WO2008120921A1 - Separation of olefins from olefins/paraffins mixed gas - Google Patents

Separation of olefins from olefins/paraffins mixed gas Download PDF

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Publication number
WO2008120921A1
WO2008120921A1 PCT/KR2008/001764 KR2008001764W WO2008120921A1 WO 2008120921 A1 WO2008120921 A1 WO 2008120921A1 KR 2008001764 W KR2008001764 W KR 2008001764W WO 2008120921 A1 WO2008120921 A1 WO 2008120921A1
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WO
WIPO (PCT)
Prior art keywords
olefins
adsorption
tower
paraffins
desorbents
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.)
Ceased
Application number
PCT/KR2008/001764
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English (en)
French (fr)
Inventor
Jong-Nam Kim
Jong-Ho Park
Seong-Jun Lee
Min-Su Ko
Hee Tae Beum
Jongkee Park
Chang Hyun Ko
Sang Sup Han
Soon-Haeng Cho
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Korea Institute of Energy Research KIER
SK Energy Co Ltd
Original Assignee
Korea Institute of Energy Research KIER
SK Energy Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Korea Institute of Energy Research KIER, SK Energy Co Ltd filed Critical Korea Institute of Energy Research KIER
Priority to JP2010500835A priority Critical patent/JP5414664B2/ja
Priority to CN200880010759.0A priority patent/CN101652339B/zh
Priority to US12/593,249 priority patent/US8436223B2/en
Priority to EP08741021.3A priority patent/EP2134667B1/en
Publication of WO2008120921A1 publication Critical patent/WO2008120921A1/en
Anticipated expiration legal-status Critical
Priority to US13/855,957 priority patent/US9034185B2/en
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B01D2257/7022—Aliphatic hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B01D2259/40054—Recycled product or process gas treated before its reuse
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/4006—Less than four
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/40062—Four
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/40067—Seven
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/403—Further details for adsorption processes and devices using three beds

Definitions

  • the present invention relates to a method for the separation of C4 olefins (butene-1, trans-2-butene, cis-2-butene, etc.) and C4 paraffins (normal butane, isobutane, etc.) from a C4 hydrocarbon mixed gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc.
  • C4 olefins butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc.
  • U.S. patent 4,718,986(1988) discloses a process for producing butene-1 with a purity of more than 99wt% from the C4 hydrocarbon mixture of butene- 1/isobutane/normal butane/butene-2 by using two distillation towers.
  • the C4 mixture is introduced into the first distillation tower to remove isobutane from the top of the tower.
  • the lower stream from the first distillation tower is introduced into the second distillation tower, obtaining butene- 1 with a purity of 99wt% from the top of the second tower and discharging a mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower.
  • the existing vapor adsorption separation process for separating a mixture of olefins/paraffins consists of an adsorption step of introducing the mixture of olefins/paraffins into an adsorption tower to adsorb olefins from the mixture and discharge paraffins, and a desorption step of desorbing the ad sorbed olefins by using desorbents.
  • olefins are produced by separation of the mixture of olefins/ desorbents resulting from the desorption step via distillation.
  • a small quantity of paraffins is generally adsorbed together with olefins onto olefin selective adsorbents, it is highly difficult to obtain C4 olefins with a high purity of more than 95wt% by a process consisting only of an adsorption step and a desorption step.
  • Technical Solution [9]
  • the method of the present invention comprises a sequence of adsorption step - olefin rinse step - desorption step.
  • olefin rinse step a portion of high purity C4 olefins resulting from the distillation of olefins/desorbents (desorption agents) is introduced into the adsorption tower where the adsorption step was completed and thus a small quantity of C4 paraffins adsorbed together with C4 olefins is removed from the adsorption tower so that high purity olefin is obtained at the next desorption step.
  • the present invention achieves an effect that the concentration of olefins in the C4 olefin product increases through the reduction of the concentration of paraffins (ex., isobutane, normal butane, etc.), by introducing a olefin rinse step into a separation process of C4 olefins (butene-1, trans-2-butene, cis-2-butene, etc.) and C4 paraffins (normal butane, isobutane, etc.) from a C4 hydrocarbon mixed gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc.
  • FIG. 1 is a schematic view of the apparatus of obtaining high purity olefins from a mixture gas of C4 olefins/paraffins according to the present invention.
  • the apparatus of the present invention comprises three adsorption towers (AD-I, AD-2 and AD-3) for separating C4 olefins via selective adsorption and two distillation towers (Dl and D2) for separating C4 olefins/desorbents and C4 paraffins/desorbents respectively.
  • Fig. 2 is a table showing a cycle sequence of the process consisting of seven steps.
  • Fig. 3 is a table showing a cycle sequence of the process composed of four steps.
  • Fig. 4 is a table showing a cycle sequence of the process composed of three steps
  • Fig. 5 is a graph of equilibrium adsorption isotherms of olefin-selective adsorbents, i.e., jT-complex adsorbents.
  • Fig. 6 is a graph of equilibrium adsorption isotherms of olefin-selective adsorbents, i.e., type 13X zeolite adsorbents. Best Mode for Carrying Out the Invention
  • the object of the present invention is to provide a method of separating olefins in high yield and purity from a mixture gas of C4 olefins/paraffins, with a reduced consumption of energy, and an apparatus for practicing the method.
  • the present invention provides a method for separating C4 olefins from a mixture gas composed of C4 olefins/paraffins by performing an adsorption separation process composed of repeated sequential adsorption, olefin rinse and desorption steps in such a way of performing displacement desorption with desorbents, in an apparatus composed of several adsorption towers loaded with adsorbents which adsorb olefins selectively and two distillation towers (one distillation tower for the separation of olefins/ desorbents and another distillation tower for the separation of paraffins/desorbents), which comprises
  • the adsorption step for introducing the mixture gas of C4 olefins/paraffins into the adsorption towers loaded with olefin selective adsorbent to adsorb olefins and discharge non-adsorbed paraffins and the desorbents retained in the adsorption tower to the outlet of the adsorption tower;
  • the C4 olefin rinse step to remove a small amount of paraffins adsorbed together with olefins on the adsorbents by introducing a portion of high purity C4 olefins resulting from the distillation process of olefins/desorbents into the adsorption tower after the completion of the adsorption step and thus increasing the purity of olefins ;
  • each adsorption towers are operated to perform the different steps with each other at the same time point
  • the method of the present invention further includes a cocurrent depres- surization step of discharging the paraffin component residue present in the adsorption towers before the olefin rinse step.
  • the method of the present invention further includes a pressure equalization step at which the paraffin components present in the interior of the adsorption tower after the completion of the adsorption step is transferred to the another adsorption tower which just completed the desorption step by connecting the two adsorption towers so that the pressure of the adsorption towers becomes equalized,
  • the method of the present invention further includes a cocurrent de- pressurization step of discharging the paraffin components present in the adsorption towers after the pressure reduction through the pressure equalization step, and a pres- surization step which pressurize the adsorption tower to the adsorption pressure by in- troducing the mixture gas of C4 olefins/paraffins into the adsorption tower partially pressurized through the pressure equalization step.
  • olefin selective adsorbents for use in the method of the present invention is ⁇ -complex adsorbent forming ⁇ -complex selectively with olefins, type X zeolite or type Y zeolite, and preferably type 13X zeolite.
  • the adsorbent for use in the method of the present invention is C5 hydrocarbon or C6 hydrocarbon.
  • the desorbent separated from the olefin/desorbent distillation tower and the paraffin/desorbent distillation tower is recirculated into adsorption tower.
  • the operating pressure of the adsorption tower in the C4 olefin/paraffin separation process is 1 to 10 atm (absolute pressure) and the temperature is 20 to 150°C.
  • the present invention also provides an apparatus for the separation of C4 olefins from a mixture gas of C4 olefins/paraffins, by carrying out repeated sequential adsorption, olefin rinse and desorption steps in such a way of performing displacement desorption with the desorbents to separate C4 olefins from the mixture gas, in three adsorption towers (AD-I, AD-2 and AD-3) loaded with adsorbents which adsorb olefins selectively and two distillation towers (one distillation tower (D2) for the separation of olefins/desorbents and another distillation tower (Dl) for the separation of paraffins/desorbents), which comprises
  • the adsorption tower (AD-I) in which the bottom of the tower is connected with the feeding conduit (1) for the mixture gas of C4 olefins/paraffins through the valve (Ia), with the C4 olefin/desorbent discharging conduit (2) through the valve (2a) which is connected to the distillation tower (D2), and with the conduit (3) through the valve (3a) which feeds an amount of C4 olefins produced by the distillation tower (D2), and in which the top of the tower is connected with the conduit (4) through the valve (4a) which introduces paraffins and deserbents from the olefin rinse step into the distillation tower (Dl), with the conduit (5) through the valve (5a) which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower (Dl), and with the conduit (6) through the valve (6a) which feeds the desorbents into the adsorption tower;
  • distillation tower (Dl) which separates C4 paraffins and desorbents introduced from the adsorption towers (AD-I, AD-2 and AD-3);
  • distillation tower (D2) which separates C4 olefins and desorbents introduced from the adsorption towers (AD-I, AD-2 and AD-3).
  • the apparatus of the present invention further includes the valve (7) in the conduit (4) connected to the distillation tower (Dl).
  • the valve (7) in the conduit (4) connected to the distillation tower (Dl).
  • FIG. 1 is a schematic view of the apparatus of separating C4 olefin from a mixture gas of C4 olefins/paraffins according to the present invention.
  • the apparatus comprises three adsorption towers for separating C4 olefins via selective adsorption and two distillation towers for separating C4 olefins/desorbents and C4 paraffins/desorbents respectively.
  • the basic process of the adsorption tower used in the present invention includes an adsorption step of selectively adsorbing C4 olefins from the gas mixture, a C4 olefin rinse step of removing a small amount of C4 paraffins adsorbed together with C4 olefins; and a C4 olefin desorption step using the desorbents and the process further can includes a pressure equalization step, a cocurrent depressurization step, and a pressurization step.
  • the desorbent discharged from the adsorption step along with olefins or paraffins is separated in the distillation tower and then recycled into the adsorption tower.
  • the preferable desorbents is C5 hydrocarbon or C6 hydrocarbon which has a large difference in boiling point from that of the C4 mixture.
  • the mixture gas containing C4 olefins/paraffins is introduced into the adsorption tower (AD-I) loaded with olefin selective adsorbents through the conduit (1) and valve (Ia) to adsorb C4 olefins thereon (adsorption step), and the olefin free paraffin stream separated from the mixture is introduced together with the desorbents retained in the adsorption tower before the adsorption step into the distillation tower (Dl) through the conduit (5) and the valve (5a) to separate paraffins and desorbents.
  • the adsorption tower (AD-2) carries out the step (desorption step) of desorbing olefin components with the desorbent while the adsorption tower (AD-I) carries out the adsorption step.
  • the desorbents used in the desorption step is obtained from the bottoms of the distillation tower (Dl) and the distillation tower (D2) and is introduced into adsorption tower (AD-2) through the conduit (6) and the valve (6b).
  • the olefins discharged with the desorbents is introduced into the distillation tower (D2) through the valve (2a) and the conduit (2) to separate the olefins and the desorbents.
  • the adsorption tower (AD-3) is provided with a portion of the olefins separated from the distillation tower (D2) through the conduit (3) and the valve (3c) to remove a small amount of paraffins adsorbed together with the olefins for the improvement of the purity of olefins (C4 olefin rinse step).
  • the gas discharged from the adsorption tower (AD-3) is introduced into the distillation tower (Dl) through the valve (4c) and the conduit (4).
  • the adsorption tower (AD-I) at high pressure which just carried out the adsorption step is connected with the adsorption tower (AD-2) at low pressure through the valve (4a) and the conduit (4) and thus a process (pressure equalization step) that allows the pressures of both towers to be in the same pressure is carried out.
  • the valve (7) is closed.
  • the adsorption tower (AD-3) after the rinse step carries out a desorption step of recovering olefins by introducing the desorbents thereto through the conduit (6) and the valve (6c).
  • the olefins discharged together with the desorbents from the adsorption tower (AD-3) is sent to the distillation tower (D2) through the valve (2c) and the conduit (2) and thus separated from the desorbent.
  • the adsorption tower (AD-I) after the pressure equalization step is depressurized through the valve (4a) and the conduit (4), and at that time, the discharged gas is introduced into the distillation tower (Dl) (cocurrent depressurition step).
  • a C4 mixture gas is introduced into the adsorption tower (AD-2) through the conduit (1) and the valve (Ib) and the adsorption tower (AD-2) carries out a step (pressurization step) of increasing the pressure to the adsorption pressure.
  • the adsorption tower (AD-3) continues to carry out the desorption step.
  • the adsorption tower (AD-I) which just finished the cocurrent depressurization step carry out a C4 olefin rinse step, the adsorption tower (AD-2) carries out the adsorption step, and the adsorption tower (AD-3) continues to carry out the desorption step.
  • each adsorption tower carry out a sequential adsorption step - pressure equalization step - cocurrent depressurization step - C4 olefin rinse step - desorption step - pressure equalization step - pressurization step continuously.
  • the pressure equalization step, the cocurrent depressurization step or the pressurization step can be omitted from the constitution of the process depending on the processing pressure of the adsorption step.
  • Fig. 5 and Fig. 6 show the adsorption isotherms of the olefin selective adsorbents which can be loaded on the adsorption tower carrying out the method of the present invention.
  • the adsorbents for use in the method of the present invention is ⁇ -complex adsorbent forming ⁇ -complex selectively with olefins, type X zeolite or type Y zeolite.
  • Example 2 [60] Table 5 is a result from the experiment conducted with cycle sequence without the pressure equalization step as shown in Fig. 3.
  • Example 3 [64] Table 6 is a result from the experiment performed with the cycle sequence of adsorption step - C4 olefin rinse step - desorption step without the pressure equalization step and the cocurrent depressurization setp as shown in Fig. 4.
  • the present invention is useful for obtaining the C4 olefins with the high purity of more than 95 wt% by introducing a C4 olefin rinse step to reduce the concentration of C4 paraffins (isobutane, normal butane, etc.) in the C4 olefin product, in the separation of C4 olefins (butene-1, trans-2-butene, cis-2-butene, etc.) and C4 paraffins (normal butane, isobutane, etc.) from a C4 hydrocarbon mixed gas including butene-1, trans- 2-butene, cis-2-butene, normal butane, isobutane, etc., as proved in the Examples of the present invention,

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation Of Gases By Adsorption (AREA)
PCT/KR2008/001764 2007-03-29 2008-03-28 Separation of olefins from olefins/paraffins mixed gas Ceased WO2008120921A1 (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
JP2010500835A JP5414664B2 (ja) 2007-03-29 2008-03-28 オレフィン／パラフィン混合気体からオレフィンを分離する技術
CN200880010759.0A CN101652339B (zh) 2007-03-29 2008-03-28 烯烃从烯烃/烷烃混合气体中的分离
US12/593,249 US8436223B2 (en) 2007-03-29 2008-03-28 Separation of olefins from olefins/paraffins mixed gas
EP08741021.3A EP2134667B1 (en) 2007-03-29 2008-03-28 Separation of olefins from olefins/paraffins mixed gas
US13/855,957 US9034185B2 (en) 2007-03-29 2013-04-03 Separation of olefins from olefins/paraffins mixed gas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR10-2007-0030970 2007-03-29
KR1020070030970A KR100822847B1 (ko) 2007-03-29 2007-03-29 올레핀/파라핀 혼합가스에서 올레핀 분리 기술

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US12/593,249 A-371-Of-International US8436223B2 (en) 2007-03-29 2008-03-28 Separation of olefins from olefins/paraffins mixed gas
US13/855,957 Division US9034185B2 (en) 2007-03-29 2013-04-03 Separation of olefins from olefins/paraffins mixed gas

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WO2008120921A1 true WO2008120921A1 (en) 2008-10-09

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PCT/KR2008/001764 Ceased WO2008120921A1 (en) 2007-03-29 2008-03-28 Separation of olefins from olefins/paraffins mixed gas

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US (1) US8436223B2 (enExample)
EP (1) EP2134667B1 (enExample)
JP (2) JP5414664B2 (enExample)
KR (1) KR100822847B1 (enExample)
CN (1) CN101652339B (enExample)
WO (1) WO2008120921A1 (enExample)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013536223A (ja) * 2010-08-26 2013-09-19 コリア インスティチュート オブ エナジー リサーチ 硬質オレフィンの分離のための置換脱着工程
JP2013540707A (ja) * 2010-08-26 2013-11-07 コリア インスティチュート オブ エナジー リサーチ 流動接触分解排ガスからのエチレンの回収方法及び装置
US8889942B2 (en) 2010-12-23 2014-11-18 Kellogg Brown & Root Llc Integrated light olefin separation/cracking process
EP2148847B1 (en) * 2007-04-25 2016-03-09 Korea Institute of Energy Research Production of high purity butene-1 from c4 olefins/paraffins mixed gas
WO2018116091A1 (en) 2016-12-21 2018-06-28 Sabic Global Technologies B.V. Process to produce olefins from a catalytically cracked hydrocarbons stream

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Publication number Priority date Publication date Assignee Title
US9034185B2 (en) 2007-03-29 2015-05-19 Korea Institute Of Energy Research Separation of olefins from olefins/paraffins mixed gas
KR100822847B1 (ko) * 2007-03-29 2008-04-16 한국에너지기술연구원 올레핀/파라핀 혼합가스에서 올레핀 분리 기술
WO2009110492A1 (ja) 2008-03-07 2009-09-11 住友精化株式会社 オレフィンの精製方法および精製装置
CN101993329A (zh) * 2010-10-18 2011-03-30 天津市泰旭物流有限公司 一种采用气相状态下采用分子筛吸附方法提纯制备丁烯的技术
KR101801387B1 (ko) 2015-10-01 2017-11-24 한국생산기술연구원 클러스레이트 화합물을 이용한 올레핀-파라핀 분리 장치 및 방법
KR101899036B1 (ko) 2016-11-09 2018-10-29 에스케이가스 주식회사 올레핀 함유 혼합가스로부터 경질 올레핀 분리방법
KR102044877B1 (ko) * 2016-11-09 2019-11-14 한국에너지기술연구원 일산화탄소 고선택성 흡착제 및 이의 제조방법
KR101985784B1 (ko) 2017-09-13 2019-06-04 연세대학교 산학협력단 이산화탄소를 이용한 올레핀과 파라핀의 분리 공정
KR102017863B1 (ko) * 2017-12-15 2019-09-03 연세대학교 산학협력단 올레핀과 파라핀의 순환 분리 공정
EP3898560A1 (en) * 2018-12-18 2021-10-27 SABIC Global Technologies B.V. Separation of olefin components from a mixture of butanes and butenes using distillation and adsorbents

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US4362537A (en) 1981-02-27 1982-12-07 Union Carbide Corporation Method for the removal of polymer from a purge medium in a monoolefin adsorption - desorption separation process
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JP2013536223A (ja) * 2010-08-26 2013-09-19 コリア インスティチュート オブ エナジー リサーチ 硬質オレフィンの分離のための置換脱着工程
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EP2134667A1 (en) 2009-12-23
KR100822847B1 (ko) 2008-04-16
JP2014051496A (ja) 2014-03-20
CN101652339A (zh) 2010-02-17
JP2010532316A (ja) 2010-10-07
EP2134667A4 (en) 2011-03-02
EP2134667B1 (en) 2016-03-16
US20100048971A1 (en) 2010-02-25
US8436223B2 (en) 2013-05-07
CN101652339B (zh) 2014-10-01

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