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    • 专利摘要:
    1431946 Separating hydrocarbons STANDARD OIL CO 4 May 1973 [12 May 1972 13 Sept 1972] 21365/73 Heading C5E Aliphatically unsaturated hydrocarbon having 2 to 8 carbon atoms is separated from a mixture by selectively transferring it across a barrier which comprises an aqueous component containing metal ions which combine with the unsaturated hydrocarbon to form a water soluble complex and a semi-permeable member which is solid, water-insoluble and impermeable to the aqueous component; the partial pressure of the unsaturated hydrocarbon on the second side of the barrier being maintained lower than that on the first side so that the unsaturated hydrocarbon is released on the second side of the barrier. The metal ions can be silver, zinc or cuprous ammonium and the aqueous component can comprise silver nitrate, optionally together with UO 2 (NO 3 ) 2 or a nitrate of Cr, Ni, Zn, Cd, Al, Li, Sr, Ca, Mg, Co, Fe<SP>3+</SP>, Na, Pb, NH 4 or K. The semi-permeable membrane can comprise polyurethane, nylon, sodium cellulose xanthate or an ethylene glycol monomethacrylate polymer. The process can be used to separate acetylene and/or ethylene from mixtures which also comprise methane and/or ethane. Many examples are given in which the aqueous component is in the form of a liquid covering the first side of the semi-permeable membrane which is either in the form of a flat sheet or a hollow tube immersed in the liquid; alternatively the aqueous component can be held within the semi-permeable membrane, e.g. by being absorbed therein or absorbed on a material such as cellulose acetate which is held between two semi-permeable sheets.
    公开号:SU1088659A3
    申请号:SU731927579
    申请日:1973-05-11
    公开日:1984-04-23
    发明作者:Фредерик Стейгелманн Эдвард；Дэвид Хушес Роберт
    申请人:Стандарт Ойл Компани (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the isolation of aliphatic unsaturated hydrocarbons from mixtures containing hydrocarbons that are separated along with other materials, in particular, to the ethylene emission of gas mixtures containing ethylene and other hydrocarbons, such as ethane and / or methane.  Aliphatic unsaturated hydrocarbons are reactive compounds that are used for various purposes, especially as intermediates for organic synthesis.  It is known that some unsaturated hydrocarbons are used as monomers to form polymers, for example ethylene, propylene, butadiene and isoprene. These olefins, as well as other unsaturated compounds, for example ethylene and acetylene, are also used to produce relatively low molecular weight products.  Often mixtures of aliphatic unsaturated hydrocarbons are byproducts.  chemical synthesis products or separation processes.  If the mixture of aliphatically unsaturated hydrocarbons is in a liquid state under normal conditions, it can be easily separated into components using a conventional distillation process or extraction separation. To isolate valuable components from a mixture of aliphatically unsaturated hydrocarbons, it is in a gaseous state. use cryogenic processes.  However, these processes are very expensive.  The closest to the invention in its technical essence and achievable result is a method of separating C -Ca aliphatic unsaturated hydrocarbons from a vaporous hydrocarbon mixture by contacting it with one side of a solid water-insoluble semi-permeable membrane at a partial pressure of non-saturated hydrocarbons to a membrane that becomes partial pressure; it, with removal of the isolated alkaline unsaturated hydrocarbons on the other side of the C1 3 membrane.  The purpose of the invention is to increase the effectiveness of the process.  This goal is achieved by the method of separating aliphatic unsaturated hydrocarbons from the vaporous hydrocarbon mixture by.   contacting it with one side of a solid water-insoluble membrane that is in contact with a layer of a liquid complexing agent containing water and metal ions selected from the group including sodium, lithium, silver, copper, magnesium, calcium, strontium, aluminum, lead, chromium, iron, cobalt, nickel, their mixtures, semipermeable to the liquid complexing agent, with a partial pressure of unsaturated hydrocarbons to a membrane exceeding the partial pressure after it, with the removal of selected aliphatically unsaturated carbohydrates genera on the other side of the membrane.  Preferred is the use of a membrane in contact with a layer of a liquid complexing agent located on the supply side of the initial mixture or the use of a membrane inside which a layer of a liquid complexing agent is located.  The method is carried out as follows.  The initial mixture, which is in the vapor state, is passed through an aqueous liquid barrier containing metal ions, which form a water-soluble complex with unsaturated hydrocarbons.  Said liquid barrier is disposed on one side of the solid membrane semi-permeable to it.  The desired product is isolated from the opposite side of the membrane.  This technique can be used to separate one or more non-saturated hydrocarbons, as well as in combination with other separation processes, such as a cryogenic process.  Although this method allows to get clean. a product, for example, an aliphatic unsaturated hydrocarbon with a purity of more than 99%, is used only to significantly increase the concentration of a given aliphatic unsaturated hydrocarbon in a mixture with other components of the feedstock.  The proposed method can be used to separate various aliphatically unsaturated hydrocarbons from other components of the feed mixture, and at least one of the aliphatically unsaturated hydrocarbons must pass through the liquid barrier faster than other feedstock components.  The method can also be used to separate aliphatically unsaturated hydrocarbons from other hydrocarbons, which may be aliphatically saturated or unsaturated, or from substances of non-hydrocarbon origin, including gases, such as hydrogen.  The initial mixture may contain one or more paraffins, including cycloparaffins, mono- or polyolefins, which may be cyclic or acyclic, and acetylenes or alkynes, and also include aromatic structures.  tours, in parts of which there may be an ali fatic configuration.  Among the materials to be divided, ethylene, propylene, butenes, butadiene, isoprene, acetylene, etc. can be mentioned. P.  The separated mixture can be in the gas or napoBoii phase when contacted with a liquid barrier containing one or several metal ions dissolved in it, forming complexes with an unsaturated hydrocarbon.  The liquid barrier is usually in contact with a semi-permeable element (membrane), essentially impermeable to the liquid, but permeable to a mixture containing an aliphatic unsaturated hydrocarbon, under the conditions created during the separation.  The semi-permeable element may be, for example, a film and a membrane for separating and cleaning various chemicals. Ij.  The liquid barrier is formed using a semipermeable membrane in various ways.  The membrane can immobilize it, inside the loading side or near it.  The liquid barrier can be between two solid permeable films that prevent the passage of liquid through them.  With such a structure, the liquid barrier can be absorbed by a porous lattice, for example, a filter of cellulose acetate.  According to the structure of the second type, a liquid barrier can be formed.  maintaining the liquid on the surface permeable to the liquid.  The initial mixture can pass into the liquid layer, with a barrier being formed on the inner surface supporting the liquid.  The liquid barrier can be partially or completely absorbed in the supporting structure, as a result.  In this case, the exit side of the structure becomes impermeable to the liquid under the process conditions, but permeable in the presence of a liquid barrier to the component of the initial mixture subjected to separation.  The liquid barrier contains enough water and soluble metal ions to form a comp.  LEXA with at least one component of aliphatically unsaturated hydrocarbons of the initial mixture subjected to separation.  Metal ions easily form a complex when contacted with the feedstock and easily decompose into a metal ion and an aliphatically unsaturated component of the complex when the desired product is removed from the opposite side of the barrier.  The liberated aliphatic unsaturated hydrocarbons are removed from the discharge side of the liquid barrier and its supporting structure using sweep gas or using a vacuum created on this side of the barrier.  The reactivity of aliphatically unsaturated hydrocarbons with respect to the complexing metal ions decreases in the direction of the acetylenes or dienes to monoolefins.  The partial pressure (PD) of the aliphatically unsaturated component of the initial mixture on the load side of the liquid barrier is much greater than on the discharge or discharge side.  The decrease in the partial pressure of the unsaturated hydrocarbon is not less than 035 kg / cm, preferably 1.4 kg / cm.  The total pressure of the initial mixture is usually up to 70.3 kg / cm.  The drop in the partial pressure of the unsaturated hydrocarbons on the discharge side of the liquid barrier can be controlled by using a purge gas, inert to the formation of a complex with metal ions in an aqueous solution in the liquid barrier.  The purge gas entrains the isolated aliphatic unsaturated components, and this gas should be easily separated from the aliphatic unsaturated compounds, if necessary for subsequent use, of unsaturated hydrocarbons.  Butane and carbon dioxide can be used as such a gas.  The temperature in the proposed barrier may be constant or may vary.  Typically, the temperature of the liquid barrier is equal to the ambient temperature, especially in.  when the feedstock is in the gaseous state at temperature and pressure, which are used on the loading side of the liquid barrier.  The temperature of the liquid barrier can be lowered or raised as compared to the ambient temperature.  Often the temperature may reach 100 ° C, and an elevated temperature may even be desirable in order to maintain the feed mixture in the gas or vapor phase. . However, neither the temperature nor the pressure should be such that there is a violation of the transfer rate difference in the liquid barrier of aliphatically unsaturated hydrocarbons compared with other components of the initial mixture.  These conditions must be such that physical destruction of the liquid barrier does not occur.  As metals that are in the form of ions contained in the complexing agent, silver, copper, magnesium, calcium, strontium, aluminum, lead, chromium, iron, cobalt, nickel, ammonium, zinc, cadmium sodium, lithium, uranium can be used.  The metal is in an aqueous liquid barrier in contact with a semipermeable element in a form soluble in this liquid, for example in the form of chlorides or nitrates.  Salt metals should not react with any components of the feedstock containing an aliphatically non-saturated hydrocarbon, with the formation of insoluble substances that can clog the film membrane or otherwise interfere with the separation of the target component of the starting mixture.  In addition, in this system, the metal is chosen in such a way that a complex is formed sufficiently resistant to decomposition and is easily removed from the liquid barrier, resulting in an increased concentration of aliphatic unsaturated hydrocarbon, which is removed from the exit side of the barrier. relation to the initial mixture; The concentration of metal ions in the liquid barrier may be lowered, but sufficient for NI9, the passing rate of complexation so that the excess surface of the semipermeable membrane does not perform the separation function.  The concentration of complexing metal ions in the aqueous solution forming the liquid barrier is at least 0.1 mol, preferably 0.512 mol.  Luchaye, if the concentration of the solution is below the saturated with respect to the complexing metal ions: to ensure the content of all metals in the solution, which prevents clogging of the membrane membrane and the violation of its permeability.  When used as complex-forming ions in the liquid barrier, copper and ammonium ions, which form a copper-ammonia complex, it is desirable to introduce them in equimolar amounts into the liquid barrier solution.  To enhance the selectivity of the copper ammonium ion complex, the liquid barrier solution can be acidified by the addition of a water soluble acid, for example hydrochloric acid.  It is desirable that the pH of the liquid barrier is not more than 5 in the presence of acid in the solution.  Since silver contributes to the formation of undesirable acetylides with acetylene, it is better to use the copper – ammonia complex in the isolation of acetylenes from various mixtures.  Mixtures of noble metals with other cations can be used for complexation.  Solutions containing more non-precious metal, ammonium or other cations are less expensive, and therefore the amount of noble metals may be about 10. a pier % or less of all cations in solution.  The amount of water in the liquid barrier may be at least 3 wt. %  In the proposed method, the membrane membrane is in contact with a water barrier with ions of the complexing metal dissolved in it.  This contact can be created by a liquid aqueous phase, more or less absorbed film without separating the aqueous phase, which is in the form of a layer on the input side of the film.  The membrane membrane can be wetted first, and if there is a tendency to dry during use, additional water can be applied to the film, for example, by introducing moisture into the feed mixture loaded into the system.  The moisture content of the film can also be maintained by creating a separate water phase, for example, in the form of a solution of complex-forming metal ions, near the entrance side of the film and preferably in contact with almost the entire side of the film during its directing, to separate the aliphatically unsaturated hydrocarbons.  Therefore, the film membrane should be wetted so that the indiscriminate permeability of the components of the feedstock does not occur, which will lead to a decrease in the concentration of aliphatically unsaturated hydrocarbon at the outlet.  The membrane membrane used in the proposed method for supporting the liquid barrier is essentially solid, hard to be soluble and semi-permeable.  In the absence of fluid filling the pores of the film; sufficient selectivity is not achieved with respect to the transmission or penetration of an aliphatically unsaturated hydrocarbon to achieve the desired separation.  Often the film is permeable to virtually all components of the feedstock, if they are in the gas phase.  However, when a film comes in contact with a sufficient amount of an aqueous liquid to form a barrier, the physical passage of gas through the film decreases or stops, therefore the components of the initial flow already selectively pass through the film, after which they are released from the aqueous liquid phase.  The proposed membrane membrane prevents the physical passage of significant quantities of liquid substances through the film under the process conditions.  Since the proposed method uses an aqueous medium, the film may have hygroscopic properties, being essentially unreactive with respect to the complexing ion of the liquid barrier.  The membrane membrane may be self-supporting and of sufficient strength not to require additional carrier material on either of its sides during application.  For some films, it may be necessary to provide sufficient support, for example, by creating an additional film or sheet-like material on one or both sides of the film membrane.  These support structures are often made of thin materials, they can be permeable both with respect to liquids and gases, but they do not perform the function of dividing the initial mixture into any of its components.  Film membranes can be of the most diverse form.  One useable form is a flat leaflet, which can communicate a large surface area and the ability to more efficiently disintegrate by using tubular fibers, such as hydrophobic and hydrophilic hollow fibers (acetate, cellulose, nylon, polyvinyl alcohols). , olefinic polymers, for example polyethylene, polypropylene, and copolymers of ethylene and propylene, etc. P. ). The thickness of the membrane membranes is not less than 0.25 mm, preferably 0.025 mm.  The thickness of the film must be sufficient to prevent its destruction at the pressures used.  When using hydrophilic polyporous aIX film membranes together with a liquid barrier containing complexing metal ions, there is no need for additional support structures.  Polymer gels can be used as films, including hydro-gels.  gels  A liquid barrier can be placed in a semipermeable membrane in various ways, and the membrane can immobilize the liquid barrier inside the membrane.  The liquid barrier is mainly located within the semi-permeable structure, and the liquid does not pass through the membrane.  The membrane is selectively permeable in the presence of a liquid barrier with respect to the components of the initial mixture subjected to separation.  Therefore, there may be a slight passage of the feedstock along the separation zones, with the exception of those components that become part of the liquid barrier or react with it in a chemical reaction.  This liquid barrier regulates the selectivity of the liquid barrier system - a semipermeable membrane.  If the water barrier is inside a hydrophilic film membrane, the amount of complexing metal in a semi-permeable membrane may vary depending on the degree of separation of the feedstock.  Often this is a small amount, t. e.  about 1-50 weight. % by weight of the membrane (without water), preferably about 5-25 wt. %  When placing a solution of a complexing metal on a semipermeable film by contacting the film with a solution, it is necessary to maintain the pressure difference between the solution and the film.  The pressure behind the solution is greater than the pressure on the opposite side of the film, as a result of which the solution enters the film under pressure.  Typically, the pressure of the solution is: above atmospheric, and on the opposite side of the film, essentially atmospheric pressure.  No need to. the pressure drop is large.  It may be, for example, not more than 0.350, 7 kg / cm.  The pressure should not be increased so that the film does not break.  The film membrane should be solid, water-insoluble, hydrophilic and semi-permeable.  In the absence of a liquid containing complexing ions in the film, the film is not sufficiently selective with respect to the transmission or penetration of an aliphatic unsaturated hydrocarbon to achieve the desired separation.  Often the film is permeable mainly to all components of the initial mixture that are in the gas phase.  If the film contains the necessary amount of an aqueous liquid to form a barrier, the simple gas diffusion through the film is reduced or prevented, and the components of the initial flow, the passage through the film, partially become part of it, and then separated from the aqueous liquid phase contained in the film.  In the absence of an ion of a complexing metal in an aqueous medium, a slight separation of hydrocarbons can occur.  The selectivity of the separation of aliphatic unsaturated hydrocarbons is significantly increased in the presence of complexing metal ions in the water barrier environment in the film.  Film membranes that can be used according to the inventive method serve to prevent simple diffusion of significant amounts of liquid material through the film. Since an aqueous medium is used in this system, the film has hydrophilic properties and basically does not react with at least some of the complexing agents. ion liquid barrier.  Film membranes are mostly self-supporting, they have sufficient strength not to require any additional carrier material on one of their sides.  Hygroscopic agents are contained in the film in small quantities, t. e.  about 0.1-40 weight. % of the total weight of the semipermeable membrane.  without this means and liquid aqueous complexing solution.  Preferably, this amount is about 1-20 wt. %, although in some cases, a hygroscopic agent is used in large quantities.  So, when using formulations containing nylon and polyvinyl alcohol, the formulations may contain about 25-75% by weight,% of each of these materials, preferably about 35-55% polyvinyl alcohol and about 4565% nylon.  Example 1  A semipermeable membrane is made by placing a cellulose acetate filter between two solid polymeric polycarbonate polymer films.  A solid cellulose acetate filter has a diameter of 25 mm and a thickness of 0.005-0.127 mm, and a pore diameter of 1.2 microns.  Silicone polycarbonate films are 0.015 mm thick and almost impermeable to water and silver ions,. but well permeable to gases.  The cellulose acetate filter is saturated with a 1 M aqueous solution of silver nitrate.  The saturated filtrate is then placed between a silicone polycarbonate film and placed in a cuvette to determine its effect. the separation of ethylene from a mixture with ethane and methane.  The cuvette is divided into upper and lower compartments by placing the membrane horizontally along the cuvette.  The cuvette internal area is 2.8 cm, so that the cross section is completely covered by a cellulose acetate filter.  The height of the main wyrpus of the cuvette is 41 mm, and there are gas holes on each side.  The inlet tube entering the upper edge of the cuvette is located about 5 mm from the membrane, and the tube for supplying the purge gas enters the lower edge of the cuvette and is located about 1 1.  mm below the membrane.  The original mixture is loaded into the upper part of the cuvette (50 ml / min).  It is in contact with the membrane, and the waste stream or purified gaseous components exit the cell through the top opening. The flow rate is considered sufficient to maintain a constant composition on the inlet side of the membrane.  The purge gas (helium, 10 ml / min) contacts the lower surface of the wound membrane, entrains hydrocarbons leaving the membrane, and then exits the cell through the lower outlet in the form of a finished product stream.  The product is analyzed. by gas chromatography, with Helium as a gas carrier.  The permeation rate, the outcome of their amount of hydrocarbon in the carrier gas, the flow rate of the carrier gas, and the response of the gas chromatograph detector to the I ml obtained g, are calculated.  mixes.  The tests continue for 2 hours during which the cuvettes and gases are at ambient temperature.  The results of these experiments are shown in Table.  one. - The data table.  Figure 1 shows the high selectivity of the system for separating ethylene, increasing the rate of penetration, and reducing the selectivity with increasing pressure.  During the experiment, no decrease in the membrane selectivity was observed for a given outlet pressure.  Examples 2-8.  The procedure described in Example 1 was repeated several times, changing the concentration of the solution (pt) B of the complex-forming metal compounds used to saturate the filter, as well as using bivalent copper nitrate to enhance the selectivity (for low concentrations of silver nitrate, which is a source of complexing metal).  The feed rate of the hydrocarbon mixture is 30 ppm / min, the inlet gas pressure is 0.7 kg / cm, other conditions as in Example 1.  The results of the experiments are given in Table.  2  . Each of the tested solutions shows good. selectivity to separate ethylene, and in each case there is an improvement out of. biration of 1 n.  silver nitrate due to the presence of other base metal ions and ammonium.  The ions of metals of groups II-VIII of the fourth and fifth periods of the element table, as well as the ions of magnesium and trivalent aluminum, appear to be most effective.  Zinc and bivalent copper ions are preferably used in combination with silver ions.  These data show that with an increase in the concentration of silver in solution, there is a significant increase in -.  the selection factor.  Similar results can be obtained at lower cost by using a non-precious metal ion to increase the total concentration of metal ions.  So, although 1-molar bivalent copper nitrate has little or no effect on the separation of ethylene because of the increased solubility of ethylene in solution compared with ethane and methane, divalent copper ions improve results when used with silver nitrate, with this is how the concentration of the latter increases.  Since copper nitrate is less expensive than silver nitrate, the use of such a combination may be desirable provided that copper does not cause any undesirable reactions with a membrane or an injected gas, Examples 9-25, the procedure described and in example 1, carry out several when using a cellulose acetate filter with a pore diameter of 0.65 μm and an I-molar solution of silver nitrate or a solution containing 1 mol of silver nitrate and 3 mol of another nitrate indicated in Table 3, the inlet pressure is 1.4 kg / cm, feed rate 30 ml / min.  Example 26 A cuvette described in example 1 is used to separate ethylene from a gas stream from mixed hydrocarbons using monovalent copper ion as a complexing metal.  Instead of the membrane described in example 1, the membrane is used in the form of a single CD-1 measure of silicone polycarbonate with a thickness of 0.007 mm.  At the top of this film, 2 mp of the aqueous complexing solution listed in Table 4 is injected. The source gas is a mixture of methane, ethane, ethylene and propylene, the gas in the cell is fed under a pressure of 0.7 kg / cm and arbotry through the complexing solution at a rate of 25 ml / min.  The back or side of the membrane is purged with nitrogen at a rate of 10 ml / min. 3-molar CuCl and NlLCl are used as complex 1310 lexophoretic solutions, and in one case also 1-molar HCl.  The results of the experiments are given in table. 4.  Although a solution of copper chloride and chlorine.  Ammonium hydroxide gives a useful complex, the rate of passage and selectivity with respect to ethylene noticeably increase in the presence of hydrogen chloride.  Ammonium chloride serves to form the complex, a ammonium ammonium ion with ethylene, and the presence of hydrochloric acid indicates the additional acidity and the increased solubility of the monovalent copper ion in solution.   Example 27  A cuvette was used in Example 1, but with a cross-sectional area of 2.75 cm, to concentrate the acetylene and ethylene contained in the mixed gaseous hydrocarbon stream.  The semi-permeable membrane is a 0.015 mm thick film of silicone rubber deposited on a porous disk.  The film is covered with 2 ml of an aqueous solution containing 3 mol CuCl, 3 mol. Cl and 3 mol HC1.  The feed gas was bubbled through the liquid solution in a cuvette at a speed of W MP / min under a pressure of 2.1 kg / cm, and helium was used as a purge gas at a flow rate of 10 ml / min.  The results of the experiments are given in table. 5.  These data show that the proposed system can be used to purify acetylene or to selectively remove acetylene from the gas. olefin containing stream.  Example 28  The proposed method is used in systems with a tubular membrane surface, using glass fiber tubular elements (outer diameter 0.2 cm, length 10.15 cm).  As a result, a semipermeable membrane is formed.  A glass tube element is usually used for electrically insulating, and it is immersed several times in a polymer solution to form a membrane.  Each end of each glass tubular element is attached to separate stainless steel tubular elements and the resulting part is immersed in water 1 and.  silver nitrate solution in a test tube with a stopper.  The coated glass tubular elements are completely immersed in solution 9 to form a membrane area of 6.4 cm, and stainless steel tubular elements are passed through. closed end of the tube.  The purge gas is passed into one of the tubes of stainless steel through the coated tubular element or section, the membrane, and then it comes out of the other stainless steel tube along with hydrocarbons that have gone through the membrane.  The source gas is bubbled into the solution in a test tube, and the HEAE outlet for removing the unreacted and undissolved components of the source gas from the tube is connected to the top of the tube at the top of the liquid complexing solution.  The source gas is fed into the tube at a rate of 50 ml / min, under a pressure of 0.7 kg / cm.  Helium is used as a purge gas through a glass fiber tube at a flow rate of 10 ml / min.  A purge effluent gas containing products that pass through the membrane is analyzed using gas chromatography.  Conducted several experiments at different temperatures, the results of which are shown in Table.  6  Example 29  The cuvette described in Example 1 is used to separate ethylene and propylene from the gas stream of mixed hydrocarbons containing hydrogen.  The membrane described in Example 1 is composed of upper and lower layers with a thickness of 0.075 mm of a film of silicone polycarbonate and a middle layer of cellulose filter paper, saturated with 6 molar solution. rum silver nitrate.  A moistened source gas mixture containing methane, ethane, ethylene, propylene and hydrogen is fed into the cuvette under a pressure of 5.4-2.8 kg / cm and at a rate of 10 ml / min.  The product passing through the membrane is purged from the bottom surface of the membrane as described in Example I, but used as a purge gas.  The results are shown in Table.  7  These data show that the invention can be effective when using source gases containing some non-hydrocarbon gases, such as hydrogen, without degrading the properties of the membrane.  Examples of HPALC To illustrate the direct introduction of a complexing solution into a gel membrane during its formation, semi-.  chaA) t gel A by displacing 1 h. liquid 12 wt. % of water-soluble polyvinyl alcohol, mol.  weighing 1820 in dimethyl sulfoxide (DMSO) with 1 mol of silver nitrate and 1 hour. liquid 20 wt. % solution of toluene diisocyanate in DMSO.  This mixing is done in a round bottom flask.  After 20 min, gel formation occurs.  The gel is removed from the bottom of the flask and washed with water.  The gel is molded to form a hydrophilic film with a thickness of 0.375-0.5 mm and placed between. two sheets of filter paper until further use.  Gel B is prepared in the same way, except that no N-silver nitrate is added to the gel-forming mixture containing polyvinyl alcohol.  After gel formation, it is washed and soaked with paper to dryness.  The film is then immersed in a 1-molar aqueous solution of silver nitrate for two days.  The membrane (gel B) is removed from the solution and blot dry with filter paper.  PRI me R s 32 and 33.  The test cuvette is divided into upper and lower compartments by placing either. films from gel A, or films from gel B horizontally along the cuvette.  . Internal cross-section of the cuvette.  is 3.8 cm.  This cross section is covered with a fully film membrane so that the effective membrane surface is 2.2 cm.  The height of the main body of the cell is 41 mm, with gas holes at each end.  The inner tube for feeding the initial mixture enters the upper end of the cuvette and its opening is located 5 mm above the film, and the tube for introducing the purge gas enters the lower end of the cuvette and its opening is located about 1 mm below the film.  The moistened mixture of raw hydrocarbons is loaded under pressure into the upper part of the cuvette at a rate of 10 ml / min in contact with the membrane, and the spent or purified gas components exit from the cuvette through the upper opening.  The speed of the initial mixture is considered sufficient if a constant gas composition is maintained on the inlet side of the membrane.  The flue gas purge, 10 ml / min., Contacts the lower surface of the membrane and entrains hydrocarbons that penetrate the membrane and then leaves the membrane through the lower outlet opening to form the target flow.  The product is analyzed using gas chromatography, with helium being used as the carrier gas.  The transmission rates are calculated based on the amount of hydrocarbon in the carrier gas, the flow rate of the carrier gas, and the response of the detector to a gas chromatograph per ml of the gas mixture under investigation.  Experiences. carried out at ambient temperature.  The results of these experiments are given in table.  eight.  The data show the selectivity of the system for the distribution of ethylene.  Each of the films provides the desired separation, but the best qualities of gel B may be due to the removal of silver nitrate from gel A as a result of washing.  PRI me R 34.  The membrane is made by dissolving 5 wt. h  a kaylon resin, which is an alcohol-soluble polyamide, and 0.5 weight. h  water-soluble polyvinyl alcohol with mol.  weighing 1820 to 94.5.  DMCO.  The mixture is heated to dissolve the polymer, and then cast onto glass. plate using the Byrd applicator with a slit size of 0.015 mm.  The resulting film is dried for 30 minutes in an oven at 45 ° C.  The film.  then it is sharply cooled in distilled water and kept immersed for 20 hours.  The film is dried with filter paper and impregnated with 6 and.  an aqueous solution of silver nitrate for 2 hours  The hydrophilic film is removed from the solution, dried, and then subjected to an apparatus test: as described in Example 32.  Hydrocarbon feed mixture, approx. in this experiment1. They are saturated with water vapor and loaded into a cuvette under a pressure of 0.7 kg / cm at a rate of 25 ml / min.  Nitrogen is used as a purge gas to remove products that have passed through the film.  Get the results presented in table.  -9.  The selectivity factor for olefins obtained from this experiment is co; is 6.75.  Example 35  The membrane is made by dissolving 27 g of nylon resin and 3 g of water-soluble polyvinyl alcohol, mol.  weighing 1820 in 120 ml DMCO.  The mixture is heated to ez.  to dissolve the polymer, and then cast on a glass plate using the Byrd applicator with a slit width of 0.015 mm.  The resulting film is partially dried for a minute in a vacuum oven at, va kzgume. 15 and an air flow rate of 500 ml / min.  The film is then rapidly cooled in a 0.5% sodium nitrate solution.  The hydrophilic film is removed from the brine, dried and subjected to tests in the apparatus described in Example 32.  In this experiment, 0.5 ml of a 5-molar solution of silver nitrate is placed on the top of the membrane.  The cuvette is closed and the initial mixture is introduced under pressure I, A kg / cm.  After a few hours, the silver nitrate solution penetrates the film.  The initial stream of hydrocarbons used in this experiment is moistened with water vapor and loaded into the cell under pressure first 0.7 kg / cm and then 1.4 kg / cm (everywhere at a rate of 25 ml / min).  Wet nitrogen is used as a purge gas to remove hydrocarbons that have passed through the membrane.  Get the results presented in table.  ten.  Example 36  A 0.5 mm thick film of sodium xanate cellulose compound is cast on a clean glass plate using 10 wt. % water mixture.  The film is coagulated by placing the coated glass plate in an O, I8-molar solution of hydrochloric acid for 30 minutes.  The film is washed several times with distilled water and dried.  A part of this gel membrane is placed in an aqueous 6 molar solution of silver nitrate, containing 5 wt. % of water-soluble polyvinyl alcohol, mol.  weighing 1820.  The hydrophilic membrane (gel B) is made up in solution for 2 hours, and then blotted with paper to dry.  Example 37  Ethylene glycol monomethacrylate is polymerized.  The polymer is dissolved in methanol to obtain a 10% solution.  And parts of the solution formed a film with a thickness of 0.375-0.5 mm at the bottom of the round bottom bowl, and the solvent was gradually evaporated.  A part of the shoulder is impregnated with 1-molar aqueous silver nitrate jar for 24 hours.  The hydrophilic membrane is then dried by blotting on filter paper and subjected to tests (gel D).  Examples -38 and 39.  Each of the gel membranes, prepared as described in Examples 36 and 37, are subjected to tests for the acceptability of the process for separating ethylene from a mixture also containing methane and ethane.  The test cuvette is similar to the cuvette described in Example 32.  The gaseous feed mixture is passed through water at 37 and injected into the cuvette at a rate of 10 ml / min. Under pressure. .  Helium is used as a purge gas, which is supplied at a rate of 10 ml / min.  The results of the experiment show that both films are effective for ethylene separation.  The results of the experiment are given in table.  eleven.  Example 40  Two membranes of divinylbenzene crosslinked sulfonated polystyrene cation exchange resins with a thickness of 1.12-1.25 mm are impregnated with at least 2 h of a 6 molar aqueous solution of silver nitrate.  The membranes are removed from the silver nitrate solution and blot dry with filter paper.  Each membrane is placed in a cuvette described in Example 3.  The permeability and selectivity of a silver ion containing membrane for ethylene separation is determined using an initial gas mixture containing methane, ethylene, and ethane.  The initial gas stream is injected under a pressure of 2.1 kg / cm at a rate of 10 ml / min.  . The humidification of the source gas is achieved by bubbling it through water at 51.7 ° C.  Edited to the test cell.  The product passed through the membrane is flushed from the cuvette with a stream of gels at a rate of 10 ml / min.  The results of the experiment are given in table. 12.  Note 41.  Several fibers of D Ynarel Electric HD-1 silicone polycarbonate resins with an outer diameter of 0.25 mm and a wall thickness of 0.025 mm are immersed in a 10% aqueous solution of polyvinyl alcohol with a mol.  weighing 1820 with the formation of a hydrophilic film deposited on a fibrous carrier from a hydrophobic resin brand HD-1.  Fibers are treated with a 30% solution of acetone in water for 45 s before applying 19108 coats.  A smooth coating is achieved by wiping the fibers from the coating solution at a controlled speed of 1.25 inches (0.31 cm) per minute.  Dp to ensure full fiber coating is carried out several dives.  After the coating is complete, the fibers are placed in a saturated sodium sulfate aqueous solution,. containing 5% hydrogen chloride, but not less than 18 hours  Hydrogen chloride plays the role of a crosslinking agent for the coating and makes it insoluble in water.  The fibers are then washed several times with distilled water to remove all salts.  After drying the grain of the fibers, they are collected to form a single hollow fiber membrane.  The fiber ends are placed in a General Electric grade PTV-616 silicone resin, which is then cured.  The ends of the fibers are re-opened and cut into small portions of resin and fibers.  The six fibers obtained are 2 cm long and an outer diameter of 0.275 mm.  This corresponds to an effective membrane area of 9.9 cm per membrane.  The fibers are impregnated with a 1 molar solution of silver nitrate by filling the tube with silver nitrate and applying pressure to the inlet side, which allows silver nitrate to penetrate into the coating for the fiber.  An excess of silver nitrate is then removed from the cuvette.  To test the coated fibers impregnated with a solution of silver nitrate, the source gas stream was introduced into the cuvette at a speed of 10 mo / min under a pressure of 1.4 kg / cm.  The feed gas contains methane, ethylene and ethane.  On the side of the fibers, a stream of nitrogen is continuously purged at a rate of 10 ml / min, which carries with it the gas passing through the fibers.  The composition of this stream is determined by vapor phase chromatography.  In tab.  13 collected data from this experience.  They represent the average of 19 measurements taken over 7.5 hours.  Example 42  A mixture of 40 g of nylon 6: 6 modified with formaldehyde and alcohol is prepared. m (VSG-819, Belding Chemical Industries), 60 g of polyvinyl alcohol (mol. weight 1820) and 120 ml of DMCO as an extrusion mixture, t. e.  dry polymers are first mixed, and then DMCO is added.  The resulting slurry is heated in a feed tank for an extruder for 1.5 hours, which leads to the melting of the polymers and the removal of gases from the mixture for extrusion.  The mixture is extruded under a nitrogen pressure of 14–70 kg / cm in a nutrient hopper and when the extruder is heated to 76 C.  Hollow fibers are formed from a polymer mixture that passes through an annular mouthpiece with openings 76.7 mm in size.  During extrusion, air is blown through the central part of the fibers.  After extrusion, they stretch up to 25-75% of their original length under controlled tension of the fibers and when heated to 65.693, 3 C.  The drawn fibers are crosslinked by immersion in a 3% solution of p-toluene sulfonic acid in a bath containing 10% aqueous solution of sodium sulfate for 90 minutes at 50-60 ° C. The fibers are then washed several times with water to remove salts from them and gradually dried.  Then the ends of three such fibers are inserted together into a stainless steel tube of 2-1 / 2 by 1/4 in size (outer diameter) filled with Armstrong C 4 epoxy resin.  The resin is cured with activator D Armstrong i by heating the mixture of resin with activator at 80 ° C for 60 minutes.  The other ends of the fibers are similarly introduced into various tubes.  The introduction of filament into the tubes is carried out in such a way that small amounts of pre-fill compound can be removed to extract the open ends of each fiber.  The fiber bundles are threaded for 16 hours with a 6 molar solution of silver nitrate and collected in a hollow fiber cell, where the total surface of the membrane is 23.4 cm.  A mixture of ethylene, ethane and methane is then injected under pressure into this cuvette at a flow rate of 10 ml / min.  The initial mixture is watered from the outside of the fibers and moistened by bubbling it through the water at 62, before entering the cuvette.  From the inside, the fibers are continuously flushed with gels at a rate of 10 ml / min, which carries substances passing through the hair.  Gas chromatography is applied to determine the rate of prozkhtseni prozdavogo flux and selectivity of fibers to ethylene.  As can be seen from the table.  14, the resulting system allows the ethylene to be successfully removed from the feed.  These data show the advantages of using the proposed method 108865922
    bu film membranes containing significant amounts of nylon and polyvinyl alcohol. Such films contain about 25-75% by weight of each of these components, preferably 45 to 65% by weight of nylon and 35 to 55% by weight of polyvinyl alcohol. Table 1
    JJ ..
    F And - the factor of selectivity, i.e. the ratio of permeability of ethylene compared with the permeability of methane and ethane.
    41,036.9
    22.1
    one
    96.91.8 AgNOg 1.31
    97,81,24 0,91 AgNOj AgNOj
    99,570.18 0.25
    69.720,95 CuCNO) 9.8
    gNOj + 0.5M Cu (NOj 1.1 97.61.3 Cu (NO j) 2 0.91
    97.81,3
    AgNOj + SM C (Koz) 2 0.47 98j90.61
    table 2
    8.37 8.87 7.45.
    0.079
    0.082
    0.085
    0,0078
    0.079
    0.070
    0.064
    Original 1M AgNOj
    1M AgNOg + CrCNOj: W AgNOj + Ni (NO) 2 W AgNOj + Zn (N03) 2 W AgNOjtCd (N03) 2 1M AgNOj + AKNOj) W AgNO + LiNQj
    W AgNOj + SrCNO-) W AgNOj-t-CaCNOj)
    1M AgNOj + MgCNOj) W AgNOj + CoCNOj) W AgNOj + FeCNOg) 1M AgNOj + NaNO
    W AgN03 + Pb (N03) 2 W AgNOj + NH NC 1M AgN03 + KN03 W AgNOg + UO CNOj)
    Table 3
    12.5 10.5 14.02 32.47 21.04 Source 0.0578 0.88 67.00 1.27 CuCl-NH Gl CuCl-NH Cl-HCl 0.0979 0.52 73.37 1.19
    Initial
    41.0
    22.1 74.5 7.9 86.2 4.8 89.8 3.6
    Table 4
    Table 6
    0,017
    4.2 0.023 9.0 12.7 0.030 32.47 - 6.16 8.16 4.935.44 30.85 25.0 24.92 31.6 Table 5
    27
    Initial
    mix5,932,8
    . 200,0160.122
    400,0180,12
    Source mixture
    20 623.42.05 11.4 16.4 1.21 2.71 40 623.4 3.22 17.9 25.9 1.91 4.26
    Selectivity factor for unsaturated compounds,
    The materials are not defined in the composition after the passage, and their number is considered insignificant or zero for normalization purposes. FI 108865928
    Table 7
    47.4 3.5 7.8 2.4 84.52, 35 - 82.45, 42 -
    Table 8 is the selectivity factor, i.e. the ratio of ethylene passed through the membrane to methane and ethane.
    13.39 31.80 22.59 32.22
    Original
    After passing through the membrane52, 25 4.79 40.07 to 2.90
    Table 9.
    64.02
    5.92 8.035,325,42
    92.32
    Table10
    Membrane
    Established.
    32.7
    17.2
    50.1
    5, 4
    2.4
    92.2
    Ta b faces 12
    9.43 15.7 9.56
    11.8 0.034
    T a b c a 14
    5.60 8.87
    5.22
    r4
    695 8.59x10
    权利要求:
    Claims (3)
    [1]
    1. METHOD FOR ISOLATING CIP-Cg ALIPHATIC UNSATURATED HYDROCARBONS FROM VAPOROUS HYDROGEN> MIXTURE by contacting it with one side of a solid water-insoluble semipermeable membrane with a partial pressure of unsaturated hydrocarbons to the membrane exceeding the partial pressure after it, with the removal of the isolated unsaturated aliphatic membranes characterized in that, in order to increase the selectivity of the process, use a membrane in contact with a layer of liquid complex brazavatel containing water and metal ions selected from the group consisting of sodium, lithium, potassium, silver, copper, magnesium, calcium, strontium, aluminum, lead, chromium, iron, cobalt, nickel, zinc, ammonium ions , uranium, mixtures thereof, and semi-permeable to liquid complexing agents.
    [2]
    2. The method of pop. 1, characterized in that they use a membrane in contact with the ’layer of a liquid complexing agent located on the supply side of the initial mixture.
    [3]
    3. The method of pop. I, characterized in that they use a membrane inside which is a layer of liquid complexing agent.
    Priority on points:
    05/12/72 for PP. 1 and 2; 09/13/72 under item 3.
    cl with oo oo <35
    SL CO
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    同族专利:
    公开号 | 公开日
    JPS4948603A|1974-05-11|
    DE2323657B2|1978-08-24|
    DE2323657C3|1979-04-19|
    FR2184809A1|1973-12-28|
    DE2323657A1|1973-11-22|
    AU5951173A|1975-03-20|
    AU476688B2|1975-03-20|
    FR2184809B1|1979-04-13|
    NL7306466A|1973-11-14|
    JPS5331842B2|1978-09-05|
    IT985014B|1974-11-30|
    NL158088B|1978-10-16|
    CA1000307A|1976-11-23|
    GB1431946A|1976-04-14|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US4272364A|1980-03-24|1981-06-09|Calgon Corporation|Frother for coal flotation|
    JPH0364544B2|1982-08-02|1991-10-07|Mitsubishi Reiyon Kk|
    CN103796742B|2011-06-07|2016-03-09|依姆泰克斯膜公司|Film liquid make-up material|
    US9056283B2|2012-03-02|2015-06-16|Saudi Arabian Oil Company|Facilitated transport membrane for the separation of aromatics from non-aromatics|
    US10471381B2|2016-06-09|2019-11-12|Uop Llc|High selectivity facilitated transport membranes and their use for olefin/paraffin separations|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US25260772A| true| 1972-05-12|1972-05-12|
    US28878172A| true| 1972-09-13|1972-09-13|
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