Patent Application
20050173345
The present invention relates generally to polymeric membranes for separating acid from acid mixtures. More particularly, it relates to particularly adapted polymeric membranes and their use in separating and recovering acids, including sulfuric acid from waste acid mixtures or streams. These streams may comprise acid, and any combination of acid and hydrocarbons and/or water and other “contaminants”, using polymeric membranes.
Numerous industrial processes use acids in their processing that contaminate the acid with process by-products in waste. These contaminated acids are commonly referred to as “spent acid”. Industrial chemical and petroleum processes are prime examples. Many of these processes require purification or regeneration of the process acid to remove impurities, which often require costly processing. Handling spent acid also raises safety and environmental concerns. Accordingly, there is ample need for a separation process to efficiently and effectively remove impurities from process contaminated acids to restore the acid to or near its original process specification. It would also be beneficial if that process could be deployed “in situ” with the process that produced the spent acid. The present invention is directed to a polymeric membrane that is suitable for acid-contaminated separation and its use in “regenerating” process acids. The polymeric membrane withstands the acid environment and preferentially diffuses the acid over the retentate contaminant. The process can be practical “in-situ” with common petroleum and petrochemical processes. Though particularly described hereinafter in relation to use in a petroleum processing stream, the polymeric membrane has application to varied acid/liquid separations.
Acids are widely used in industrial chemical and petroleum refining applications that require acid “regeneration,” which generally means removal of contaminants (including often water) from the process acid to restore the acid to, or near to, its original process specification or requirements. An exemplary acid use to illustrate the present invention is sulfuric acid, which is used in a number of petrochemical and petroleum refining processes.
Sulfuric acid is widely used in industrial chemical and petroleum refining processes. Depending on the use, commercial “fresh” acid is typically supplied in strengths of 70-99.5 wt % sulfuric acid with the remainder typically being water. Many uses generate a waste or spent acid stream containing organic hydrocarbon materials. This spent acid stream is typically reprocessed to remove the organic material. Incineration and reconstitution of the sulfuric acid is conventionally used to remove the organic material.
An exemplary petroleum processing use of sulfuric acid is as a catalyst for alkylation processes. In a typical alkylation process the relatively high purity, concentrated sulfuric acid becomes diluted or contaminated with water and organic hydrocarbon materials commonly referred to as acid soluble oil (ASO). When sufficiently diluted or contaminated, the catalytic activity of the acid degrades. Spent sulfuric acid from the alkylation process can be regenerated but at a considerable cost using existing methods.
Conventional methods for spent acid regeneration involve generally combustion of the spent acid to form sulfur dioxide, conversion of the sulfur dioxide to sulfur trioxide, and absorption of the sulfur trioxide in water. While this technology is widely used to produce high strength acid (>98 wt % H2SO4), it is capital intensive. Thus, it is usually more economical for low volume users of sulfuric acid to transfer spent sulfuric acid by various means such as rail, truck, ship, or pipeline to a central regeneration facility rather than construct their own facilities for acid regeneration. Freight costs can be a significant part of the total costs for regenerating spent acid.
Sulfuric acid can also be concentrated from about 70 wt % H2SO4 to about 85 wt % or about 96 wt % sulfuric acid by using evaporation with one or two stages. The evaporation method is highly energy intensive as the acid/water mixture must be heated to a high temperature to vaporize the water. It also requires special materials such as glass lined vessels and tantalum heaters to prevent corrosion. An improved, less expensive method for regenerating spent sulfuric acid is needed.
The present invention, relates generally to an improved polymeric membrane and its use in regenerating spent acid. One embodiment of the present invention relates to particularly adapted crosslinked polymer membranes that are capable of withstanding an acid environment and its use in a method for recovering an acid such as sulfuric acid from a feed mixture comprising acid, hydrocarbons and water. The method comprises processing said mixture using a the polymeric membrane to form a first retentate containing a substantially greater concentration of hydrocarbons than the feed mixture and a first permeate containing a substantially greater concentration of acid and water than said feed mixture. In another embodiment, the method comprises processing the first permeate using a second polymeric membrane to form a second retentate containing a substantially greater concentration of acid than the first permeate and a second permeate containing a substantially greater concentration of water than the first permeate, and recovering said second retentate. A further embodiment includes conventional processing of the first retentate.
Yet another embodiment of the present invention relates to an improved alkylation process. The alkylation process comprises contacting an olefin mixture with an isoparaffin mixture in the presence of a liquid acid catalyst under conditions effective to produce an alkylate product. The liquid acid catalyst can be any liquid acid suitable for catalyzing the alkylation reaction such as sulfuric acid. The spent acid which is a mixture comprising sulfuric acid, hydrocarbons and water is recovered and processed using a first polymeric membrane to form a first retentate containing a substantially greater concentration of hydrocarbons than said spent sulfuric acid mixture and a first permeate containing a substantially greater concentration of sulfuric acid and water than the spent acid mixture. In one embodiment, the first permeate is recycled back to the alkylation reactor. In a second embodiment, the first permeate is optionally further processed to reduce its water content. Optimally, this further processing includes evaporation under vacuum, adding acid anhydride, adding oleum, or using a second polymeric membrane to reduce water content. Each further processing will form a first stream containing a substantially greater concentration of sulfuric acid than said first permeate and a second stream containing a substantially greater concentration of water than said first permeate. The first stream is recovered and recycled to the alkylation process.
FIGS. 1 to 5 are simplified schematics of different embodiments of the present invention.
The present invention relates generally to polymeric membranes for separating acid from acid mixtures. More particularly, it relates to particularly adapted polymeric membranes and their use in separating and recovering acids, including sulfuric acid from waste acid mixtures or streams. These streams may comprise acid, and any combination of acid and hydrocarbons and/or water and other “contaminants”, using polymeric membranes. The membranes of the present invention comprise crosslinked polymer membranes. More particularly, the membrane is a crosslinked polyvinyl alcohol membrane characterized by its crosslink density. Crosslink density as used herein, is defined as percent of available alcohol groups reacted with a crosslinking agent, e.g., 5% crosslinking means that about 5% of the vinyl alcohol groups have been reacted with the chemical cross-linking agent. The membrane crosslink density ranges from about 1.0% to about 25.0%. In a preferred embodiment the crosslink density ranges from about 2.5% to about 20.0%, and most preferably ranges from about 5.0% to about 10.0%. While not fully understood, the crosslink density, as taught herein, produces a membrane that may be adapted to withstand acid environments typically encountered in petroleum processing applications such as sulfuric acid alkylation for example. The degree of crosslinking is also believed to influence the selectivity and flux characteristics of the membrane, in addition to its mechanical and structural stability. The PVA membrane is preferably crosslinked using 1,4 diisocyanatohexane before use in an acid environment. Preferably the membranes are made of crosslinked PVA, PVS and other oxoanion modified PVAs. Other suitable crosslinking agents include 1,4 diisocyanatobutane, 1,8 diisocyanatooctane, 1,12 diisocyanatododecane, 1,5 diisocyanateo-2-methyl pentane, and 4,4′ diisocyanato-diphenylmethane. In a preferred embodiment, the crosslinked PVA membrane described above is contacted with a sulfur-containing agent such as sulfuric acid, sufficient to react with the hydroxyl groups of the PVA membrane to form sulfate groups. The crosslinked polymer thereby becomes a polyvinyl sulfate membrane (“PVS”), or a copolymer of vinyl sulfate and vinyl alcohol, (“PVS/PVA”). The PVS and/or PVS/PVA membranes are suitable for membrane application in acid environments, such as sulfuric acid membrane application where acid strength may range from about 70% to about 98 wt % acid. The term “acid environment”, when used herein, means a liquid or fluid substance containing about 70% to about 98 wt % acid. In addition to poly(vinyl sulfate), other membrane materials can be poly(vinyl phosphate) and or other vinyl groups which may have affinity to sulfuric acid or an affinity to the particular acid comprising the acid environment.
In addition to the formation of polyvinylsulfate (PVS) from the reaction of polyvinyl alcohol with sulfuric acid, other inorganic oxoanion modified polymer membranes may be used. They include polyvinyl phosphate membranes made from PVA membranes.
In addition to the phosphate, one can also use arsenate, antimonate, or bismuthate to form polyvinyl arsenate, polyvinyl antimonate, and polyvinyl bismuthate, respectively. Calcogenic oxides, such as polyvinyl selenate and polyvinyl telurate, formed from the reaction of selenic and teluric acids with PVA may also be used.
Another suitable membrane is formed by reacting PVA with boric acid.
In alternative embodiments, other polymerized alcohols and their oxoanion modified compounds, referred herein as oxoanion modified polymerized alcohols may be used in the practice of the present invention. Examples of suitable polymerized alcohols include polypropyl alcohol, polybutyl alcohol, and the like. These structures also may include polymerized alcohol copolymers, polymerized terpolymers, oxoanion modified polymerized alcohol copolymers, oxoanion modified polymerized alcohol terpolymers and the like. These also would form the corresponding modified polymers.
In a preferred embodiment, the membrane is supported by a secondary membrane such as teflon or Gore-Tex™ for example, having a membrane pore size selected to compliment the pore characteristics of the primary membrane. The secondary membrane may also serve as a suitable substrate for the formation, deposition or coating of the primary membrane.
In separating acid from acid waste streams the flow rate of the feed across the membrane surface should be sufficient to prevent undue selectivity loss by concentration polarization. The flow rate of the feed depends on the particular geometry and configuration of the membrane and any supporting or containment vessel used, as well as on temperature. Generally, higher temperatures, lower flow rates can be tolerated. Establishing the optimum flow rate for a membrane configuration and set of operating conditions can be readily determined by a skilled practitioner.
High flux can be achieved by operating with the thinnest membrane that will maintain its physical integrity under the operating conditions. To help the membrane maintain its physical integrity, a composite membrane may be used. For example, a thin selective polymeric layer (or membrane) may be supported on a non-selective, highly porous membrane, to produce a laminate structure. The selective membrane layer is preferably securely attached on top of the porous membrane material which constitutes a physical support. The thin polymeric layer may range in thickness from 1 micron to 50 microns.
The membranes used in the process of the present invention may be utilized in the form of hollow fibers, tubes, films, sheets, etc. The process may conveniently be carried out in a test cell which is divided into compartments by means of a membrane or membranes. The compartments will each have means for removing the contents therefrom. The process may be carried out continuously or batchwise, but preferably in a continuous manner.
In one embodiment, the feed to a membrane unit is maintained under conditions of pressure such that substantially all of the acid is in liquid phase. The permeate may be withdrawn in a vacuum, which is generally maintained in the range of 2 to 150 mm Hg. The permeated phase will be in a vapor phase, and subsequently condensed by cooling in a condenser. This process is generally known in the art as pervaporation.
The vacuum on the permeate side of the membrane can affect both selectivity and flux. The selectivity and the flux generally increase as the vacuum pressure on the permeate increases. Higher vacuum pressure can be tolerated at higher temperatures, or with a lower boiling point acid. In yet another embodiment, a sweep gas may be passed across the membrane at a rate sufficient to increase the permeation rate. Suitable sweep gases include carbon dioxide, nitrogen, hydrogen, air, or low boiling hydrocarbons such as methane, ethane or propane.
Alternatively, the permeate side of the membrane may be swept by a liquid perstraction solvent in which the permeate is soluble and which is non-corrosive with respect to the membrane, at a rate sufficient to enhance the permeation rate of the permeable component or components through the membrane. Suitable perstraction solvents include higher molecular weight paraffins, organic acids, and compressed gases, e.g., ethane, propane, butane, etc. Especially suitable perstraction solvents are those which do not form azeotropic mixtures with any of the components of the waste acid mixture.
Referring now to
The first permeate 18, referred to as the acid and water product low in hydrocarbons, may preferably contain hydrocarbons in an amount ranging from about 0 to about 7 percent by weight, preferably less than about 5 percent by weight. It may also contain acid in an amount of from about 89 to about 96 percent by weight and water in an amount of from about 3 to about 5 percent by weight.
Retentate 20, may contain hydrocarbon in an amount of from about 7 to about 30, acid in an amount of from about 65 to about 89, and water in an amount of from about 2 to about 4 percent by weight.
In a preferred embodiment, the separation mechanism is understood to be the “solution-diffusion” type. According to this mechanism feed components which have higher solubility in the polymer material get preferentially sorbed and then diffuse through the membrane to the permeate side. Separation is based primarily on sorption and diffusion.
The invention further includes feeding the first permeate 18 via a second pump 22 or some other means to a second membrane unit 24, as illustrated in
Preferably, the acid in the feed stream 10 may range from about 83 to about 95 wt %, ASO (or hydrocarbons) from about 2.0 to about 15 wt % and water from about 0.5 to about 4 wt %. As Table 2 shows, the first retentate 20 contains a substantially greater concentration of hydrocarbons (ASO) than the feed mixture, and the first permeate 18 contains a substantially greater concentration of acid and water than the feed mixture. A substantially greater concentration of hydrocarbons in the retentate than the feed mixture means a concentration of hydrocarbons in the retentate that is greater than the concentration of the hydrocarbons in the feed mixture by at least about 3 wt %, preferably at least about 10 wt % and more preferably at least about 18 wt %. A substantially greater concentration of acid and water in the permeate than the feed mixture means a concentration of acid and water in the permeate greater than the concentration of acid and water in the feed mixture by at least about 1 wt %, preferably at least about 3 wt %, and more preferably at least about 6 wt %.
Also, Table 2 shows that the second retentate contains a substantially greater concentration of acid than the first permeate, and the second permeate contains a substantially greater concentration of water than the first permeate. A substantially greater concentration of acid in the second retentate than the first permeate means that the concentration of acid in the second retentate is greater than the concentration of the acid in the first permeate (i.e., the feed mixture to the second membrane) at least about 1 wt %, preferably at least about 3 wt %, and more preferably at least about 6 wt %. A substantially greater concentration of water in said second permeate then said first permeate means that the concentration of water in said second permeate is greater than the concentration of water in said first permeate at least about 3 wt %, preferably at least about 10 wt %, and more preferably at least about 18 wt %.
In the embodiment of
In one embodiment of the present invention shown in
One advantage of the present invention may be appreciated by reference to an improved alkylation process for the manufacture of higher octane gasoline blending component, the improvement residing in the use of membranes to regenerate the spent acid. Referring now to
More specifically, a fresh isobutane stream 64 is fed to a reactor 70 where it is reacted with olefins 66 such as butenes in the presence of an acid catalyst 69 such as sulfuric acid. The alkylation product 72 from reactor 70 is transferred to a settler 74. Settler 74 separates the alkylation product into a spent acid stream 78 and hydrocarbon stream 76. The strength of the spent sulfuric acid stream 78 is reduced because of moisture and ASO material generated due to undesirable side reactions in the alkylation reactor 70. The hydrocarbon stream 76 from settler 74 is transferred to a wash unit 79 where it is caustic and water washed. Then via line 80 it is transferred to a fractionation column 82 to recover an alkylate stream 86 and an overhead stream 84. The overhead stream 84 contains mainly isobutane with some small amount of propane and n-butane.
The isobutane stream 84 contains soluble water picked up in the caustic and water wash. Of course, water is an undesirable component of the alkylation process, as it dilutes the sulfuric acid strength in addition to causing corrosion problems. The spent acid stream 78 from settler 74 is directed to a membrane unit 62 to remove ASO and water. An ASO rich spent acid stream 92 is then used to reduce the water concentration in the recycled isobutane stream 84 by contacting the two streams in unit 94 so that the water dissolves in the spent acid phase. A dry isobutane recycle stream 96 is mixed with the olefin stream 66 and then transferred to said reactor 70 via line 98. It is also possible to feed stream 66 and stream 96 separately to reactor 70.
This invention reduces the water and ASO concentrations in the alkylation process acid stream, maintaining acid strength in the alkylation process, which in turn maintains or increases the alkylation efficiency, and helps to enhance the octane value of the alkylation product. This process will also reduce the cost of sulfuric acid regeneration by reducing the total amount of spent acid shipped for regeneration.
Yet another embodiment of the present invention includes a crystallization step to remove water from the recycled spent acid, as shown in
In yet another embodiment shown in
The invention will be further illustrated by the following examples.
0.9 g of polyvinylalcohol (PVA) was dissolved into a 50/50 mixture of dimethylsulfoxide (DMSO) and dimethylforamide (DMF). In this particular example, PVA was added to a 15 g/15 g DMSO/DMF solvent mixture. The PVA (Aldrich Chemical Co.) was 99% hydrolyzed and had a molecular weight between 124-186 Kg/mol. The solution was subsequently heated to 80° C. for approximately 5 hours. The solution was then cooled to 10° C. and mixed with 0.084 g of hexamethyldiisocyanate dissolved in a 2.5 g DMSO/2.5 g DMF mixture (also cooled to 10° C.). The solution visually became more viscous due to the reaction of the PVA and the diisocynanate. After approximately 2-3 minutes, the 2.7 wt % solution was cast onto a 0.2 micron pore size Gore-Tex substrate using conventional casting knife procedures. This solvent system was selected due to its favorable solubility characteristics and its corresponding chemical inertness.
The Gore-Tex substrate was placed on a support glass plate. The solution of PVA and crosslinking agent was knife coated on top of the support. The coating was first dried overnight (room temperature) under a continuous flow of nitrogen gas. Further drying was performed by thermal treating the membrane in a vacuum oven at 130° C. for 5 hours to ensure completion of the crosslinking reaction (approximately 5%) as well as to ensure complete evaporation of the solvent. The dried membrane was next tested with a spent acid solution in Sepa®ST membrane cell from Osmonics at 24° C.
The feed was pressurized to 700 psig, and permeate pressure was at atmospheric pressure. Feed and permeate streams were analyzed for compositions. Initial permeate rate was 1.83 kg/hr/m2.
First Test
Second Membrane Tested at 300 psig feed pressure and atmospheric pressure permeate, gave an initial flux of 3.6 kg/hr/m2. Feed and permeate compositions are reported below.
The synthesis procedure described in this example can be used for forming crosslinked polyvinylalcohol membranes and other hydroxyl-containing polymers and copolymers, e.g., copolymers of vinylacetate and vinylalcohol membranes for use in separation of ASO from sulfuric acid in the alkylation process. Several parameters that can be controlled are as follows:
The reaction of the sulfuric acid with a crosslinked (with 1,6 diisocyanatohexane) poly(vinyl alcohol) (PVA) membrane was followed with FTIR. The reaction took place by placing the crosslinked PVA membrane into a spent sulfuric acid fluid. The thickness of the original membrane, as determined by SEM (shown in
The schematic of
In operation to maintain a given temperature, heat exchanger 823 is operatively connected to a chiller 822. The spent acid is directed via line 820 to a membrane cell 816. The permeate which is rich in acid and water is collected in a permeate vessel 818. The retentate rich in hydrocarbons is recycled via back pressure regulator 814 and line 812 to the feed vessel 810. The permeate and retentate are analyzed for acid, water and hydrocarbon concentration using well known techniques. The results of the measurements at 500 psig feed pressure and 20° C. are presented in
The above preferred embodiments are provided for purposes of illustrating the invention and should not be construed as limiting the scope of the invention as delineated by the following claims.
This application is a Continuation-in-Part of U.S. Ser. No. 10/773,789 filed Feb. 6, 2004.
| Number | Date | Country | |
|---|---|---|---|
| Parent | 10773789 | Feb 2004 | US |
| Child | 10947019 | Sep 2004 | US |
