• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Normal paraffins are separated from mixtures of the same with cyclic hydrocarbons having more than six carbon atoms per molecule and/or branched chain hydrocarbons by contacting the mixture at adsorption conditions with an adsorbent comprising silicalite, whereby the normal paraffin is selectively adsorbed. It may then be recovered from the adsorbent by desorption with a desorbent material. Preferably a simulated moving bed countercurrentflowadsorption system is used.
    公开号:SU1431675A3
    申请号:SU823473704
    申请日:1982-07-29
    公开日:1988-10-15
    发明作者:Кулпратипанья Санти；Неузил Вильям
    申请人:Юоп Инк (Фирма)；
    IPC主号:
    专利说明:

    An invention of the method of isolating normal paraffins, more specifically to a method that uses an adsorbent based on crystalline silicon oxide, to separate nororg of highly paraffins from the nasal paraffins and some other structural classes of hydrocarbons,
    The aim of the invention is to increase the speed of the process.
    Example 8 P Ip In the adsorber, silicalite adsorbent is used on an under-WEAKER and Conoco and 75/25 mixture, k-octane and isooctane as a desorbent to measure the adsorption characteristics, retaining capacitance and exchange rate. Silicalite c; L. 8.cc stalled dioxide dioxide with a purity of 99 May, 7, and above and having an average pore size of 5.5 A and: pore volume 18 cm - / g.
    The adsorber consists of a spiral ad.d-: sorbent chamber with a volume of 70 cm, aprn: the presence of an introductory and an outlet section-: goats at opposite ends of the chamber. The chamber is located in a device for temperature control and, besides using the equipment, the following parameters are used for operating the device at a constant predetermined pressure, which saves the components S to the liquid phase; in this case, with 1.; 03 MPa excess, equipment for quantitative and qualitative analysis5 such as refractometers, polarimeters and chromatographs, are connected to the outlet line of the chamber and used for quantitative deactivation or qualitative determination of one or more the numbers of the components of the outlet stream leaving the adsorbent chamber; C. lycalite is filled to equilibrium with the desorbent mixture while passing it through the adsorbent chamber. Makeup. Ko koko contains 27.8 May, 7, normal paraffins CC, (, С,) and 72.8 May:% of other components containing С с: yl benzenes,., 5 - cyclic alkane alkenes, -dicyclo- ; skanYr S .d., - bkcycloalkanes or cycloalkane. 1 and C ,,,, and C .. -methyl-branched a.pcayi Conoco air Absolute UV up to 30% desorbent ;, 1 spray for several minutes at Then pass a stream of deoorbent mixture at 120 ° C and ext
    rakt and raffinate are eluted in the same way as liquid-solid chromatography. The effluent is analyzed continuously as it is received or the samples of the effluent can be periodically collected and subsequently analyzed separately,
    In this experiment, normal paraffins were separated from other components and therefore all of these components were combined. The graph (see drawing) shows five peaks of normal hydrocarbons (-C 4) and one peak for the combined other components.
    Example 2 (comparative) Use commercial molecular sieve inserts using clay as a binder (ca. 20 May, 7c, containing type 5A Ca, and the water content in the sieves is 2 wt.% (Input pore size 5A) The first mixture containing 16% n-tetradecane in isooctane is introduced from one end of the fixed bed, thus contacting a 40 cm layer consisting of these fresh molecular sieves at a pressure of 2070 KPa, a temperature of 23 2 C and liquid flow rate 3 h, When the cavity of the molecules pH Their forces are completely filled with n-tetradecane, a second desorption mixture is introduced, containing 16 wt.% chemically pure n-decane in chemically pure isooctane, under the indicated conditions, in order to ensure the replacement of n-tetradecan inside the cavities of the sieves with n-decane. This is continued until no n-tetradecane is fixed in the effluent stream using gas-liquid chromatography, after which the first mixture is re-introduced until the absence of n-decane is fixed in the effluent stream. As a measure of the sorption rate of n-tetradecane, the degree of change of the concentration gradient is taken when n-tetradecane appears in the output stream.
    Similarly, a change in the concentration gradient from the moment of the appearance of n-decane in the output stream is noted during the sorption of n-decane n-C. The volume of the first mixture, which is required in order to change the amount of n-tetradecane released from the output stream, from 10 to 90 wt.% Of the total amount of this normal paraffin contained in the output stream, can be taken as a measure of sorption rate. n-tetradecane n-C The volume of the second mixture, which is needed to change the amount in the effluent from 10 to 90% by weight of the total amount of normal paraffin contained in the output stream, can be taken as a measure of sorption rate. The volume required to change the concentration from 10 to 90% is called the slope.
    For the above commercially available adsorbent of zeolite 5A, the n-C pass-through slope is 60.0 ml, and for H-Cf it is 12.8 ml, while for n-C, if silicalite is used, it is J9.3 ml, and for nC - 12.6 mm, t, e. Three times the sorption rate on silicalite is greater than in the case of zeolite 5A.
    In addition, it can be noted that the sorption rates of various and paraffins in the case of silicalite are closer to each other than in the case of the adsorbent 5A,
    Form L and Infections
    The method of separating normal paraffin hydrocarbons having 10-4 carbon atoms from hydrocarbon mixtures, also containing isoparaffin and cyclic hydrocarbons having more than six carbon atoms in a molecule, by passing the raw material at a temperature of 120 ° C and pressure, liquid phase, through an adsorbent followed by desorption of adsorbed normal paraffin hydrocarbons, normal paraffin hydrocarbon not contained in the feedstock and having a boiling point different t boiling point of evolved hydrocarbons at AS-IZS C, at a desorption temperature of 120 ° C and a pressure sufficient to maintain the liquid phase, characterized in that, in order to increase the process speed, a silica-based sieve is used as an adsorbent - silicalite.
    权利要求:
    Claims (1)
    [1]
    Claim
    The method of separation of normal paraffin hydrocarbons having ΙΟΙ 4 carbon atoms from hydrocarbon mixtures also containing isoparaffin and cyclic hydrocarbons having more than six carbon atoms in the molecule by passing the raw material at a temperature of 120 ° C and a pressure that ensures the raw materials are maintained. liquid phase, through an adsorbent, followed by desorption of the adsorbed normal paraffinic hydrocarbons with normal paraffin hydrocarbon, not contained in the feedstock and having a boiling point different from the boiling point of the hydrocarbons produced by 48-128 ° C, at a desorption temperature of 120 ° C and a pressure sufficient for maintaining a liquid phase, characterized in that, in order to increase the speed of the process, a molecular sieve based on silica-silicalite is used as an adsorbent.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1431675A3|1988-10-15|Method of separating normal paraffin hydrocarbons
    KR890002141B1|1989-06-21|Serial flow continuous separation process
    EP0271147B1|1991-10-16|Process for isomerization of a hydrocarbon feed stream
    CA1266834A|1990-03-20|Process for separating isoprene
    JPH0776186B2|1995-08-16|Adsorption separation method of para-xylene using tetralin desorbent
    US5276246A|1994-01-04|Process for separating normal olefins from non-normal olefins
    US4791235A|1988-12-13|Process for separating 2,6-dimethylnaphthalene
    US4529828A|1985-07-16|Separation of ortho-xylene
    JPH083077A|1996-01-09|Process for adsorbing and separating ethylbenzene from hydrocarbon having other eight carbon atoms using cesium-exchanged zeolite x
    EP0086035B1|1985-05-29|Process for the separation of ortho aromatic isomers by selective adsorption
    US4298472A|1981-11-03|Process for manufacturing impregnated silicas and the use of these silicas for analysis or purification of industrial products
    EP0549245A1|1993-06-30|Para-xylene adsorptive separation with indan or indan derivatives as heavy desorbent
    US3053913A|1962-09-11|Separation of high molecular weight hydrocarbons with molecular sieves
    US5414192A|1995-05-09|Process for separating linear and branched hydrocarbons using aryl-bridged polysilsesquioxanes
    US4175099A|1979-11-20|Separation and recovery of ethylbenzene from C8 aromatic mixtures using rubidium-X sieves
    US5476985A|1995-12-19|Process for separating linear and branched hydrocarbons using alkylene-bridged polysilsesquioxanes
    US4567309A|1986-01-28|Separation of 1,3-butadiene
    US5396020A|1995-03-07|Process for separating hydrocarbons using aryl-bridged polysilsesquioxanes
    US5220102A|1993-06-15|Process for separating normal olefins from non-normal olefins
    US4442222A|1984-04-10|Adsorbent for separation of para-xylene
    US5132485A|1992-07-21|Adsorptive separation of alpha-olefins and internal olefins
    US3365394A|1968-01-23|Process for separation of mixed hydrocarbons by adsorption
    US4992621A|1991-02-12|Separation of coumarone from indene
    EP0137584B1|1988-06-08|Separation of ethylbenzene from xylenes
    JP2002540178A|2002-11-26|Separation of para-xylene using ether as desorbent
    同族专利:
    公开号 | 公开日
    JPS621678B2|1987-01-14|
    ES8403848A1|1984-04-01|
    EG15831A|1986-12-30|
    KR870001464B1|1987-08-12|
    AT8037T|1984-07-15|
    EP0071477B2|1991-10-02|
    JPS5827789A|1983-02-18|
    KR840000455A|1984-02-22|
    DE3260273D1|1984-07-26|
    US4367364A|1983-01-04|
    ES514500A0|1984-04-01|
    AU557295B2|1986-12-18|
    EP0071477A1|1983-02-09|
    EP0071477B1|1984-06-20|
    AU8659282A|1983-02-03|
    CA1190482A|1985-07-16|
    IN158308B|1986-10-18|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2985589A|1957-05-22|1961-05-23|Universal Oil Prod Co|Continuous sorption process employing fixed bed of sorbent and moving inlets and outlets|
    US2957927A|1957-06-27|1960-10-25|Universal Oil Prod Co|Process for separating normal aliphatic hydrocarbons from hydrocarbon mixtures|
    US3150079A|1960-07-13|1964-09-22|Exxon Research Engineering Co|Separation by selective desorption of silica gel|
    US3239455A|1963-05-13|1966-03-08|Universal Oil Prod Co|Separation of aliphatic paraffins from normally liquid hydrocarbon mixtures|
    GB1009974A|1963-05-13|1965-11-17|British Petroleum Co|Improvements relating to molecular sieve separation processes|
    US3405057A|1966-01-28|1968-10-08|Universal Oil Prod Co|Method for improving molecular sieves|
    GB1454179A|1974-03-20|1976-10-27|British Petroleum Co|Hydrocarbon separation process|
    US4061724A|1975-09-22|1977-12-06|Union Carbide Corporation|Crystalline silica|
    US4006197A|1975-11-19|1977-02-01|Uop Inc.|Process for separating normal paraffins|
    US4309281A|1979-12-19|1982-01-05|Mobil Oil Corporation|Selective sorption by zeolites|
    US4329280A|1981-04-10|1982-05-11|Uop Inc.|Process for separating esters of fatty and rosin acids|US4487688A|1979-12-19|1984-12-11|Mobil Oil Corporation|Selective sorption of lubricants of high viscosity index|
    US4486618A|1981-07-30|1984-12-04|Uop Inc.|Process for separating C6 olefin hydrocarbons|
    US4455444A|1981-07-30|1984-06-19|Uop Inc.|Low temperature process for separating hydrocarbons|
    US4455445A|1982-03-12|1984-06-19|Uop Inc.|Separation of C4 olefins|
    US4425226A|1982-12-10|1984-01-10|Phillips Petroleum Company|Polymerization catalyst and deodorizing agent|
    US4433194A|1983-05-06|1984-02-21|Uop Inc.|Purification of cyclohexane|
    EP0150544B1|1984-01-25|1988-04-13|Uop Inc.|Process for the separation of isobutylene from a normal c4 hydrocarbon|
    JPH0320366B2|1984-01-30|1991-03-19|Uop Inc|
    US4547205A|1984-10-11|1985-10-15|Uop Inc.|Dehydrocyclodimerization process|
    JPH0329768B2|1984-12-03|1991-04-25|
    US4808300A|1987-02-13|1989-02-28|Exxon Research And Engineering Company|Simultaneous removal of aromatics and wax from lube distillate by an adsorption process|
    US4950382A|1987-02-13|1990-08-21|Exxon Research & Engineering Company|Process for improving the low temperature performance of dewaxed oil and formulated oil products|
    US4956521A|1988-10-06|1990-09-11|Uop|Adsorption and isomerization of normal and mono-methyl paraffins|
    US5055634A|1988-10-06|1991-10-08|Uop|Adsorption and isomerization of normal and mono-methyl paraffins|
    US5055633A|1988-10-06|1991-10-08|Uop|Adsorption and isomerization of normal and mono-methyl paraffins|
    US4982052A|1988-12-23|1991-01-01|Texaco Inc.|Separation of a mixture of normal paraffins branched chain paraffins and cyclic paraffins|
    US5132486A|1990-10-09|1992-07-21|Wylie Engineering & Construction, Inc.|Adsorption-desorption separation process for the separation of low and high octane components in virgin naphthas|
    JP2657006B2|1991-02-08|1997-09-24|ユーオーピー|Improved method for adsorptive separation of n-paraffins using a non-n-hydrocarbon prepulse stream|
    US5466364A|1993-07-02|1995-11-14|Exxon Research & Engineering Co.|Performance of contaminated wax isomerate oil and hydrocarbon synthesis liquid products by silica adsorption|
    US6617481B1|1998-12-29|2003-09-09|Uop Llc|Process for producing phenyl-alkanes using an adsorptive separation section|
    US6252127B1|1998-12-29|2001-06-26|Uop Llc|Process for monomethyl acyclic hydrocarbon adsorptive separation|
    US7795483B2|1998-12-29|2010-09-14|Uop Llc|Phenyl-alkane compositions produced using an adsorptive separation section|
    US6468417B1|1999-06-11|2002-10-22|Chevron U.S.A. Inc.|Filtering lubricating oils to remove haze precursors|
    US6222088B1|1999-09-27|2001-04-24|Uop Llc|Monomethyl paraffin adsorptive separation process|
    US6407305B1|2000-09-27|2002-06-18|Uop Llc|Adsorptive separation process for recovery of two paraffin products|
    KR20010079104A|2001-06-13|2001-08-22|지문환|Preparation method of fresh mugwort as a food additive and its blending ratio|
    US6670519B1|2001-10-15|2003-12-30|Uop Llc|Monomethyl paraffin adsorptive separation process|
    KR100645660B1|2001-11-09|2006-11-13|에스케이 주식회사|Process for separating normal paraffins from hydrocarbons and application schemes for the separated hydrocarbons|
    ES2249183B1|2004-09-15|2007-12-01|Universidad Politecnica De Valencia|USE OF MICROPOROUS CRYSTAL MATERIAL OF ZEOLITIC NATURE WITH LTA STRUCTUREIN PROCESSES OF ADSORTION AND SEPARATION OF ORGANIC COMPOUNDS.|
    WO2013160292A1|2012-04-27|2013-10-31|Universiteit Van Amsterdam|Process for separating mixtures comprising straight-chain and branched alkanes by adsorption on zif-77|
    US10570343B2|2016-09-19|2020-02-25|Exxonmobil Research And Engineering Company|Systems and methods for separating classes of paraffinic compounds|
    CN109180413B|2018-08-09|2021-07-27|天津大学|Method and device for separating 1-hexene from Fischer-Tropsch synthetic oil by using reaction separation coupling process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/288,570|US4367364A|1981-07-30|1981-07-30|Process for separating normal paraffins using silicalite adsorbent|
    [返回顶部]