REVERSE OSMOSIS MEMBRANE QUENCHING

Abstract: In the preparation of permselective membranes by extracting a solvent-cast membrane with non-solvent, the improvement of quenching with a polar liquid before extraction.

Description: TITLE Reverse Osmosis Membrane Quenching BACKGROUND OF THE INVENTION Asymmetric membranes have long been used in a variety of purification operations. Permeation selective or permselective membranes preferentially pass certain components of liquid mixtures while retaining other components. In reverse osmosis membranes, a hydrostatic pressure in excess of the equilibrium osmostic pressure of the liquid mixture or solution is applied to the liquid to force the more permeable components, usually water, through the membrane in preference to the less permeable components, such as a salt, contrary to the normal osmotic flow. In the preparation of membranes for these applications, a film or hollow fiber is first cast from a casting dope. This film is then extracted by treating with a nonsolvent to replace the original casting solvent. Continuous effort has been directed toward the improvement of this process to increase the flux and salt rejection of the final membrane. SUMMARY OF THE INVENTION The instant invention provides an improvement in the process for preparing reverse osmosis membranes which improves the membrane characteristics during subsequent processing. Specifically, the instant invention provides, in the process for preparing perselective A membranes by extracting a membrane composed of polymer, organic solvent and optionally dissolved salt and water with a nonsolvent for the polymer to extract the solvent and the salt, the improvement wherein the membrane is contacted, before extraction, with an aqueous quenching liquid for a period of about from 5 seconds to 5 minutes, the quenching liquid comprising about from 5 to 50 weight percent of at least one polar liquid selected from the group consisting of alkanols and alkane diols and triols of 1-4 carbon atoms and carbonyl compounds of the general formula EMI2.1 wherein A is H, NH2, CH3, or CH2CH3 and B is H, OH, NH2, CH3, NHCH3 or N(CH3)2. DETAILED DESCRIPTION OF THE INVENTION The instant invention is applicable to those polymeric reverse osmosis membranes previously used in the art. The typical preparation of these polymers involves first casting a "proto-membrane" consisting of polymer, organic polar solvent, and, in general, dissolved salt and water. The proto-membrane is then typically extracted by contacting it with water which frequently serves as the storage medium for the finished membrane. Such polymers and their preparation are described in detail in Richter, et al, U.S. Patent 3,567,632, hereby incorporated by reference. The present invention is based on the discovery that the subsequent processing of a permselective membrane is facilitated and the final properties of the membrane are improved if the membrane is first quenched, prior to extraction, with a liquid containing about from 20-50% of certain polar compounds. These compounds include alkanols and alkane diols and triols of 1-4 carbon atoms and carbonyl compounds of a general formula EMI2.2 wherein A is H, NH2, CH or CH2CH3 and B is H, OH, NH21 CH3, NHCH, or N(C}33)2. Alkanols that are preferred in the instant process are methanol and ethanol. The preferred glycols are propylene glycols and ethylene glycol. Representative carbonyl compounds which can be used in the instant invention include formic acid, acetic acid, propionic acid, formamide, acetone, dimethyl formamide, dimethyl acetamide and urea. Of these, formic acid, formamide, and urea are preferred, and formic acid provides a particularly outstanding combination of performance characteristics, ease of handling and ready availability. The concentration of the above compounds in the quench solution should be about from 5 to 50 weight percent. The concentration is preferably about from 20 to 40 weight percent for flat membranes and about from 5 to 20 weight percent for hollow fibers. Less than 5% does not generally provide a significant benefit to the overall process, while concentrations in excess of 50% result in depreciation of the performance characteristics of the final permselective membrane. Because of the water solubility of each of the presently required polar compounds, they can be combined with the aqueous quench solution by simple mixing. The unextracted or proto-membranes should be contacted with the quench solution for a period of about from 5 seconds to 5 minutes. A period of about from 5-20 seconds is generally preferred to minimize the degree of solvent and salt extraction in the. quenching stage. Contact times in excess of 5 minutes generally result in a modification of the polymer structure which results in a weaker membrane, having less mechanical stability, and which therefore exhibits poorer flux and rejection characteristics in extended use. The instant process is applicable to a wide range of temperatures extending from the freezing point of the liquid up to the drying temperature used for the membrane. Preferably, a temperature from about from 10 to 300C is used. The process of the instant invention results in membranes having particularly high flux and improved resistance to long-term exposure to elevated temperatures. These benefits are due in part to the quenching step of the instant process, which sets or stabilizes the membrane prior to final extraction. The invention is further illustrated by the following specific examples, in which parts and percentages are by weight unless otherwise indicated. Example 1 and Comparative Examples A-B For Example 1 and Comparative Examples A and B, an aromatic copolyamide was prepared from m-phenylene diamine and m-phenylene diamine-4-sulfonic acid (8/2 mole ratio) with isophthaloyl and terephthaloyl chlorides (7/3 mole ot2#0C ratio) with an inherent viscosity OL 0.75 dl/g (0.5% in DMF). 20 parts of the polyaramide and 11 parts of MgC12 6H2O were dissolved in 80 parts of dimethyl formamide and the resulting solution filtered through a filter of 5 micron porosity. From this solution, membranes were cast on a glass plate at 950C, and dried for 120 seconds. The membranes were cooled in air for 90 seconds and then quenched for 15 minutes in formic acid or water as indicated below. The membranes were extracted in water at room temperature for 45 minutes, followed by annealing in water at 600C for 30 minutes The membranes were stored in water until test#6d#. The membranes were tested for reverse osmosis performance in stirred monel cells using salt solutions at concentrations of 1.5 to 3.2 g/l at pressures up to 800 psi. Fractional rejection of salt and the flux constant of the water, reported in Tn/s.TPa, were calculated from the conductivity of the permeate water and its rate of flow through the membrane. The results are summarized in the following Table I. TABLE I Quench As prepared After 140 hrs in H20 Example Medium Rejection Flux Constant Rejection Flux Constant A Water at 40C 0.986 1.32 0.958 1.00 for 15 mins B 85% Formic 0.955 0.75 0.938 0.65 acid at 50C for 15 mins 1 50% Formic 0.979 1.63 0.959 1.47 acid at 50C for 15 mins The membrane quenched in 50% formic acid before extraction not only exhibits higher flux levels as prepared but sharply better performance on aging. Examples 2-4 and Comparative Examples C-D A series of membranes was prepared and tested substantially as in Example 1 except that the concentration of formic acid was varied. The results are summarized in the following Table II. ?aBLE II As prepared After 132 hrs at 550C Exart## Quench Flux Flux ple Medium (50C) Rejection Constant Rejection Constant C Water 0.981 1.334 0.922 1.067 D 65% Formic 0.979 1.185 acid 2 50% Formic 0.982 1.945 0.954 1.544 acid 3 40% Formic 0.976 2.022 0.952 1.620 acid 4 258 Formic 0.984 2.174 0.956 1.549 acid Membranes prepared according to the present invention exhibit superior flux both as prepared and after aging. Examples 5 & 6 The general procedure of Example 1 was repeated, except that the membranes were quenched in 35% formic acid for a very short period. The results are summarized in the following Table III. TABLE III As prepared After 132 hrs at 550C Exam- Quench Flux Flux ple Period Rejection Constant Rejection Constant 5 1 sec 0.972 2.045 0.948 1.897 6 4 secs 0.966 2.182 0.949 2.018 Comparative Example E and Examples 7-12 A series of hollow fiber samples were spun by standard dry spinning techniques followed by immediate in line quenching with water or formic acid solutions. The spinning rate was 20 m/min through a 1 meter long drying cell kept at 175-1800C. The solution temperature at the spinneret was 125 + l0C. The solution was pumped through a one hole spinneret at the rate of 10 cc/hour. The solution viscosity was 810 poises at 1200C. The fibers were assembled into test permeators and evaluated. The results are summarized in the following Table IV, together with the outer and inner diameters of the fibers in microns. TABLE IV % Formic Outer Inner Exam- Acid in Diam- Diam- Flux ple Quench Bath eter eter Rejection Constant E 0 101 30 0.896 0.32 7 4.2 104 38 0.955 0.60 8 10.4 100 35 0.942 0.68 9 14.5 113 35 0.895 0.58 10 20.4 113 39 0.930 0.43 11 28.6 114 33 0.850 0.25 12 40.0 117 31 0.380 0.14 Examples 8-42 and Comparative Example F A copolyaramide was prepared from m-phenylene diamine and isophthalic and terephthalic acids in the ratio of 70/30, with one-fifth of the diamine residues sulfonated in the 4-position to give a copolyaramide with 2.5 weight % sulfur. Its inherent viscosity, as determined at 0.5 g/100 ml of dimethyl formamide was 0.75-0.8 dl/g. The copolyaramide was dissolved (18 parts by weight) with 10.3 parts of MgCl2#6H2O in 17.7 parts of dimethyl formamide and the resulting solution then filtered through a 5 micron filter. Membranes were cast on a glass plate at 950C with a Gardner knife at varying thickness, dried under a stream of nitrogen, and quenched in an aqueous medium before extracting overnight in distilled water. In Comparative Example F, the quench medium was water at 80C. After annealing in water for four hours at the temperatures indicated in Table V, the permeability properties of the membranes were determined in stirred cells, with a feed solution containing 3.5 grams per liter of sodium chloride. The data shown were obtained at 22-30C and 800 psi pressure, and are expressed as R/Kw, where the rejection, R, is the fraction of the salt that is turned back by the membrane, and Kw, in meters per second per TeraPascal, is the hydraulic permeability constant. TABLE V Exam- Cast Dry Quench Annealed at ple mils mins Additive 8 550C 650C 750C F 15 2 - - .983/1.48 8 " " Methanol 20 .994/2.57 9 " " 35 .992/2.70 10 " " " 50 .981/2.50 11 " 2.5 Ethanol 20 .989/3.05 .988/1.66 12 " 3 n 35 .986/2.85 13 " 2.5 " 50 .958/2.80 .978/2.30 14 n 2.5 - - .991/2.80 .983/1.70 15 n n Formic 35 .983/3.82 .983/2.85 Acid 16 11 2 " 25 .984/2.53 17 " n n 45 .988/2.12 18 n 2.5 " 35 35 .985/2.06 600C 700C 19 " 2 n 35 .978/2.21 .973/1.90 20 " " Acetic 45 .976/2.28 .961/1.61 Acid 21 n n Propionic 56 .967/2.00 .940/1.78 Acid 22 15 3 Acetone 20 .982/1.83 23 " " " 28 .992/2.10 24 n n n 40 .985/2.37 25 " n n 45 .947/2.71 .971/1.83 26 " " " 55 .861/2.21 .940/1.31 27 " 2 - - .975/1.64 28 " " Formamide 20 .993/2.61 29 " " Acetamide " .995/2.29 30 " " Propion " .995/2.23 amide 31 " " Dimethyl 15 .992/2.39 Acetamide 32 " " " 25 .993/1.04 33 " " " 35 .972/0.63 34 " " - .983/1.48 35 " 2.5 - - .991/2.80 .983/1.70 36 " " Formamide 35 .980/4.21 .985/3.37 37 " 2 Urea 30 .992/2.64 38 " " " 40 .970/2.91 39 " " " 50 .986/2.52 40 " 3 Dimethyl 20 .989/1.77 Formamide 41 " n n 30 .988/1.74 42 " " " 45 .870/0.70

Claims: I CLAIM: 1. In the process for preparing peraselective membranesby extracting a membrane composed of polymer, organic solvent and optionally dissolved salt and water with a nonsolvent for the polymer to extract the solvent and the salt, the improvement wherein the membrane is contacted, before extraction, with an aqueous quenching liquid for a period of about from 5 seconds to 5 minutes, the quenching liquid comprising about from 5 to 50 weight percent of at least one polar liquid selected from the group consisting of alkanols and alkane diols and triols of 1-4 carbon atoms and carbonyl compounds of the general formula EMI13.1 wherein A is H, NH2, CH3, or CH2CH3 and B is H, OH, NX2, CH3, NHCH3 or N(CH3)2. 2. A process of Claim 1 wherein the polar liquid consists essentially of formic acid. 3. A process of Claim 1 wherein the polar liquid consists essentially of formamide. 4. A process of Claim 1 wherein the polar liquid consists essentially of dimethyl acetamide. 5. A process of Claim 1 wherein the aqueous quench solution is maintained at a temperature of about from 10 to 300C. 6. A process of Claim 1 wherein the membrane is in the form of a hollow fiber and the aqueous quenching liquid comprises about from 5 to 20 weight percent polar liquid. 7. A process of Claim 1 wherein the membrane is in the form of a flat sheet and the aqueous quenching liquid comprises about from 20 to 40 weight percent polar liquid. 8. A semipermeable membrane resulting from the process of Claim 1.

Inventors: SUNDET, SHERMAN ARCHIE
Applicants: E.I. DU PONT DE NEMOURS AND COMPANY
Application year: 1982
Main classification: B01D13
IPC codes: B01D67, B01D71