WO2020173510A2 - Dispositif et procédé de concentration de glycérol faisant appel à une membrane fibre creuse de pervaporation - Google Patents

Dispositif et procédé de concentration de glycérol faisant appel à une membrane fibre creuse de pervaporation Download PDF

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Publication number
WO2020173510A2
WO2020173510A2 PCT/CN2020/087360 CN2020087360W WO2020173510A2 WO 2020173510 A2 WO2020173510 A2 WO 2020173510A2 CN 2020087360 W CN2020087360 W CN 2020087360W WO 2020173510 A2 WO2020173510 A2 WO 2020173510A2
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Prior art keywords
membrane
liquid
hollow fiber
pervaporation
pervaporation membrane
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PCT/CN2020/087360
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English (en)
Chinese (zh)
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WO2020173510A3 (fr
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唐宇攀
刘军
汪旺华
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南京惟新环保装备技术研究院有限公司
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Publication of WO2020173510A2 publication Critical patent/WO2020173510A2/fr
Publication of WO2020173510A3 publication Critical patent/WO2020173510A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/08—Hollow fibre membranes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/78—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by condensation or crystallisation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/18—Polyhydroxylic acyclic alcohols
    • C07C31/22—Trihydroxylic alcohols, e.g. glycerol
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals

Definitions

  • the present invention relates to the field of glycerol preparation, and in particular to a glycerol concentration equipment and method based on a hollow fiber pervaporation membrane. Background technique
  • Glycerin has a wide range of uses in industries such as medicine, coatings, textiles, papermaking, cosmetics, food, tanning, electrical materials and rubber.
  • glycerin prepared from natural fats and oils as raw material
  • Synthetic glycerin prepared from propylene as raw material Glycerin synthesized by the above two methods
  • the water content of glycerin is above 70-80%. Therefore, dehydrating and concentrating glycerin is an important part of obtaining high-purity glycerin.
  • the dehydration effect directly affects the quality of the final glycerin.
  • the recovery of glycerin-containing waste liquid produced in industrial applications is also a very important market demand.
  • the main method of removing water from glycerol is distillation.
  • glycerin is very sensitive to temperature, even if the temperature is 150- Under the conditions of vacuum distillation at 180 ° C, there will still be a small amount of glycerol quality change; fifth, the environmental impact is great.
  • Pervaporation as a simple and energy-saving cutting-edge technology, can provide an efficient way to concentrate in the preparation and recovery of glycerol.
  • the current inorganic pervaporation membrane materials on the market have many restrictions: (1) The water content of the original solution cannot exceed 20%; (2) It is very sensitive to impurities, conductivity, pH, etc., and the selective layer is easily divided by acid, alkali, salt, etc.
  • Glycerol is easy to block the selective layer of the inorganic pervaporation membrane due to its high viscosity characteristics, so that the membrane separation performance is rapidly reduced. Therefore, there is currently no suitable pervaporation membrane on the market that can be used for the dehydration and concentration of glycerol, and there are no relevant case studies in industry and academia. Summary of the invention
  • the purpose of the present invention is to provide a glycerol concentration equipment and method based on a hollow fiber pervaporation membrane, which is a brand-new glycerol concentration process, and the use of an original pervaporation membrane can treat high-water content C
  • the triol solution is dehydrated and concentrated to completely replace the multi-stage vacuum distillation technology, so that the energy consumption of the glycerol concentration process is greatly reduced, and the product quality is greatly improved, and the equipment is simple and has the advantages of small footprint and low environmental impact.
  • the present invention provides a hollow fiber pervaporation membrane-based glycerol concentration method, which includes the following steps:
  • step S3 Use a hollow fiber pervaporation membrane to dehydrate, concentrate and filter the clear liquid to obtain recovered glycerol.
  • the crude liquid containing 20%-50% of glycerol first enters the ultrafiltration unit to filter out TSS suspended impurities, where the TSS suspended impurities include cellulose, lignin, protein, suspended particles, etc., the ultrafiltration
  • the unit is implemented as an ultrafiltration membrane, the ultrafiltration membrane is an inorganic ceramic membrane or an organic membrane, and the ultrafiltration membrane is selected from hollow fiber membranes, plate membranes, single-channel tubular membranes or multi-channel tubular membranes.
  • the pore size of the membrane is 0.01-0. 2 microns.
  • the pore size of the ceramic ultrafiltration membrane 01-0. 1 micron;
  • the ultrafiltration membrane is an organic ultrafiltration membrane, the organic ultrafiltration membrane is a hollow fiber membrane, the pore size is 0.01-0. 05 microns, the operating pressure is 0. l -3bar, the purpose of this step is to filter the TSS suspended impurities and protect the pervaporation unit;
  • step S2 the filtered clear liquid obtained in step S1 is collected in a buffer tank, and the filtered clear liquid is heated to a set temperature of 60-100 ° C through a preheater and a heater.
  • the heating temperature of the filtered clear liquid does not exceed 100 degrees Celsius. Therefore, it is guaranteed that the glycerol solution with high water content can be dehydrated and concentrated at less than 100 degrees Celsius, so as to prevent the glycerol from becoming malonaldehyde under high temperature environments.
  • impurities such as polyglycerol, ensure the purity and quality of the final product.
  • an original hollow fiber pervaporation membrane is used to pervaporate and dehydrate the heated filtered supernatant.
  • the hollow fiber pervaporation membrane used in the present invention sequentially forms the inner membrane from the inside to the outside of the membrane.
  • the membrane outer diameter of the membrane is 0.8-1. 5mm, the inner diameter is 0.5-1. 2mm, and the wall thickness is 0.1-0. 2mm.
  • the hollow fiber pervaporation membrane constitutes a pervaporation module, and the permeate side of the pervaporation module is connected to a vacuum unit to maintain a vacuum degree of 5-30 mbar.
  • the moisture diffuses in the pervaporation membrane to the permeate side and condenses After condensing into liquid in the vessel, it is stored in the permeate tank, and the concentrated glycerol enters the product tank after cooling.
  • the gauge pressure on the intercept side of the pervaporation component is 0-3 bar, and the absolute pressure on the permeate side is 5-30 mbar, the purity of the obtained product is 92-95%.
  • it includes at least 1-15 pervaporation components, preferably 5-15 pervaporation components.
  • the present invention provides a glycerin concentration equipment based on a hollow fiber pervaporation membrane, which includes at least an ultrafiltration device, a heating device, a pervaporation device, a condensation device, a conveying device, and a storage device.
  • the conveying device includes an ultrafiltration device and a heating device.
  • the pervaporation device and the condensation device are connected in sequence to complete the dehydration and concentration of glycerol.
  • the ultrafiltration device includes at least one ultrafiltration unit, wherein the ultrafiltration unit is composed of an ultrafiltration membrane module and auxiliary equipment.
  • the ultrafiltration membrane is an inorganic ceramic membrane or an organic membrane, and the ultrafiltration membrane is selected from a hollow fiber membrane, a plate membrane, a single-channel tubular membrane or a multi-channel tubular membrane, and the ultrafiltration membrane has a pore size of 0.01 -0. 2 microns.
  • the ultrafiltration unit is used to filter the TSS impurities in the crude liquid, such as lignin, protein, suspended particles, etc., to protect the subsequent pervaporation unit.
  • the heating device includes at least one preheater and a heater.
  • the waste heat of the preheater is reused, the waste heat of the product is reasonably used to heat the raw material liquid, and the heater functions to heat the material liquid to a specific temperature to increase the pervaporation unit Processing power.
  • the permeation device includes at least one pervaporation membrane group, and the membrane used in the pervaporation membrane group is an original hollow fiber pervaporation membrane.
  • the hollow fiber pervaporation membrane has high water permeability and can be used at temperatures below 100 degrees Celsius Glycerol is dehydrated efficiently, and the condensing device is a condenser to condense evaporated water.
  • the glycerin concentration equipment may be a continuous operation equipment or an intermittent operation equipment.
  • the glycerin concentration equipment includes a first delivery pump 1 and an ultrafiltration device connected in sequence.
  • Unit 2 buffer tank 3, preheater 5, heater 6 and pervaporation membrane group 7, wherein the permeate side of the pervaporation membrane group 7 is connected to the vacuum unit 14, and the vacuum unit 14 and the pervaporation membrane group 7 is provided with a second condenser 11, the second condenser 11 is connected to the permeate tank 12, one end of the permeate tank 12 is connected to the third transfer pump 13, the moisture is evaporated from the permeate side of the pervaporation membrane group 7, and is After condensing into liquid in the second condenser 11, it is stored in the permeate tank 12; wherein the intercept side of the pervaporation membrane group 7 is connected to the product tank 9, and a first condenser is provided between the product tank 9 and the pervaporation membrane group 7 8.
  • One end of the product tank 9 is connected to the fourth delivery pump 10.
  • the dehydrated glycerol flows out from the intercept side of the pervaporation membrane group 7, and is condensed into a liquid in the first condenser 8, and then stored in the product tank 9. .
  • a second delivery pump 4 is provided between the buffer tank 3 and the preheater 5, and the second delivery pump 4 transports materials into the preheater 5 and the heater 6 for heating.
  • the working process of the whole machine is as follows: Contains 20%-50% Glycine After the crude alcohol liquid enters the ultrafiltration unit 2 to filter out the TSS suspended impurities, the obtained filtered supernatant is buffered in the buffer tank 3; under the action of the second delivery pump 4, it is delivered to the preheater 5 and the heater 6, and is heated to After a certain temperature, it enters the pervaporation membrane group 7; a certain degree of vacuum is given on the permeate side of the pervaporation membrane group 7, water evaporates from the permeate side, and the material flows out from the retention side, and is condensed to obtain dehydrated and concentrated glycerol.
  • the ultrafiltration unit When it is a gap operation equipment, it can only include the liquid tank 3, the heating device 15, the second transfer pump 4, the pervaporation membrane group 7, the second condenser 11, the permeate tank 12 and the vacuum unit 14. At this time, The ultrafiltration unit is not attached to the concentration equipment, and is operated separately.
  • one side of the material liquid tank 3 is connected to the heating device 15, and one side of the material liquid tank 3 is connected to the pervaporation membrane group 7, wherein the permeation side of the pervaporation membrane group 7 is connected to the vacuum unit 14, and A second condenser 11 is provided between the vacuum unit 14 and the pervaporation membrane group 7, and the second condenser 11 is connected to the permeate tank 12.
  • the moisture is vaporized from the permeate side of the pervaporation membrane group 7, and is in the second After condensing into liquid in the condenser 11, it is stored in the permeate tank 12; the intercept side of the pervaporation membrane group 7 is connected to the material liquid tank 3, and the material liquid transfer pump 4 is arranged between the material liquid tank 3 and the pervaporation membrane group 7 , The glycerol obtained from the concentration of the pervaporation membrane group 7 is sent back to the liquid tank 3.
  • the hollow fiber pervaporation membrane is used in the present invention, and the hollow fiber pervaporation membrane has a high flux and rejection rate, and the flux can reach 5-10 times that of the cross-linked polyvinyl alcohol membrane. 2-5 times of the hollow fiber pervaporation membrane; the filling area of the membrane module composed of the hollow fiber pervaporation membrane is large, and the unit volume can reach more than 5 times of the plate-and-frame membrane module and 20 times of the tubular membrane module.
  • the specific content of the pervaporation membrane is introduced as follows:
  • Step 1 preparing inner layer casting liquid, outer layer casting liquid and core liquid, said inner layer casting liquid, said outer layer casting liquid and said core liquid form a hollow tubular liquid film through a spinneret;
  • Step 2 The hollow tubular liquid film enters the coagulation bath after passing through the air gap to be solidified by phase change, to obtain Hollow fiber membrane yarn;
  • Step 3 Process the hollow fiber membrane filaments to obtain a hollow fiber pervaporation membrane.
  • step S3 you can choose in the step S3:
  • Step S31 Soak the hollow fiber filaments with water, replacement liquid and micropore protection liquid in sequence, and then dry them in the air.
  • the flow rate of the inner layer casting liquid it is preferable to control the flow rate of the inner layer casting liquid to be 0.1-30ml/min, the outer layer casting liquid flow rate is 0.1-30ml/min, the core liquid flow rate is 0. l_30ml/min, core liquid
  • the temperature of the casting liquid is 5-80 degrees Celsius
  • the temperature of the spinneret is 5-80 degrees Celsius
  • the winding wheel speed is 1-50 m/min
  • the temperature of the coagulation bath is 5-80 degrees Celsius.
  • the outer layer casting liquid includes a hydrophilic polymer and a solvent
  • the hydrophilic polymer includes but is not limited to sulfonated polysulfone, sulfonated polyphenylsulfone, sulfonated polyethersulfone, and sulfonated polyamide And sulfonated polyimide, polyvinyl alcohol, polyoxyethylene, cellulose, cellulose acetate, hydrolyzed polyacrylonitrile, polyvinylpyrrolidone, chitosan, polyetheramine and polyethyleneimine; the solvent Including but not limited to n-methyl-2-pyrrolidone, N,N-dimethylacetamide, dimethylformamide, dimethyl sulfoxide, tetrahydrofuran, dichloromethane, chloroform;
  • the inner layer casting liquid includes polymer polymers, solvents and additives, wherein the polymer polymers include but are not limited to polysulfone, polyethersulfone, polyphenylsulfone, polyamide, polyimide, and polyimide Amide-imide, polyvinylidene fluoride, polytetrafluoroethylene, polyacrylonitrile, polypropylene, polycarbonate, polybenzimidazole, polyurethane; the solvent includes but is not limited to n-methyl-2-pyrrolidone , N,N-dimethylacetamide, dimethylformamide, dimethylsulfoxide, tetrahydrofuran, dichloromethane, chloroform; and the auxiliary agent includes but not limited to polyethylene glycol, ethylene glycol , Glycerol, polyvinylpyrrolidone, water, ethanol, acetone, chlorinated Lithium, lithium bromide, calcium chloride;
  • the core liquid includes solvents, non-solvents and auxiliary agents
  • the auxiliary agents include but are not limited to polyethylene glycol, ethylene glycol, glycerol, polyvinylpyrrolidone, ethanol, acetone, n-butanol, among them
  • the solvent includes but is not limited to n-methyl-2-pyrrolidone, N,N-dimethylacetamide, dimethylformamide, dimethylsulfoxide, tetrahydrofuran, dichloromethane, chloroform, the non- The solvent is water.
  • the structure is as follows:
  • the traditional hollow fiber pervaporation membrane sequentially forms a traditional inner support layer, a traditional transition support layer, and a traditional selective separation layer from the inside to the outside, that is, the traditional selective separation layer is located at this time
  • the outermost layer of the traditional hollow fiber pervaporation membrane is prone to problems such as swelling, chemical decomposition, and physical destruction of the separation layer in practical applications, thereby destroying the membrane structural integrity of the pervaporation membrane and reducing the separation efficiency.
  • the hollow fiber pervaporation membrane provided by the present invention sequentially forms an inner support layer, a selective separation layer, and an outer protective layer from the inside to the outside, that is, the selective separation layer is located in the outer protective layer at this time.
  • the outer protective layer has good hydrophilicity and avoids problems such as chemical and physical damage.
  • the hollow structure of the hollow fiber pervaporation membrane provided by the present invention is achieved by controlling the formula of the inner layer casting liquid and the outer layer casting liquid. If the compatibility of the inner and outer layers is good, the middle selective separation layer is formed No, if the compatibility of the inner and outer layers is too poor, delamination and peeling of the inner and outer layers will occur, and the separation effect and stability will be poor.
  • the specific selection series of formulas are as follows:
  • Inner layer casting liquid formula a mixture of polyphenylene sulfone, ethylene glycol and n_methyl-2-P pyrrolidone, wherein the mass ratio of the polyphenylsulfone is 10-30%, and the ethylene glycol
  • the mass ratio of the n-methyl-2-pyrrolidone is between 2-20%, the mass ratio of the n-methyl-2-pyrrolidone is 50-88%, and the combined ratio of the three formulas is 100%;
  • the core liquid formula n-methyl- 2-pyrroli
  • the second set of formulas The outer layer casting liquid: a mixed liquid of cellulose acetate and n_methyl-2-pyrrolidone, wherein the mass ratio of the cellulose acetate is between 1-15%, The mass ratio of n_methyl-2-pyrrolidone is 85-99%, and the combined ratio of the two formulas is 100%;
  • the inner layer casting liquid polyetherimide, polyethylene glycol and n- A mixture of methyl-2-pyrrolidone, wherein the mass ratio of the polyphenylsulfone is 10-30%, the mass ratio of the polyethylene glycol is between 1-10%, and the n-methyl-2 -The mass ratio of pyrrolidone is 60-89%, and the combined ratio of the three formulas is 100%;
  • the core liquid n-methyl-2-pyrrolidone, water and polyethylene glycol, wherein the n-methyl The mass ratio of -2-pyrrolidone is 50-99%, the mass ratio of the water is 1-40%, the mass ratio of the poly
  • Outer layer casting liquid formula a mixture of cellulose acetate acetate and n-methyl-2-pyrrolidone, wherein the mass ratio of the cellulose acetate acetate is between 1-15%, The mass ratio of the n-methyl-2-pyrrolidone is 85-99%, and the combined ratio of the two formulas is 100%;
  • the inner layer casting liquid formula polyetherimide, ethanol and n-methyl- 2-pyrrolidone mixture, wherein the mass ratio of the polyphenylsulfone is 10-30%, the mass ratio of the ethanol is between 1-10%, and the mass ratio of the n-methyl-2-pyrrolidone is 60-89%, the combined ratio of the three formulas is 100%;
  • Core liquid formula n-methyl-2-pyrrolidone, water and polyethylene glycol, wherein the mass ratio of n-methyl-2-pyrrolidone is 50-99%, and the mass ratio of water is 1-40 %, the mass ratio of the polyethylene glycol is 0-10%, and
  • the original hollow fiber pervaporation membrane is adopted.
  • the hollow fiber pervaporation membrane has a high flux and rejection rate.
  • the flux can reach 5-10 times that of cross-linked polyvinyl alcohol membranes and 2-5 times that of inorganic membranes.
  • the processing capacity of the hollow fiber pervaporation membrane is greatly improved, and the separation efficiency is high.
  • the hollow fiber pervaporation membrane has strong tolerance to pH, conductivity and water content, and can directly dehydrate and concentrate crude glycerol with a water content of more than 50-90%.
  • the glycerol concentration equipment provided includes a combination of pervaporation membrane units, heating devices, condensers and other equipment.
  • the equipment investment is small, and it saves space.
  • the corresponding process is simple and practical, and has good practicability.
  • the glycerin product concentrated by this new process is stable. Glycerol is dehydrated and concentrated at a temperature lower than 100 degrees Celsius, without producing malonaldehyde and polyglycerol, without by-products, and with high product recovery rate and minimal impact on the environment.
  • Figure i is an equipment schematic diagram of a glycerin concentration equipment based on a hollow fiber pervaporation membrane according to an embodiment of the present invention.
  • Figure 2 is a glycerol concentration device based on a hollow fiber pervaporation membrane according to another embodiment of the present invention Schematic diagram of the prepared equipment.
  • Fig. 3 is a surface morphology diagram of an ultrafiltration membrane according to an embodiment of the present invention.
  • FIGS 4 and 5 are schematic diagrams of the structure of an ultrafiltration membrane according to another embodiment of the present invention.
  • Figures 6 and 7 are schematic diagrams of the hollow fiber pervaporation membrane structure according to an embodiment of the present invention.
  • Figure 8 shows the experimental results of Example 3 according to the present invention.
  • the term “a” should be understood as “at least one” or “one or more”, that is, in one embodiment, the number of an element may be one, and in another embodiment, the number of the element The number can be multiple, and the term “one” cannot be understood as a restriction on the number.
  • the crude glycerol liquid is transported to the ultrafiltration unit 2 by the first delivery pump 1 for filtration.
  • the ultrafiltration membrane is an inorganic ceramic membrane with a pore size of 0.05-0. 1 micron and an operating pressure of 0.1-0. 2bar, Get a clean water content of 80% Liquid, turbidity is less than 10NTU, stored in buffer tank 3. At this time, the recovery rate of the ultrafiltration unit 2 is 97-99%.
  • the glycerol clear liquid in the buffer tank 3 is heated to 90 °C through the preheater 5 and the heater 6, and is transported to the pervaporation membrane group 7 for dehydration and concentration.
  • the concentrated product is stored in the product tank 9, and is transported to the use site by the fourth transfer pump 10, and the final product purity is 95 wt%, and the yield is 99%.
  • the vacuum degree of the vacuum pump 14 is set to 20 mbar, and the temperature of the condenser 11 is controlled to be less than 5 ° C.
  • the crude glycerol liquid is transported to the ultrafiltration unit 2 by the first delivery pump 1 for filtration.
  • the ultrafiltration membrane is an organic hollow fiber membrane with a pore size of 0.01-0. 1 micron, an operating pressure of 1 bar, and a water content of 70% of the clear liquid, with a turbidity of less than 10NTU, is stored in buffer tank 3.
  • the recovery ultrafiltration unit 2 is 95% o
  • the glycerol clear liquid in the buffer tank 3 is heated to 80°C by the preheater 5 and heater 6, and is transported to the pervaporation membrane group 7 for dehydration and concentration.
  • the concentrated product is stored in the product tank 9 and transported to the use site by the fourth transfer pump 10.
  • the final product purity is 92 wt%, and the recovery rate is greater than 99%.
  • the vacuum degree of the vacuum pump 14 is set to 15-20 mbar, and the temperature of the condenser 11 is controlled to be less than 5 ° C.
  • Self-prepared 15 kg of glycerol and aqueous solution at this time, the configured glycerol aqueous solution does not have a water content of about 80 wt%.
  • This is an intermittent operation process, as shown in the schematic diagram of the equipment in Figure 2.
  • the clear liquid obtained after filtering the glycerin waste liquid is placed in the material liquid tank 3, the heating device 15 is turned on, and the temperature of the material liquid is increased to 90°C.
  • the final product has a purity of 92.5 wt% and a yield of about 99%.
  • the present invention is not limited to the above-mentioned best embodiment. Under the enlightenment of the present invention, anyone can derive other products in various forms, but regardless of any changes in its shape or structure, any products that are the same as or similar to the present application Approximate technical solutions fall within the protection scope of the present invention.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un procédé et un dispositif de concentration de glycérol faisant appel à une membrane fibre creuse de pervaporation. Le procédé utilise une membrane fibre creuse de pervaporation pour effectuer une déshydratation et une concentration sur du glycérol brut, la membrane fibre creuse de pervaporation possédant une perméabilité élevée à l'eau, et le flux pouvant atteindre 5-10 fois celui d'une membrane d'alcool polyvinylique réticulé et 2 à 5 fois celui d'une membrane inorganique. La membrane fibre creuse de pervaporation n'a pas d'exigences concernant la teneur en eau d'une solution d'alimentation et possède une grande plage de tolérance pour le pH et la conductivité. Par conséquent, le présent procédé peut remplacer des procédés de consommation d'énergie classiques tels qu'une distillation à plusieurs étages à pression réduite, et peut être utilisé directement pour effectuer une déshydratation et une concentration sur une solution d'alimentation à teneur élevée en eau, ce qui permet de diminuer significativement la consommation d'énergie de production, de réduire les coûts d'investissement de dispositif et, par conséquent, de réduire les coûts de production de glycérol. Les coûts de fonctionnement peuvent être réduits de plus de 50 % par rapport à ceux des procédés classiques. De plus, la température de concentration du présent procédé est inférieure à 100 °C, ce qui permet d'éviter la décomposition et la polymérisation du glycérol dans une large mesure, de réduire les sous-produits et d'augmenter la qualité du produit.
PCT/CN2020/087360 2019-02-28 2020-04-28 Dispositif et procédé de concentration de glycérol faisant appel à une membrane fibre creuse de pervaporation WO2020173510A2 (fr)

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CN105218316A (zh) * 2014-11-28 2016-01-06 杭州奇纯膜技术有限公司 一种中空纤维渗透汽化膜制备无水乙醇的装置及方法
CN105906476B (zh) * 2016-05-26 2018-08-24 淮南天力生物工程开发有限公司 一种从生物柴油生产废水中提取甘油的方法
CN109809965B (zh) * 2019-02-28 2021-08-20 南京惟新环保装备技术研究院有限公司 基于中空纤维渗透汽化膜的甘油浓缩设备及方法

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