WO2012073618A1 - Système de récupération d'un fractionnement de gpl - Google Patents

Système de récupération d'un fractionnement de gpl Download PDF

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Publication number
WO2012073618A1
WO2012073618A1 PCT/JP2011/074577 JP2011074577W WO2012073618A1 WO 2012073618 A1 WO2012073618 A1 WO 2012073618A1 JP 2011074577 W JP2011074577 W JP 2011074577W WO 2012073618 A1 WO2012073618 A1 WO 2012073618A1
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WO
WIPO (PCT)
Prior art keywords
sponge oil
gas
fraction
lpg
oil
Prior art date
Application number
PCT/JP2011/074577
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English (en)
Japanese (ja)
Inventor
直幸 石渡
宏 依田
利弘 寺田
達之 津久井
Original Assignee
キャメロンジャパン株式会社
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Filing date
Publication date
Application filed by キャメロンジャパン株式会社 filed Critical キャメロンジャパン株式会社
Priority to US13/990,700 priority Critical patent/US20130256093A1/en
Publication of WO2012073618A1 publication Critical patent/WO2012073618A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/12—Liquefied petroleum gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/02—Combustion or pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/46—Compressors or pumps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel

Definitions

  • the present invention relates to an LPG fraction recovery apparatus, and more particularly to an apparatus for effectively using surplus gas generated with the production of crude oil in an oil field.
  • the accompanying gas is generally a gas containing a hydrocarbon having 1 to 5 carbon atoms, and is generated by decompressing hydrocarbon dissolved in crude oil in a high-pressure oil layer by a separator.
  • the accompanying gas is mainly composed of methane and ethane, and is characterized by a low content of components more than propane effective as LPG (Liquid Petroleum Gas).
  • LPG Liquid Petroleum Gas
  • Patent Document 1 discloses a product gas containing carbon dioxide, methane, etc., ethane, propane, and heavy components from natural gas or petroleum-associated gas using a membrane separation method, an absorption separation method, and a distillation separation method. Describes a method for producing NGL (Natural Gas Liquid), which is mainly composed of bismuth.
  • NGL Natural Gas Liquid
  • the present invention has been made in view of the above circumstances, and can efficiently recover an LPG fraction from an accompanying gas, and effectively uses the accompanying gas of an oil field of a scale that cannot be profitable by the conventional liquefaction process.
  • An object of the present invention is to provide an LPG fraction collection device useful for use.
  • the LPG fraction recovery device is a gas containing propane and butane and pressurizes all or a part of surplus gas generated during the production of crude oil, the surplus gas that has been boosted, and sponge oil.
  • a sponge oil transfer pipe discharged from the tower is connected to the deethanizer tower via the sponge oil transfer pipe.
  • the debutane tower separates propane and butane from the sponge oil, and the debutane tower contains propane and butane.
  • Sponge oil is discharged from the LPG fraction discharge pipe and the debutane tower.
  • a sponge oil return pipe for returning the Le in the deethanizer.
  • the content of gas (methane and ethane) having 2 or less carbon atoms can be sufficiently reduced by the treatment of the accompanying gas (surplus gas) in the deethanizer and debutane towers. And the fluid containing the LPG fraction is discharged from the debutane tower.
  • the liquefied LPG fraction can be transported by a normal tank truck or the like, and even if it is an oil field of a scale that is not profitable in the conventional liquefaction process Can be used effectively.
  • the reduction of the fluid having 2 or less carbon atoms is insufficient, it is necessary to prepare a special tank truck having high pressure resistance for transporting the LPG fraction.
  • LNG containing methane as a main component is liquefied by cooling to about ⁇ 160 ° C., whereas the LPG fraction is liquefied relatively easily by pressurization.
  • the “LPG fraction” means a fraction containing propane (C3) and butane (C4) as main components and a sufficiently low content of methane (C1) and ethane (C2).
  • it is a fraction mainly composed of propane and butane, and the total amount of methane and ethane is about 5 mol% or less and having 5 or more carbon atoms (hereinafter referred to as “heavy fraction”).
  • the fraction having a total amount of about 30 mol% or less is an LPG fraction.
  • the surplus gas contains a heavy fraction
  • the heavy fraction is dissolved in sponge oil in the deethanizer together with propane and butane, and then separated and recovered from the sponge oil in the debutanizer.
  • the above-mentioned deethanizer and debutanizer can be operated if there is a heating means and a means for circulating sponge oil. Therefore, in comparison with a cryogenic separation apparatus that requires high cooling in terms of operating cost and construction cost. This has the advantage of being easy to install in oilfield plants.
  • Sponge oil here means oil in which hydrocarbons having 3 or more carbon atoms dissolve in the deethanizer.
  • the sponge oil may be, for example, jet fuel or kerosene, a fraction equivalent to jet fuel or kerosene, a mixed hydrocarbon having 7 to 16 carbon atoms, or a carbon having 10 to 14 carbon atoms. Normal paraffin or isoparaffin can be used.
  • the compressor is preferably driven by a motor or gas engine that uses surplus gas as fuel.
  • the LPG fraction recovery device includes a first circulation pipe that branches from the middle of the sponge oil transfer pipe and returns a part of the sponge oil from the deethanizer to the deethanizer, and a middle of the first circulation pipe.
  • a first heating tube through which the fluid flows.
  • the LPG fraction collection device includes a second circulation pipe that branches from the middle of the sponge oil return pipe and returns a part of the sponge oil from the debutane tower to the debutane tower, and is arranged in the middle of the second circulation pipe. And a second reboiler provided with a second main body for containing sponge oil, and a fluid that is provided to pass through the second main body and is heated by combustion of surplus gas. It is preferable to have the 2nd heating tube which flows.
  • the LPG fraction recovery device further includes a depentane tower which is supplied with a fraction having 3 or more carbon atoms from the debutane tower through the LPG fraction discharge pipe and separates a fraction having 5 or more carbon atoms from the fraction. Good.
  • a depentane tower which is supplied with a fraction having 3 or more carbon atoms from the debutane tower through the LPG fraction discharge pipe and separates a fraction having 5 or more carbon atoms from the fraction. Good.
  • a collection device is provided.
  • the LPG fraction collection device 50 shown in FIG. 1 is for obtaining an LPG fraction from surplus gas such as accompanying gas generated in connection with production of crude oil in an oil field.
  • the LPG fraction collection device 50 is intended for processing all or part of the surplus gas, and the gas to be treated is supplied through the pipe L2 branched from the pipe L1 for transferring the surplus gas to the flare stack (not shown). It has come to be.
  • the composition of the associated gas varies depending on the oil field, but the associated gas having the following composition range can be treated.
  • Methane (C1) 30 to 85 mol%
  • Ethane (C2) 10 to 50 mol%
  • Propane (C3) 1 to 40 mol%
  • Butane (C4) 1 to 40 mol%
  • Pentane (C5) 1 to 20 mol%
  • the LPG fraction recovery apparatus 50 mainly includes two-stage compressors 11 and 12 that pressurize the gas to be processed, and a deethanizer 20 that separates a gas having 2 or less carbon atoms from the gas to be processed using sponge oil.
  • a sponge oil return pipe L7 for returning sponge oil from the debutanizer 30 to the deethanizer 20.
  • the compressors 11 and 12 are for boosting the low-pressure gas (for example, 100 to 250 kPa) to be processed in the pipe L2 to about 500 to 2000 kPa.
  • the compressors 11 and 12 are preferably driven by a gas engine GE that uses surplus gas as fuel.
  • cooling devices 11a and 12a and separators 13, 14, and 15 for separating water and condensate from the gas to be processed are installed. Suitable cooling devices include air-cooled type and water-cooled type, and an air fin cooler and a water circulation type cooler are particularly suitable in an area where water is not abundant.
  • the deethanizer 20 is made to gas-liquid contact the gas to be processed and the sponge oil pressurized by the compressors 11 and 12 to dissolve propane, butane and heavy fractions contained in the gas to be processed in the sponge oil, This is for separating methane and ethane (gas having 2 or less carbon atoms) from the gas to be treated.
  • Sponge oil is supplied from a sponge oil return pipe L7 connected above the deethanizer 20. Methane and ethane that are not absorbed by the sponge oil are discharged from the pipe L4 connected to the top of the deethanizer 20 and sent to the flare stack.
  • the sponge oil that has absorbed propane, butane, and heavy fraction is discharged from a sponge oil transfer pipe L5 connected to the bottom of the deethanizer 20.
  • a reboiler is provided at the bottom of the deethanizer 20 so that C1 and C2 absorbed by the sponge oil are efficiently removed from the sponge oil.
  • the temperature in the column 20 is preferably 100 to 220 ° C., and the pressure is preferably 700 to 2000 kPa.
  • the sponge oil transfer pipe L5 has a circulation pipe (first circulation pipe) L5a branched from the middle, and a part of the sponge oil is returned to the deethanizer 20 through the circulation pipe L5a. Can be done.
  • a reboiler (first reboiler) 16 is disposed in the middle of the circulation pipe L5a. The circulation pipe L5a and the reboiler 16 can more reliably reduce the amounts of methane and ethane flowing into the debutane tower 30 together with the sponge oil.
  • the reboiler 16 is provided with a main body (first main body) 16a for containing sponge oil, and oil heated by combustion of surplus gas flows so as to pass through the main body 16a. And a heating tube (first heating tube) 16b.
  • the sponge oil in the main body portion 16a is heated in contact with the outer surface of the heating pipe 16b, and is returned to the deethanizer 20 in a gas-liquid mixed phase state.
  • the debutane tower 30 is connected to the tip of a sponge oil transfer pipe L5 in the middle, and is for separating the LPG fraction from the sponge oil supplied through this pipe L5.
  • the LPG fraction vaporized from sponge oil in the debutane tower 30 is discharged from an LPG fraction discharge pipe L6 connected to the top of the debutane tower 30.
  • the sponge oil from which the LPG fraction has been separated is discharged from a sponge oil return pipe L7 connected to the bottom of the debutane tower 30.
  • the temperature in the tower 30 is preferably 150 to 300 ° C., and the pressure is preferably 500 to 1500 kPa.
  • the sponge oil return pipe L7 has a circulation pipe (second circulation pipe) L7a branched from the middle, and a part of the sponge oil is returned to the debutane tower 30 through the circulation pipe L7a. Can be done.
  • a reboiler (second reboiler) 26 is disposed in the middle of the circulation pipe L7a. With the circulation pipe L7a and the reboiler 26, the amount of the LPG fraction returned to the deethanizer 20 together with the sponge oil can be reduced to improve the yield of the LPG fraction.
  • a heat exchanger 22 and a cooling device 23 are provided in the middle of the sponge oil return pipe L7.
  • the reboiler 26 has the same configuration as the reboiler 16 shown in FIG.
  • the reboiler 26 includes a main body portion (second main body portion) 26a that stores sponge oil, and a heating pipe (second heating portion) that is provided so as to pass through the main body portion 26a and through which oil heated by combustion of surplus gas flows. Tube) 26b.
  • the sponge oil in the main body portion 26a is heated in contact with the outer surface of the heating pipe 26b, and is returned to the debutane tower 30 in a gas-liquid mixed phase state.
  • surplus gas combustion gas may flow directly into the heating pipe 26b.
  • the LPG fraction discharge pipe L6 is for discharging the LPG fraction from the debutane tower 30 and transferring it to the separator 32.
  • a cooling device 31 is provided in the middle of the pipe L6.
  • all or part of the LPG fraction condensed by cooling is temporarily stored.
  • the LPG fraction that has undergone the treatment in the separator 32 is transferred to the LPG tank 45 through the pipe L9.
  • the LPG fraction can be stored under conditions of a temperature of 30 to 60 ° C. and a pressure of 500 to 1800 kPa.
  • the purity of a LPG fraction can be raised by refluxing a part of LPG fraction discharged
  • the LPG fraction recovery apparatus 50 methane and ethane are efficiently removed from the accompanying gas, and an LPG fraction exceeding 99% by volume (if the propane and butane and the accompanying gas contain a fraction having 5 or more carbon atoms, (Including fractions) can be stably obtained.
  • the LPG fraction having such a composition can be transported by a normal tank truck. For this reason, even in areas where small and medium-sized oil fields are scattered, the LPG fraction collection device 50 is installed in each oil field and each gathering station, and the LPG fraction is collected from each LPG tank 45 to the refining plant and collected in the LPG. Can be commercialized. In the refining plant, a process such as removing a fraction having 5 or more carbon atoms remaining in the LPG fraction is performed. In some cases, the LPG fraction may be transported by a pipeline, a tanker or the like instead of the tank truck.
  • the LPG fraction recovery device 50 can obtain the LPG fraction contained in the accompanying gas at a recovery rate of 70 to 99%, and by using flare gas (surplus gas) as an energy source, The feature is that the energy supply from can be zero. Furthermore, it is also possible to separate C1 to C2 and C3 to C6 without generating a freezing point or a cryogenic temperature by a refrigerator or self-freezing.
  • flare gas surplus gas
  • the LPG fraction collection device 50 can also be applied to offshore oil fields.
  • the LPG fraction recovered from the associated gas may be mixed with a crude oil line or a condensate line (C4, C5 equal fraction) of the oil mining equipment.
  • the LPG fraction can be used as a product raw material.
  • the LPG fraction collection apparatus 60 shown in FIG. 3 includes a depentane tower 40 that separates a fraction having 5 or more carbon atoms (C5 +) from the LPG fraction at the rear stage of the debutane tower 30.
  • the LPG fraction collection device 60 has the same configuration as the LPG fraction collection device 50 except that it includes a depentane tower 40. According to the LPG fraction collection device 60, an LPG fraction substantially consisting of propane and butane can be obtained, and can be adapted to a commercially available LPG standard.
  • the case where a two-stage compressor is provided to increase the pressure of the gas to be processed is illustrated, but the number of stages of the compressor is not limited to two, and may be, for example, one.
  • the compressor is not limited to one driven by the gas engine GE, and for example, a compressor driven by a motor may be adopted.
  • the motor preferably uses an engine generator that uses surplus gas as fuel.
  • a collection device is provided.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un système de récupération d'un fractionnement de GPL comprenant : un compresseur qui augmente le gaz en excès tel qu'un gaz associé ; un dééthaniseur qui dissout le propane et le butane contenus dans le gaz en excès dans une huile absorbante, tout en isolant le gaz ayant un indice de carbone inférieur ou égal à 2 du gaz en excès ; un tuyau de transfert d'huile absorbante qui évacue l'huile absorbante hors du dééthaniseur ; un débutaniseur qui isole le propane et le butane de l'huile absorbante ; un tuyau d'évacuation du fractionnement de GPL qui évacue le fractionnement contenant le propane et le butane hors du débutaniseur ; et un tuyau de retour d'huile absorbante qui renvoie l'huile absorbante du débutaniseur vers le dééthaniseur.
PCT/JP2011/074577 2010-12-02 2011-10-25 Système de récupération d'un fractionnement de gpl WO2012073618A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US13/990,700 US20130256093A1 (en) 2010-12-02 2011-10-25 LPG Fractionation Recovery System

Applications Claiming Priority (2)

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JP2010269374A JP4745456B1 (ja) 2010-12-02 2010-12-02 Ｌｐｇ留分回収装置
JP2010-269374 2010-12-02

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Cited By (2)

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US8841499B2 (en) 2012-11-08 2014-09-23 Uop Llc Methods and apparatuses for isomerization of paraffins
CN104132504A (zh) * 2014-07-17 2014-11-05 西安长庆科技工程有限责任公司 一种从井场天然气回收混烃的系统及方法

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JP2014122284A (ja) * 2012-12-21 2014-07-03 Japan Petroleum Exploration Co Ltd フレアガスからの粗ｌｐｇの回収設備
US10717937B2 (en) 2015-09-25 2020-07-21 Haldor Topsøe A/S Process for LPG recovery
US10344219B2 (en) * 2015-10-29 2019-07-09 Process Consulting Services, Inc. Crude stabilizer process
CN110498147A (zh) * 2019-09-17 2019-11-26 滕州市森河建筑工程有限公司 一种石油储油罐用外冷式油气安全回收装置
CN111575042B (zh) * 2020-06-11 2022-06-24 中国人民解放军军事科学院国防工程研究院工程防护研究所 一种组合油气回收装置及回收工艺
US20230069964A1 (en) * 2021-09-09 2023-03-09 Gas Technology Institute Production of liquefied petroleum gas (lpg) hydrocarbons from carbon dioxide-containing feeds

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JP2637611B2 (ja) * 1990-07-04 1997-08-06 三菱重工業株式会社 Ｎｇｌまたはｌｐｇの回収方法
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JP2004536176A (ja) * 2001-06-29 2004-12-02 エクソンモービル アップストリーム リサーチ カンパニー メタン豊富な加圧液体混合物からエタン及びより重い炭化水素を回収する方法
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8841499B2 (en) 2012-11-08 2014-09-23 Uop Llc Methods and apparatuses for isomerization of paraffins
CN104132504A (zh) * 2014-07-17 2014-11-05 西安长庆科技工程有限责任公司 一种从井场天然气回收混烃的系统及方法

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JP4745456B1 (ja) 2011-08-10
JP2012116981A (ja) 2012-06-21

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