (5) communicates with the middle part of debutylize rectifying tower (6); Large-scale debutylize rectifying tower (6) bottom communicates with interchanger (5), bottom reboiler (3-1), interchanger (2), water cooler (7); Divide two strands in water cooler (7) back, a stock-traders' know-how propane evaporator (8), recycle pump (9) and the deethanizing top, absorption tower (3) of heavily boiling communicates, and another thigh (C) communicates with the stable crude storage tank; Debutylize rectifying tower (6) top is through water cooler (6-3), and backflow surge tank (6-4) bottom liquid advances reflux pump (6-5) and (6) cat head surge tank (6-4) top gas that communicates, refluxes and communicates with outlet (D) through propane evaporator (10), surge tank (11) and LPG topping-up pump (12).
3. according to claim 1 three-in-one stable treatment technique for crude oil, it is characterized in that for small-sized rectifying tower equipment by pressure regulator valve (1), interchanger (2), deethanizing heavily boil absorption tower (3) and bottom reboiler (3-1), topping-up pump (4), interchanger (5), debutylize rectifying tower (6) and bottom reboiler (6-1) and cat head fractional distillating tube (6-2), water cooler (7), propane evaporator (8), recycle pump (9) propane evaporator (10), surge tank (11), LPG topping-up pump (12) is formed, pressure regulator valve (1), interchanger (2) and the deethanizing middle part, absorption tower (3) of heavily boiling communicates, the deethanizing top, absorption tower (3) of heavily boiling has pipe (E) directly to communicate with dry gas outlet user, and pipe and topping-up pump (4) are arranged at the deethanizing bottom, absorption tower (3) of heavily boiling, interchanger (5) communicates with the middle part of debutylize rectifying tower (6); Small-sized debutylize rectifying tower (6) bottom communicates with interchanger (5), bottom reboiler (3-1) interchanger (2), water cooler (7), divide two strands in water cooler (7) back, a stock-traders' know-how propane evaporator (8), recycle pump (9) and the deethanizing top, absorption tower (3) of heavily boiling communicates; Another strand (C) communicates with the stable crude storage tank; Debutylize rectifying tower (6) top communicates with propane evaporator (10), surge tank (11) and LPG topping-up pump (12) outlet (D) through fractional distillating tube (6-2).
4. according to claim 1 three-in-one stable treatment technique for crude oil, the not stabilize oil stream that it is characterized in that import (A) can be incorporated in the import (A) if any the lighter hydrocarbons that reclaim from Sweet natural gas (B) through liquid phase or gas-liquid two-phase hydrocarbon flow after initial gross separation of oil gas water and the dehydration; Increase to force external reflux at the deethanizing top, absorption tower (3) of heavily boiling, take off heavily boil lighter hydrocarbons in the flash overhead vapour of absorption tower (3) of second in order to absorption, forcing the external reflux medium is the stable crude (C) of debutylize rectifying tower (6) tower bottom outlet.
5. according to claim 1 three-in-one stable treatment technique for crude oil, the reflux condensation mode that it is characterized in that debutylize rectifying tower (6) tower top outlet gas has two kinds of forms: first kind of overhead gas for large-scale rectifying tower adopts two sections condensation coolings, first section phlegma removes trim the top of column through pump, second section backflow surge tank (6-4) top gas is sent to the LPG storage tank stores by LPG topping-up pump (12) after propane evaporator (10) condensation; Second kind for small-sized rectifying tower employing cat head fractional distillating tube (6-2) condensing reflux.
6. according to claim 1 three-in-one stable treatment technique for crude oil, it is characterized in that propane evaporator (8) and (10) can be to use vaporizer or the interchanger of other cryogens as low-temperature receiver.
7. according to claim 1 three-in-one stable treatment technique for crude oil, it is characterized in that interchanger (5), bottom reboiler (3-1) and interchanger (2) should at first be connected with debutylize rectifying tower (6) tower bottom outlet.
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| CN101735849A (en) * | 2009-12-11 | 2010-06-16 | 辽河石油勘探局 | SAGD (steam-assisted gravity drainage) super-heavy oil high-temperature flash-evaporation dehydration method |
| CN101571340B (en) * | 2009-06-04 | 2011-02-23 | 中国海洋石油总公司 | Air separation method utilizing liquefied natural gas cold energy |
| CN102796580A (en) * | 2012-08-28 | 2012-11-28 | 安瑞科(蚌埠)压缩机有限公司 | Method for stabilizing liquid mixed hydrocarbon |
| CN103484154A (en) * | 2013-09-06 | 2014-01-01 | 中国石油化工股份有限公司 | Condensed water stripped crude oil stabilization method and special device thereof |
| RU2515242C1 (en) * | 2012-11-20 | 2014-05-10 | Общество с ограниченной ответственностью "Научно-исследовательский институт природных газов и газовых технологий - Газпром ВНИИГАЗ" | Procedure for utilisation of flash gas |
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Family Cites Families (4)
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| US5090977A (en) * | 1990-11-13 | 1992-02-25 | Exxon Chemical Patents Inc. | Sequence for separating propylene from cracked gases |
| US6125653A (en) * | 1999-04-26 | 2000-10-03 | Texaco Inc. | LNG with ethane enrichment and reinjection gas as refrigerant |
| CN1137967C (en) * | 2002-03-02 | 2004-02-11 | 中国石化集团洛阳石油化工工程公司 | Method for separating hydrocarbon hydrocracking products |
| US7294749B2 (en) * | 2004-07-02 | 2007-11-13 | Kellogg Brown & Root Llc | Low pressure olefin recovery process |
-
2007
- 2007-11-27 CN CN2007100318476A patent/CN101205484B/en active Active
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| CN101735849A (en) * | 2009-12-11 | 2010-06-16 | 辽河石油勘探局 | SAGD (steam-assisted gravity drainage) super-heavy oil high-temperature flash-evaporation dehydration method |
| CN102796580A (en) * | 2012-08-28 | 2012-11-28 | 安瑞科(蚌埠)压缩机有限公司 | Method for stabilizing liquid mixed hydrocarbon |
| RU2515242C1 (en) * | 2012-11-20 | 2014-05-10 | Общество с ограниченной ответственностью "Научно-исследовательский институт природных газов и газовых технологий - Газпром ВНИИГАЗ" | Procedure for utilisation of flash gas |
| CN103484154B (en) * | 2013-09-06 | 2015-09-23 | 中国石油化工股份有限公司 | Condensed water stripping stabilization of crude oil method and special purpose device thereof |
| CN103484154A (en) * | 2013-09-06 | 2014-01-01 | 中国石油化工股份有限公司 | Condensed water stripped crude oil stabilization method and special device thereof |
| CN104833175A (en) * | 2015-04-15 | 2015-08-12 | 中国海洋石油总公司 | FLNG/FLPG oil gas pretreatment and liquefaction method |
| CN108424788A (en) * | 2017-02-14 | 2018-08-21 | 中国石化工程建设有限公司 | A kind of cracking air separation and technique |
| CN108424788B (en) * | 2017-02-14 | 2020-10-13 | 中国石化工程建设有限公司 | Pyrolysis gas separation device and process |
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| CN111704518B (en) * | 2020-07-08 | 2024-04-02 | 西安长庆科技工程有限责任公司 | Device and method for controlling gaseous ethane condensation rate at top of deethanizer |
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| Publication number | Publication date |
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| CN101205484B (en) | 2012-01-25 |
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