50 results about "Osmolyte" patented technology

A water treatment plant or system for the production of permeate includes a reverse osmosis stage and a permeate stage. The reverse osmosis stage can include a piping system having a supply line for process input water, a reverse osmosis pump, and a reverse osmosis tank. The reverse osmosis tank has an inlet for process input water coming from the reverse osmosis pump, a membrane, and an outlet for permeate. The permeate stage, which can have a line system forming a circuit, can include a permeate tank, a permeate pump, and a tapping point for connecting at least one consumer or user of permeate. The reverse osmosis stage and the permeate stage can be connected to one another via a connecting line in such a way that the reverse osmosis stage feeds the permeate stage with permeate. The circuit of the permeate stage can include a sterile filter.

The application provides an assisted permeation roll type membrane assembly. Compared with the prior art, the assisted permeation roll type membrane assembly provided by the application can realize high concentration of raw liquid under low operating pressure; in addition, the membrane assembly can also be used in a forward osmosis membrane separation process. By introducing an assisted permeation liquid on the permeation liquid side of the RO or NF membrane in the assembly, the osmotic pressure on both sides of the membrane can be reduced, and then the pressure applied on the raw liquid side can be reduced, and the pressure can be regulated by adjusting the components of the assisted permeation liquid, so as to reduce the pressure and cost of solution concentration and improve the concentration ratio. The assisted permeation roll type membrane assembly provided by the application can be applied to industrial wastewater zero discharge, seawater desalination, material separation and other industrial fields, and can also be used as a forward osmosis, diffusion dialysis, gas separation, organic solvent nanofiltration and organic solvent reverse osmosis and other membrane separation processes in addition to reverse osmosis and nanofiltration.

The application discloses a phosphorus recovery method and system in phosphogypsum leachate, and relates to the technical field of environmental protection. The phosphorus recovery method comprises the following steps: adding calcium oxide into the phosphogypsum leachate, adjusting the pH value to 4, removing filter residues, removing COD through sand filtration and ultrafiltration; adjusting the pH value of the ultrafiltrate to 4, producing water through first nanofiltration, adjusting the pH value of the permeate to 10, collecting reaction generated gas into a second sedimentation tank for dissolution, continuously producing water through second nanofiltration, and obtaining concentrated water as phosphorus recovery liquid; collecting the first nanofiltration concentrated water and the second nanofiltration permeate, adding phosphate into the second sedimentation tank to obtain magnesium ammonium phosphate precipitation, and performing reverse osmosis treatment on the filtrate. The phosphorus recovery method provided by the application is simple in operation, low in cost, and can make the phosphorus recovery rate reach more than 90%, has a high removal rate of impurities such as F and S, and the obtained products in the treatment process can be recycled, and have high economic value.

An amine-containing water concentration system comprising an apparatus 1, which comprises an osmotic pressure generator 10, and a carbon dioxide introducing unit 21. The osmotic pressure generator inc

The present technology comprises stable aqueous pharmaceutical compositions and formulation comprising non-naturally occurring melanocortin analogs. In some embodiments, the non-naturally occurring melanocortin analogs may be agonists or antagonists of the melanocortin 5 receptor (MC5R) with sub-micromolar or low-nanomolar binding activity. In some embodiments, the present technology comprises a pharmaceutical composition having a pH of about 4.0 to about 6.5, comprising a non-naturally occurring melanocortin analog having at least one cationic amino acid residue, an osmolyte, a pH adjusting agent, and a buffer.

This pure water production apparatus comprises a reverse osmosis membrane and an electrodeionization device 2. In the electrodeionization device 2, anion exchange membranes 11 and cation exchange membranes 12 are alternately arranged between an anode plate 15 and a cathode plate 16, and by constituting compartments with the anion exchange membranes 11 and the cation exchange membranes 12, a desalting chamber 13 and a concentration chamber 14 are formed, and an anode chamber and a cathode chamber are formed at respective ends. As feed water to the desalting chamber 13, permeated water W1 from a reverse osmosis membrane device 1 is supplied to the desalting chamber 13 to obtain treated water W2. Further, as feed water W3 to the concentration chamber 14, permeate from the reverse osmosis membrane device 1 is supplied, and concentrated water W4 is discharged. In the electrodeionization device 2, the desalting chamber 13 is filled with substantially 100% by weight of an anion exchange resin. According to this pure water production apparatus, the removal efficiency of weak acid ions such as boron and silica can be improved without using chemicals.

This waste liquid treatment method for selectively recovering boric acid from a waste liquid generated in a polarizing plate manufacturing process comprises a first membrane separation step for passing the waste liquid having a pH of 8.5 or less or the waste liquid pH-adjusted to a pH of 8.5 or less through a first separation membrane module provided with a reverse osmosis membrane to separate the waste liquid into a first permeate including boric acid (B1) and a substance (R1) other than boric acid in the waste liquid and a first concentrated liquid including the boric acid (B2) and a substance (R2) other than boric acid in the waste liquid, and a boric acid concentration crystallization step for recovering boric acid by concentration crystallization of the first permeate obtained by the first membrane separation step.

The present invention provides a water treatment device that can efficiently concentrate and discharge difficult-to-remove substances from the system without degrading the water quality of the permeate from the first reverse osmosis membrane. [Solution] The water treatment device 1 includes a water treatment tank 2 for storing water to be treated W, a high-pressure pump 3 for supplying the pre-treated water W, a first reverse osmosis membrane 4, a concentrated water tank 5 for storing the concentrated water W1 from the first reverse osmosis membrane 4, a high-pressure pump 6, and a second reverse osmosis membrane 7 for treating the concentrated water W1 from the first reverse osmosis membrane 4. The permeate water W2 from the second reverse osmosis membrane 7 is returned to the water treatment tank 2, and the concentrated water from the second reverse osmosis membrane 7 is discharged. The first reverse osmosis membrane 4 and the second reverse osmosis membrane 7 are reverse osmosis membranes having a permeate flow rate of 0.5 m / day or more and 1.0 m / day or less at an effective membrane surface pressure of 2 MPa (water temperature 25°C, pure water), or a permeate flow rate of 0.5 m / day or more and 1.0 m / day or less at an effective membrane surface pressure of 1.5 MPa (water temperature 25°C, pure water).

The utility model provides an RO (Reverse Osmosis) acetic acid recovery system. The RO acetic acid recovery system comprises an RO water inlet buffer tank, a primary reverse osmosis membrane group and a secondary reverse osmosis membrane group, the liquid inlet end of the RO water inlet buffer tank is connected with an RO water inlet pipe; the output end of the buffer tank is sequentially connected with a reverse osmosis low-pressure pump and a reverse osmosis high-pressure pump through a conveying pipeline; the output end of the reverse osmosis high-pressure pump is connected with the primary reverse osmosis membrane group through a pipeline; one end, provided with a double-pipeline output end, of the second-stage reverse osmosis membrane group is connected with a liquid inlet end of the first-stage RO water production tank, and the other end of the second-stage reverse osmosis membrane group is connected with a liquid return opening of the RO water inlet buffer tank; the penetrating fluid conveying pump is connected with the sewage treatment device through an output pipeline; and a conveying pipeline connected with a liquid return port of the secondary RO water production tank is arranged on the output pipeline between the penetrating fluid conveying pump and the sewage treatment device. According to the RO acetic acid recovery system disclosed by the utility model, the recovery rate of acetic acid in water is improved, the consumption of fresh acetic acid is reduced and considerable economic benefits are brought to enterprises by arranging two groups of reverse osmosis membrane group operation loads.

This water treatment system provides optimal blockage suppression treatment that can be performed according to the fouling risk of two or more types of raw water. [Solution] The water treatment system 1 includes a reverse osmosis membrane device 6 that separates mixed water, obtained by mixing multiple raw waters of different water qualities, into permeate and concentrated water; a clogging suppression means 9 that suppresses clogging of the reverse osmosis membrane of the reverse osmosis membrane device; a flow rate measuring means 11 that measures the flow rate of each of the multiple raw waters; and a control device 10 that obtains the flow rate ratio of the multiple raw waters based on the measurement value of the flow rate measuring means 11 and controls the clogging suppression operation of the clogging suppression means 9 in stages according to the flow rate ratio.

A stool resuspension comprising a hemoglobin stabilizing reagent is provided.SOLUTION: In some embodiments, the hemoglobin stabilizing reagent may be an osmolyte, a multivalent cation, a sugar or polysaccharide, and optionally a multivalent cation, a protoporphyrin, or an HRP stabilizing component, and optionally a multivalent cation. Also provided are methods of stabilizing hemoglobin in a stool sample in a solution, and sample collection devices comprising the solution.SELECTED DRAWING: None

A method for treating waste liquid according to the present invention comprises: a boric acid adsorption step for selectively adsorbing boric acid onto an adsorbent from a waste liquid having a pH adjusted to be alkaline; a boric acid desorption step for bringing an acidic solution into contact with the adsorbent to cause the boric acid to elute from the adsorbent into the acidic solution to obtain an eluate; an NF membrane separation step for adding a base to the eluate and passing the eluate that has been pH adjusted further to the acidic side from neutral through a NF membrane to separate the eluate into a permeate containing the boric acid without containing acid-derived anions or base-derived cations, and a concentrate containing acid-derived anions and base-derived cations; and a boric acid recovery step for recovering boric acid from the permeate.

A process and system for producing a hydrogenated drinking water has a reverse osmosis filter, an ionizer and a power supply. The reverse osmosis filter has an inlet on one side thereof and first and second outlets on an opposite side thereof. The first outlet is adapted to pass a permeate from the reverse osmosis filter. The second outlet is adapted to pass brine from the reverse osmosis filter. The ionizer is in fluid communication with the reverse osmosis filter. The ionizer has a first inlet connected to the first outlet of the progress osmosis filter. The ionizer has a second inlet connected to the second outlet of the reverse osmosis filter. The power supply is connected to the ionizer so as to electrolysize the brine and the permeate.

Main requirement: Water treatment plant for the production of permeate, especially for dialysis therapy, comprising • a reverse osmosis stage (137) with a piping system comprising a supply line (131) for process inlet water (100), a reverse osmosis pump (103) and a reverse osmosis tank (130), wherein the reverse osmosis tank (130) has an inlet (143) for the process inlet water (100) coming from the reverse osmosis pump (103), a membrane (104) and an outlet (144) for permeate (108), • a permeate stage (139) with a circulating piping system comprising a permeate tank (112), a permeate pump (114) and a take-off point (134) for connecting at least one consumer or user of permeate (108), wherein the reverse osmosis stage (137) and the permeate stage (139) are connected to each other via a connecting line (138) such that the reverse osmosis stage (137) feeds the permeate stage (139) with permeate (108), and wherein the circuit of the permeate stage (138) comprises a sterile filter (116).

To provide a multistage reverse osmosis membrane treatment system capable of obtaining treated water of high quality while suppressing operation energy.SOLUTION: A multistage reverse osmotic membrane treatment system 1 is equipped with a storage tank 2 for storing W0 to be treated and the water supply pipe 3 connected to the storage tank 2 and a liquid supply pump 4, a first reverse osmotic membrane 5 and a second reverse osmotic membrane 6 are successively provided to the water supply pipe 3. An aqueous NaOH soln. adding means 7 is connected to the front stage of the second reverse osmotic membrane 6 and the addition amt. of an aqueous NaOH soln. can be controlled so that the water to be treated of the second reverse osmotic membrane 6 becomes an alkali region corresponding to the flow amt. of the water passing pipe 3 and the pH of the W0 of the water to be treated. The first reverse-osmosis membrane 5 has a permeation flow rate of 2. 1MPa / (0m3·day) or more per membrane surface effective pressure m2 (water temperature 25 °C., pure water (RO permeate)), and the second reverse-osmosis membrane 6 has a permeation flow rate of 0. 1MPa / (8m3·day) or more and less than 2. m2 / (0m3·day) per membrane surface effective pressure m2 (water temperature 25 °C., pure water (RO permeate)).SELECTED DRAWING: Figure 1

A pharmaceutical formulation presented, comprising an insulin or an insulin analog, and at least one protective excipient, in high concentration, selected from: a protective osmolyte, a surfactant, and a phenolic preservative. In embodiments, the insulin or insulin analog is one or more of: regular human insulin, insulin lispro, insulin aspart, insulin glulisine, insulin glargine, insulin detemir, or insulin degludec. In some embodiments, at least one of: the concentration of the protective osmolyte confers an osmolarity greater than 250 mOsm / L, the concentration of the surfactant is greater than 0.1% w / v, or the concentration of the phenolic preservative is greater than 0.4% w / v. In some embodiments, insulin API is dissolved and incubated for 20 to 40 minutes at high pH before the protective excipients are added.

The present invention relates to methods for ultrafiltration of molecules of interest and to related uses, respectively, which advantageously employ osmolytes. Among others, the invention provides methods and uses for concentrating molecules of interest via ultrafiltration.

The invention relates to a continuous production method and system of terephthalic acid diester. The method comprises the following steps: introducing terephthalic acid and alcohols into a first tubular reactor for primary esterification reaction, and condensing to obtain a reaction mixture; carrying out reverse osmosis treatment on the reaction mixture through a membrane module to respectively obtain a concentrated solution and a penetrating fluid containing water and alcohols; carrying out pervaporation separation treatment on the penetrating fluid to respectively obtain alcohols and water; and introducing the obtained alcohol and the concentrated solution into a second tubular reactor for secondary esterification reaction to obtain the terephthalic acid diester. According to the method, the tubular reactor is combined with the reverse osmosis membrane and the vaporizing osmosis membrane, so that the mass and heat transfer effects are enhanced, the use of a catalyst is avoided, the reaction time is shortened, and the generation of byproducts is reduced; meanwhile, by separating water and breaking reversible reaction balance, the reaction can be continuously and positively carried out, the yield of the target product terephthalic acid diester is increased, the technological process is simple, and the method is suitable for industrial production.

Compositions and methods for synthesizing an RNA product are provided herein. For example, the present disclosure provides a method of producing an RNA product comprising incubating an in vitro transcription mixture, thereby producing an RNA product that comprises a plurality of single-stranded RNA molecules. In some embodiments, an in vitro transcription mixture comprises a DNA template comprising an RNA polymerase promoter sequence operatively linked to a target sequence; at least one RNA polymerase that recognizes the RNA polymerase promoter sequence; a plurality of ribonucleotides comprising at least two different types of ribonucleotides, each type comprising a different nucleoside; and a transcription buffer comprising an osmolyte.

The invention relates to the technical field of epsilon-CL-20 crystal material preparation, in particular to a spherical epsilon-CL-20 crystal preparation method and system.The method comprises the steps that CL-20 and methyl lactate are prepared into a saturated solution, circulating concentration is carried out in a crystallizer through a nanofiltration membrane assembly, and meanwhile through control over the transmembrane pressure and the outflow rate of penetrating fluid, the spherical epsilon-CL-20 crystal is obtained; the supersaturation degree of the solution is precisely regulated and controlled, and closed-loop circulation of the solvent is realized through real-time recovery and resaturation of penetrating fluid. The green solvent methyl lactate is adopted, the membrane crystallization technology is combined for operation at normal temperature, and the method has the advantages of low energy consumption, zero solvent emission, controllable crystal morphology, uniform particle size distribution and the like, and is suitable for industrial continuous production of high-purity spherical epsilon-CL-20 crystals.

Main claim: Water treatment plant for the production of permeate, in particular for dialysis therapy, comprising: • a reverse osmosis stage (137) with a piping system comprising a supply line (131) for process inlet water (100), a reverse osmosis pump (103) and a reverse osmosis tank (130), wherein the reverse osmosis tank (130) has an inlet (143) for the process inlet water (100) coming from the reverse osmosis pump (103), a membrane (104) and an outlet (144) for permeate (108), • a permeate stage (139) with a circulating piping system comprising a permeate tank (112), a permeate pump (114) and a discharge point (134) for connecting at least one consumer or user of permeate (108), wherein the reverse osmosis stage (137) and the permeate stage (139) are connected to each other via a connecting line (138) such that the reverse osmosis stage (137) feeds the permeate stage (139) with permeate (108),and wherein the permeate stage circuit (138) includes a sterile filter (116).

The presently disclosed subject matter relates generally to the production of a desalinated, filtrated or other way treated water simultaneously with generation of renewal energy source, in particular hydrogen, using osmotic and / or gauge pressure driven filtration processes and systems. The co-generation of hydrogen from water produced during pressure driven water desalination / filtration processes, such as reverse osmosis, forward osmosis, pressure retarded osmosis or ultrafiltration. A small part of feed, raw saline solution and / or permeate involved in a desalination / filtration processes is subjected to electrolysis thereby splitting the water to produce hydrogen. This is achieved by the provision of novel RO type semi-permeable membranes and UF type membrane that incorporate electrodes within the membrane to allow splitting of the water via electrolysis.

A method for operating a tapered flow pressure driven arrangement containing a plurality of membrane modules, which comprises positioning said membrane modules in at least a first and a second successively arranged flow passes and at least a first and a second successively arranged flow stages in said 1st pass, passing a feed stream through said first flow stage to generate a permeate and a concentrate, directing said concentrate to the said consecutive flow stage and passing said concentrate therethrough, while passing at least part of the combined 1st pass permeate through said second pass, while periodically replacing one or more of the membrane modules belonging to said second flow stage with one or more membrane modules belonging to any flow stage in said consecutive flow pass, wherein the periodicity of said replacement is such that the surface of membranes disposed in said consecutive flow stages of the first pass is exposed to super-saturation conditions associated with the passage of said concentrate for a period of time that is shorter than the time required for said concentrate to precipitate therefrom one or more sparingly soluble salts and / or minerals, onto the surface of the membranes in said consecutive flow stages under said saturation or super-saturation conditions, or before deposit of organic substances can occur in the last of said two or more successively arranged flow stages.

Provided are a pure water production system and a pure water production method where, during pure water production in which a reverse osmosis membrane treatment, an ion-exchange treatment using an ion-exchange resin, and a reverse osmosis membrane treatment are sequentially carried out, the concentration of TOC components in obtained pure water can be reduced while suppressing decreases in the water recovery rate of the entire system. A pure water production system (1) comprises: a first reverse osmosis membrane treatment device (16) that causes raw water to pass through a first reverse osmosis membrane; an ion-exchange treatment device (22) that subjects first reverse osmosis (RO) permeated water to an ion-exchange treatment by using an ion-exchange resin; a second reverse osmosis membrane treatment device (26) that causes the ion-exchange treated water to pass through a second reverse osmosis membrane; and a return means that returns second RO concentrated water to a stage preceding the first reverse osmosis membrane treatment device (16).

This acid / alkali recovery method is a method for separating a liquid to be treated, which is obtained by adding an acidic solution and an alkaline solution to a waste liquid containing boric acid and potassium iodide generated in a polarizing plate production process, into an acidic solution, an alkaline solution, and a mainly-boric acid-based treatment liquid by electrodialysis. The acid / alkali recovery method comprises: an NF membrane separation step for passing a liquid to be treated through an NF membrane to separate the liquid to be treated into a permeated liquid containing iodide ions and a concentrated liquid containing iodide ions at a lower concentration than the permeated liquid; and an electrodialysis step for passing the concentrated liquid through an electrodialysis device to separate the concentrated liquid into a mainly-boric acid-based treatment liquid, an acidic treatment liquid, and an alkaline treatment liquid.

According to the present disclosure, a sewage and wastewater effluent treatment method is provided. The method comprises the steps of: providing sewage and wastewater effluent; using a nanofilter (NF) to separate the sewage and wastewater effluent into NF concentrate and NF permeate; removing organic materials from the NF concentrate; introducing the NF permeate into reverse osmosis so as to separate same into reverse osmosis concentrate and deionized water; removing nitrogen from the reverse osmosis concentrate, the nitrogen removal step being performed by a biological or electrochemical method; and combining the NF concentrate that passed through the organic material removal step and the reverse osmosis concentrate that passed through nitrogen removal step. The method enables environmentally friendly and efficient treatment of sewage and wastewater effluent.

Disclosed herein is a bioreactor comprising a vessel comprising; a first tube for transporting retentate to a retentate receiving tank; a second tube that surrounds the first tube for transporting a permeate to a permeate receiving tank; and a third tube that surrounds the second tube; wherein the third tube is in fluid communication with a sparger; and wherein the third tube transports a fluid that sparges a biological broth disposed in the vessel and wherein a membrane that separates the first tube from the second tube separates the biological broth into the permeate and the retentate.

Compositions, methods, and kits for stable Trypan Blue solutions are provided. In one example, a method includes: cooling a solution of Trypan Blue; and filtering the cooled solution. In another example, a method includes: mixing a water-soluble polymer with a Trypan Blue solution. The method may further include adding one or more ingredients such as an aqueous buffer, an osmolyte, an acid, a base, a buffer, a cell culture medium, water, or combinations thereof.

A process for dealcoholizing a starting liquid (F) containing water and alcohol, in particular ethanol, as well as flavorings and / or nutrients, by means of a first membrane separation unit (1), in particular a diafiltration unit (10), comprising at least one separation membrane (12), wherein the starting liquid (F) is introduced under overpressure into a primary-side chamber (13) of the first membrane separation unit (1), in the secondary-side chamber (14) of which downstream of the at least one separation membrane (12) a lower pressure prevails than in the primary-side chamber (13), wherein water and alcohol pass through the at least one separation membrane (12) into the secondary-side chamber (14) as an alcohol-containing liquid permeate (P1), wherein water or a water-containing liquid is added directly or indirectly as a diluent (V) to a retentate (R1) retained by the at least one separation membrane (12) in the primary-side chamber (13).The system is characterized by the fact that the alcohol-containing liquid permeate (P1) is post-treated in a pervaporation unit (20) of a second membrane separation unit (2), wherein the alcohol-containing liquid permeate (P1) is first introduced into a primary-side chamber (23) of the pervaporation unit (20), where the alcohol evaporates in at least one pervaporation membrane (22) and enters as alcohol-containing gaseous permeate (P2) into a secondary-side chamber (26) of the pervaporation unit (20) downstream of the at least one pervaporation membrane (22), and wherein the water of the alcohol-containing liquid permeate (P1) is retained as retentate (R2) in the primary-side chamber (23) of the pervaporation unit (20) and reused.

Disclosed herein is a bioreactor comprising a vessel comprising; a first tube for transporting retentate to a retentate receiving tank; a second tube that surrounds the first tube for transporting a permeate to a permeate receiving tank; and a third tube that surrounds the second tube; wherein the third tube is in fluid communication with a sparger; and wherein the third tube transports a fluid that sparges a biological broth disposed in the vessel and wherein a membrane that separates the first tube from the second tube separates the biological broth into the permeate and the retentate.