• 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:
    Process for solvent transmission from an extract/solvent mixture to a feed to be extracted, by passing the feed along one side of a membrane and the extract/solvent mixture along the other side thereof.
    公开号:SU1282822A3
    申请号:SU833561498
    申请日:1983-03-02
    公开日:1987-01-07
    发明作者:Джордж Альберт Биттер Йохан
    申请人:Шелл Интернэшнл Рисерч,Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:


    M
    AT
    A + B
    1chE 00 Is5 00 Is3 IND
    Fzg
     01
    one
    The invention relates to the separation of a liquid carbon mixture comprising two comrades.

    The aim of the invention is to reduce solvent consumption and energy costs.
    The method is carried out as follows.
    Examples of the implementation of the method are given in Table I. Processes 11 and 12 relate to the separation of liquid – solid systems, the remaining processes are structure in liquid – liquid systems. Asphaltenes (process 1) are sometimes very viscous, but they are liquids from the point of view of physics.
    According to the invention, the extracting agent, which was previously subject to separation from component B in a cumbersome and expensive way (for example, by distillation, crystallization or distillation), followed by reintroduction into the mixture to be separated, now comes from component B, which is already separated, to processing mixture. Separation and re-introduction can be carried out at the same temperature and pressure, which significantly reduces energy consumption.
    Depending on the conditions used, a larger or smaller portion of the total amount of extracting agent is transferred across the membrane. Consequently, in certain cases a more complete separation will be carried out, but such a separation will always be carried out on a smaller scale, therefore it will be less expensive than the process carried out without prior removal of the extracting agent through the membrane.
    The membrane is permeable to the extracting agent and not permeable to component A, under certain conditions, the membrane is also permeable to component B, which is beneficial if the concentration of component B is higher in the mixture of components A and B than in the stream containing extractant. In this case, the gradient concentration causes diffusion of component B from one side of the membrane to the other, which gives separation
    components A and B. But if the concentration of component B in the stream containing the extracting agent is permeable and the membrane is permeable to component B, the concentration of the latter should be lowered, for example, by adding an extracting agent. This increases the solvent content.
    In processes based on the use of membranes, concentration polarization may occur. As a result, where the extracting agent diffuses from one side to the other, a layer consisting almost exclusively of component B can form along the first side of the membrane, and, similarly, a layer almost entirely can form along the second side of the membrane. exclusively from extracting agent. Such a local change in the concentration gradient on the reverse causes a slower diffusion of the extracting agent. To prevent this concentration polarization, flow- -. Pumps along both sides of the membrane and — in order to avoid the need to use a membrane with too large a surface — the streams are recycled. Thus, the mixture as homogeneous as possible is constantly located on one side and on the other side of the membrane. The pumping rate must be such that the molecule diffusing through the membrane passes along the membrane 10-30 times before it diffuses through it.
    This means that part of the mixture of components A and B, which partially absorbed the extracting agent, is reintroduced into the stream of the mixture of components A and B (upstream with respect to the membrane) and, thus, is fed again along one side of the membrane. The mixture of components A and B is pre-diluted before passing along the membrane. In particular, in the case of separation of highly viscous liquids, for example, residual oils, this improves their
    pumping ability and / or lowering the temperature. Part of the stream of extracting agent containing the dissolved component B, which runs along
    re-entering the extracting agent containing the dissolved component B, and thus again passing along the other side of the membrane.
    Although in many cases a single membrane is enough, there are cases when, due to imperfect devices, it is preferable to use several membranes either to achieve greater performance (parallel installation) or for more complete extraction (sequential installation). In the latter case, several membranes are installed in series, and the flow of the A + B components, which are passed along one side of any of the membranes, then passed along the same side of the next membrane, and, similarly, the flow of extracting agent containing the dissolved component B, which passes along the other side of any of the membranes, then pass along the same side of the protruding membrane. Then the flow of components a and b is fed to the separator. Another stream, now consisting almost entirely of pure component B, is not necessary to be subjected to final purification (for example, distillation).
    When using several membranes, their number depends on the type of process, the feed rate per unit of time and the size of the membrane. Typically 2-20 membranes are used, preferably 4-10 membranes.
    The material for the membrane can be selected from known materials used for this purpose, for example, polypropylene, cellulose acetate, butyl rubber, methyl rubber, silicone rubber, polystyrene, polytet, rafluoroethylene, and other polymeric materials. The material must be insoluble both in components A and B and in the extracting agent. It must also be completely or practically impermeable to component A, but permeable to the extracting agent. The membrane is not clogged with solid or viscous elements of the mixture of components A and B - the membrane remains clean, as it is continuously washed with a diffusing extracting agent.
     By configuration, the applied membrane can be one of the flow capable of maintaining along both its
    five
    0 0
    five
    0 5 0 5
    sides, for example, flat or tubular. However, such forms are not very economical from the point of view of area and therefore do not allow to achieve high packing density (m of membrane / m of apparatus).
    Preferably the use of a spiral-wound membrane. It combines such qualities as resistance to pressure, low initial costs and high packing density of the known spiral-wound membranes supporting flows on one side of the membrane, with the possibility of maintaining flow on both sides of the membrane.
    FIG. 1 is a flow chart of the process according to the proposed method; in fig. 2 and 3 are flow diagrams of dewaxing and deasphalting installations, respectively.
    The mixture A - «- B to be separated. (Fig. 1) enters membrane device M, where extracting agent E is attached to the stream of the mixture to be separated. The resulting stream then enters the separator S, where component A is separated. The residue (component B and extracting agent) is recycled to membrane device M to transfer the extracting agent to a fresh portion of the mixture to be separated. If the membrane is permeable to component B and if the concentration of component B is higher in mixture A + B than in mixture E + B, component B migrates along the membrane in the opposite direction to the extracting agent (dotted line B).
    The dewaxing unit (Figure 2) includes a membrane device. The feedstock, for example paraffin furfural raffinate, enters through line 1 to the membrane unit 2, where the solvent (extracting agent) 3 is attached to the raw material. A mixture of aromatic hydrocarbons (benzene, toluene, etc.) and methyl ethyl ketone can be used as a solvent. Through pipes 4 and 5, the raw materials and the solvent flow further through the heat exchanger 6 and the cooler 7 into the rotating drum-type vacuum filter B. In the refrigerator 7, the raw materials and plant are cooled to a temperature of approximately; but -20 ° C for crystallization of paraffins contained. The paraffin crystals are washed on the drum of the drum filter 8 using a thin stream of solvent 9, then raked and together with a small amount of the remaining solvent is fed through pipe 10 to the paraffin treatment unit II, where the so-called wax paraffin 12 is separated from the solvent that is pipe 13 enters recycle line 14.
    The filtrate, consisting of the dewaxed oil and solvent, from the rotating drum-type vacuum filter 8 flows through the pipe 15 through the heat exchanger 6 to the membrane device 2, And the heat exchanger 6 and the membrane device 2 are pre-cooled to some extent by indirect contact with cold filtrate. After diffusion of a significant part of the solvent through the membrane (stream 3), the dewaxed oil together with the remaining solvent flows through pipe 16 to the installation 17 for the treatment of dewaxed oil.
    Installation 17 typically includes two evaporation columns (one operates at low pressure and temperature, the other at elevated pressure and temperature), behind which stands a column for stripping the dewaxed oil, in combination with distillation columns to remove water from the solvent and p yes pumps, burners and pipes reverse refrigerators. The required heat is supplied by heat exchanger 18. Here the dewaxed oil 19 is finally separated from the bodies, which through pipes 20 and 14 through the cooler 21 re-enters the system, i.e. in raw materials coming in line 5.
    In a deasphalting unit (Fig. 3), pipe 1 feedstock (usually the residue from vacuum distillation) is fed to mixer 12, where it is pre-diluted with a stream already diluted with extracting agent leaving pipe 3. Mixer 2 functions the same as a buffer vessel leveling the supply fluctuations. From mixer 2 through pipe 4, a stream is continuously withdrawn, part of which flows through the pipe
    5c, the membrane device 6, and the remaining part through pipes 7 and 8 enters the membrane device 9. In these membrane devices, a certain amount of extracting agent, represented as streams 10 and II, diffuses from the stream of desalted oil and solvent entering through pipes 12
    and 13, respectively, through the membrane into the pre-diluted flow of shf, which flows through pipes 5 and 8, respectively, and discharges through pipes 14 and 15, respectively. Pipe .4 is connected to pipe 3, which leads to the mixer. The pipe 15 recirculates part of the diluted feedstock to the membrane device 9 through the pipe 16 and pipe 8, and the remainder of the diluted feeds enters the next membrane device through the pipe 17. Flow of deasphalted oil with extracting agent, which is part of the extracting agent to the membrane devices
    6 and 9, respectively, are discharged through pipes 18 and 19, respectively. Part of it is recycled to the first membrane unit through pipes 20 and 12 and 21 and 13, respectively, while the remainder is discharged through pipes 21 and 22, respectively. The pipe 22 is connected to the previous membrane device by pipe 12, and the pipe
    21 is connected to a stripping column 23, in which the residues of the extracting agent 24 are removed by steam from the deasphalted oil stream 25.
    The number of membrane devices may vary; in the installation described, their number is 7. Part of the feed stream with an extracting agent, which is discharged through the pipe
    26, is supplied to a Rotating Disc Contactor 27, where this stream is divided into an asphaltene fraction discharged through pipe 28, and a fraction of the deasphalted oil with
    an extracting agent, which flows through pipe 29 into pipe 30 to remove the solvent in the membrane device 7 (and then in the membrane devices 6.5, etc.). The asphaltene fraction is separated from the residual extracting agent (if it contains the latter) in the stripping column 31. Some amount of asphaltenes can be removed.
    pipe 32 and some amount of extracting agent through pipe 33. Both streams flowing through pipe 33 recirculate through pipe 34 to the rotating disk contactor 27 so that the entire extracting agent is mixed with the raw material.
    The production of steam and the subsequent separation of steam and extracting agent (for example, propane) in the stripping column 23 requires a certain amount of energy, which is the greater, the larger the fraction of the extracting agent in the deasphalted oil. This fraction is small because the maximum possible amount of extracting agent enters the fresh feed through the membrane unit. If special material is used for membranes; for example, polypropylene, then in addition; a large part of the deasphalted oil comes directly from streams 5, 8, etc. in streams 18, 19, etc. through membranes, resulting in an additional reduction in total costs.
    The movement of the extracting agent can be either countercurrent (FIG. 3) or continuous.
    Example 1. The experiment was carried out in a deparaffinizer (Fig. 2). The paraffin furfural raffinate is treated with a mixture of selective solvents (an extractive agent) consisting of 50 vol.% Methyl ethyl ketone and 50 vol.% Toluene in a membrane unit 2 containing a spirally wound membrane of polypropylene-polyethylene copolymer 1 μm thick. From 1,714 tons / day of the solvent mixture supplied together with 299 tons / day of dewaxed oil through pipeline 15 to the membrane unit 2, 1,264 tons / day, i.e. Nearly 74% by weight of the solvent mixture present in stream 15 is fed through the membrane into stream 4 and then passed with a paraffin furfurol raffinate through a heat exchanger 6, a cooler 7 and a pipe 5 to a vacuum rotary drum filter 8. Paraffin crystals obtained after cooling the paraffinic raffinate and the solvent mixture in the refrigerator 7, washed on the filter 8 using a small stream of the solvent mixture 9, then removed and fed through pipe 10 to the paraffin treatment unit 11.
    th -

    W
    f5
    20
    25
    282822-8
    The filtrate from filter 8, consisting of a dewaxed oil and solvent mixture, is a specified stream of 15. 299 tons / day of dewaxed oil, which comes from membrane unit 2 together with 450 tons / day of the remaining solvent mixture, is fed through line 16 to block 17, which contains two evaporation columns and a stripping section to thereby separate 299 tons / day of dewaxed oil through conduit 19 and re-supply 450 tons / day of the solvent mixture through conduit 20 to the deparaffinizer.
    In tab. 2 shows the effect of the junction of the membrane assembly on the treatment of dewaxed oil.
    As can be seen from the table. 2, stream 16 contains a significantly smaller amount of solvent as compared to the option where the membrane is not used. Accordingly, a smaller amount of solvent has to be extracted in the separation unit 17. In this connection, less heat is required to remove the solvent from the dewaxed oil (8708 instead of 21855 MJ / h).
    Example 2. The experiment was carried out in a deasphalting unit (Fig. 3). A short feed of the residue obtained by vacuum distillation of the atmospheric residue after the distillation of crude oil is pre-diluted in a mixing tank 32 with a mixture of feed and p-butane fed through conduit 33. The mixture of short residue and p-butane, thus obtained, is fed into six parallel membrane blocks where use polypropylene membranes 3 microns thick. In these units with a working temperature of 60 ° C, 859 p-butane (a selective solvent is used) diffuses from the streams containing deasphalted oil and n-butane, and from stream 18 (263 m / day) of the deasphalted oil
    35
    40
    45
    50
    55
    la and 1321 p-butane) through membranes into a pre-diluted feed. Deasphalted oil streams containing butane residue, which is supplied from membrane blocks, are collected in stream 19 (263 meters of deasphalted oil and 462 p-butane) and fed to the evaporative
    the section where the deasphalic oil is separated from the n-butane. A short residue feed stream mixed with tan, which is removed from the membrane blocks, is fed to a contact apparatus with rotating disks, where the stream is divided into an asphaltenic fraction (106 m VcyT - stream 39) and the specified stream containing deasphalted oil and n-butane. The asphaltenes fraction (stream 39) is fed to the stripping section and separated from the remaining p-butane (20 m / day).
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    A method of separating a liquid two-component hydrocarbon mixture, comprising contacting it with an extractant.
    . Furfural - on extraction
    . Phenolic extracysh
    . SO extraction,
    Deasphalised residual oil, spun oil, t - excellent recycling oil
    Deasphalised residual oil, spun oil, heavy recirc. Corrosive oil Deasphalted residual oil, t Furfural raffinate
    Phenolic raffinate
    SO ,, raffinate
    dissolving one of the two components, separating the other component in the separator from the obtained extract solution and separating the last dissolved component, characterized in that, in order to reduce solvent consumption and energy costs, the initial hydrocarbon mixture is passed through one side of the membrane permeable to the extractant the impermeable component which is not soluble in the extra agent, the extract solution is passed along the other side of the membrane with the subsequent feeding of the initial hydrocarbon mixture and absorbing the extra agent into a separator with separation of the extract solution directed along the other side of the membrane.
    Table 1
    Furfural Furfural extract
    Phenolic extract
    Phenol
    50 Extract
    Liquid 80 „
     M-methylpyrrolidone;
    #-TO-)(
    tetrahydrothiophene-1,1-DIOXIDE}
    triethylene glycol or tetraethylene glycol may also be used.
    13
    Flow
     LIII ji-TKl

    299-299299
    1714-1714 - 1714
    299-299299
    17141264450 - 450
    }
    : ± no head
    128282214
    table 2
    Flow
    20
    / "
    13
    2S
    Iff
    17
    .12
     18
    puz.Z
    fig.}
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1282822A3|1987-01-07|Method of separating two-component hydrocarbon mixture
    US20110000823A1|2011-01-06|Membrane desulfurization of liquid hydrocarbons using an extractive liquid membrane contactor system and method
    KR102003498B1|2019-07-24|Regeneration process of polar solvents from aromatic extraction process by treating with light hydrocarbons
    GB477567A|1938-01-03|A process for extracting liquid mixtures in countercurrent
    AU675323B2|1997-01-30|Lubricating oil dewaxing using cold solvent recycle process
    US5651877A|1997-07-29|Lubricating oil dewaxing with membrane separation
    TWI488679B|2015-06-21|Extraction process with novel solvent regeneration methods
    US5494566A|1996-02-27|Lubricating oil dewaxing with membrane separation of cold solvent
    AU674962B2|1997-01-16|Lubricating oil dewaxing using membrane separation of cold solvent from dewaxed oil
    US20090200208A1|2009-08-13|Method of producing mineral oils based on hydrocarbon distillates
    BR0108171B1|2010-02-09|Method for extracting fat or oil soluble components, for example, pah, npd, and / or btx, from water produced that is separated from an oil and / or gas plant, and water cleaning system at a oil / gas, for the removal of oil-soluble components, such as pah, npd and / or btx, from water extracted in a well stream.
    US2602044A|1952-07-01|Clay decolorizing of solvent refined lubricating oils
    CN101734737A|2010-06-16|Processing method of water flowing out of technological water stripper of ethylene unit
    SU563116A3|1977-06-25|The method of separation of aromatic hydrocarbons
    DE1296724B|1969-06-04|Process for preventing ice and hydrate formation in the separation of a water-containing mixture containing light hydrocarbons by fractionation
    CN106457065B|2019-12-10|Heavy hydrocarbon removal
    SU57124A1|Method for the continuous freezing of high-melting substances from a mixture of them with low-melting
    US2173915A|1939-09-26|Method of solvent refining
    Overfield1989|Chromatographic analysis of hydrocarbons
    GB782051A|1957-08-28|Improvements in or relating to countercurrent contacting of fluids
    同族专利:
    公开号 | 公开日
    EP0088458A3|1984-03-07|
    ZA831414B|1984-01-25|
    AU1197083A|1983-09-08|
    BR8301003A|1983-11-22|
    AR241868A1|1993-01-29|
    CA1201660A|1986-03-11|
    IN158141B|1986-09-13|
    JPS58159804A|1983-09-22|
    GB2116071B|1985-01-30|
    GB8305738D0|1983-04-07|
    NL193983C|2001-04-03|
    GB2116071A|1983-09-21|
    MY8700269A|1987-12-31|
    DE3368013D1|1987-01-15|
    JPH0330401B2|1991-04-30|
    US4670151A|1987-06-02|
    AU559866B2|1987-03-19|
    KR840003820A|1984-10-04|
    EP0088458B1|1986-12-03|
    NL193983B|2000-12-01|
    NZ203440A|1985-08-30|
    KR900008728B1|1990-11-29|
    EP0088458A2|1983-09-14|
    NL8200881A|1983-10-03|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2501936C1|2012-04-06|2013-12-20|Ильмар Раисович Айсматуллин|Heat exchanger device for removal of paraffin and resins from oil before its transportation|
    WO2014088951A1|2012-12-03|2014-06-12|Renewable Process Technologies Llc|System and method for film-based chromatographic separation|
    RU170496U1|2017-02-06|2017-04-26|Федеральное государственное бюджетное учреждение науки Ордена Трудового Красного Знамени Институт нефтехимического синтеза им. А.В. Топчиева Российской академии наук |DEVICE FOR CONTINUOUS SEPARATION OF A MIXTURE OF HYDROCARBON GASES|US2276210A|1940-01-12|1942-03-10|Shell Dev|Acid purification and recovery process|
    GB645876A|1947-05-12|1950-11-08|Robert Andrew Gordon Stockdale|Improvements in and relating to the extraction and purification of organic compounds|
    CH291180A|1951-06-20|1953-06-15|Zyma Sa|Continuous extraction and dialysis machine.|
    US3305595A|1963-06-18|1967-02-21|Sun Oil Co|Aromatics separation and purification by dialysis|
    US3450608A|1966-03-09|1969-06-17|Nalco Chemical Co|Purification of ethers|
    US3370102A|1967-05-05|1968-02-20|Abcor Inc|Isothermal-liquid-liquid permeation separation systems|
    US3556991A|1968-12-06|1971-01-19|Universal Oil Prod Co|Method for the solvent extraction of aromatic hydrocarbons|
    US3956112A|1973-01-02|1976-05-11|Allied Chemical Corporation|Membrane solvent extraction|
    DE2947089A1|1979-11-22|1981-05-27|Helmut Dr.-Ing. 5804 Herdecke Michele|METHOD FOR SEPARATING FLUIDS BY PERMEATION|
    JPS57118559A|1981-01-16|1982-07-23|Toray Ind Inc|Separation of sulfuric acid from reaction mixture of beckmann rearrangement|US4510047A|1983-12-14|1985-04-09|Exxon Research And Engineering Co.|Selective extraction solvent recovery using regenerated cellulose membrane under reverse osmosis conditions|
    US4571444A|1984-04-27|1986-02-18|Exxon Research And Engineering Co.|Process for separating alkylaromatics from aromatic solvents and the separation of the alkylaromatic isomers using membranes|
    US4532029A|1984-04-27|1985-07-30|Exxon Research And Engineering Co.|Aromatic solvent upgrading using membranes|
    US4606903A|1984-04-27|1986-08-19|Exxon Research And Engineering Co.|Membrane separation of uncoverted carbon fiber precursors from flux solvent and/or anti-solvent|
    US4797200A|1984-05-04|1989-01-10|Exxon Research And Engineering Company|Upgrading heavy oils by solvent dissolution and ultrafiltration|
    GB8619278D0|1986-08-07|1986-09-17|Shell Int Research|Separating fluid feed mixture|
    US5350681A|1986-08-18|1994-09-27|The Coca-Cola Company|Enzymatic membrane method for the synthesis and separation of peptides|
    US5202235A|1986-08-18|1993-04-13|The Coca-Cola Company|Enzymatic method for the synthesis and separation of peptides|
    US5336601A|1986-08-18|1994-08-09|The Coca-Cola Company|Enzymatic membrane method for the snythesis and separation of peptides|
    US4962271A|1989-12-19|1990-10-09|Exxon Research And Engineering Company|Selective separation of multi-ring aromatic hydrocarbons from distillates by perstraction|
    US4982051A|1990-01-18|1991-01-01|Texaco Inc.|Separation of furfural/middle distillate streams|
    US5041227A|1990-10-09|1991-08-20|Bend Research, Inc.|Selective aqueous extraction of organics coupled with trapping by membrane separation|
    US5133867A|1990-10-31|1992-07-28|Exxon Research And Engineering Company|Reverse osmosis process for recovery of C3 -C6 aliphatic hydrocarbon from oil|
    US5084183A|1990-10-31|1992-01-28|Exxon Research And Engineering Company|Fractionation of light/heavy waxes by use of porous membranes|
    US5107059A|1990-12-05|1992-04-21|Exxon Research & Engineering Company|Iso/normal paraffin separation by membrane extraction|
    US5107058A|1990-12-05|1992-04-21|Exxon Research And Engineering Company|Olefin/paraffin separation via membrane extraction|
    US5107056A|1990-12-05|1992-04-21|Exxon Research And Engineering Company|Selective separation of naphthenes from paraffins by membrane extraction|
    US5045206A|1990-12-05|1991-09-03|Exxon Research & Engineering Company|Selective multi-ring aromatics extraction using a porous, non-selective partition membrane barrier|
    US5120900A|1990-12-05|1992-06-09|Exxon Research And Engineering Company|Integrated solvent extraction/membrane extraction with retentate recycle for improved raffinate yield|
    US5095170A|1990-12-05|1992-03-10|Exxon And Research And Engineering Company|Intergrated membrane pre-extraction/solvent extraction of distillates|
    US5149340A|1991-03-12|1992-09-22|Marathon Oil Company|Process and apparatus for separating impurities from hydrocarbons|
    US5256297A|1992-12-17|1993-10-26|Exxon Research And Engineering Company|Multi-stage ultrafiltration process |
    US5360530A|1993-04-23|1994-11-01|Mobil Oil Corporation|Lubricating oil dewaxing using membrane separation of cold solvent from dewaxed oil and recycle of cold solvent to filter feed|
    US5358625A|1993-04-23|1994-10-25|Mobile Oil Corporation|Lubricating oil dewaxing using membrane separation of cold solvent from dewaxed oil|
    US6112908A|1998-02-11|2000-09-05|Rentiers Machinery Pty, Ltd.|Membrane laminates and methods for their preparation|
    US6273937B1|2000-03-29|2001-08-14|Trans Ionics Corporation|Membrane pervaporation and vapor permeation system|
    WO2002078821A1|2001-03-30|2002-10-10|Trans Ionics Corporation|Membrane pervaporation and vapor permeation system|
    JP4956294B2|2007-06-27|2012-06-20|東芝産業機器製造株式会社|Closed switchboard|
    DE102014100694A1|2014-01-22|2015-07-23|Friedrich-Alexander-Universität Erlangen-Nürnberg|Process and apparatus for separating fluorinated hydrocarbons from an aqueous phase|
    RU2642641C1|2016-11-16|2018-01-25|федеральное государственное бюджетное образовательное учреждение высшего образования "Алтайский государственный университет"|Membrane extractor|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL8200881A|NL193983C|1982-03-04|1982-03-04|Method for separating a liquid mixture.|
    [返回顶部]