68results about "Azeotropic distillation" patented technology

The invention provides a polymer devolatilization process and a devolatilization system. The devolatilization process comprises the following steps: heating a polymer raw material containing volatile components to obtain a molten polymer, pressurizing the molten polymer, mixing with an entrainer, and feeding into a falling film device; after sudden pressure drop and heating, the entrainer carries volatile components to be separated from the system, and a devolatilization product is obtained; the mass ratio of the polymer raw material to the entrainer is (10: 1)-(10000: 1). According to the polymer devolatilization process provided by the invention, the entrainer with a low boiling point is introduced into a reaction system, a large number of microbubbles are formed through vaporization of the entrainer and azeotropy of volatile components, removal of the volatile components in the material is enhanced through pressure swing flash evaporation, and extremely low pressure does not need to be reached in a devolatilization device.

The invention relates to the technical field of refrigerant raw material preparation, and discloses a novel energy-saving environment-friendly refrigerant raw material preparation system which comprises a raw material preparation and supply unit, a reaction and separation unit and a refining unit which are connected in sequence, the reaction and separation unit comprises a mixer, a reflux device, a reactor, a cooling separation device, a membrane type absorption device and a tail gas tower which are connected in sequence; the refining unit comprises an azeotropic tower, a rectifying tower I and a rectifying tower II which are connected in sequence, and is used for performing dehydration, deacidification and rectifying purification on the separated crude chlorinated liquid to obtain a high-purity carbon tetrachloride product; by optimizing the technological process of the raw material preparation and supply unit, the reaction and separation unit and the refining unit, efficient, environment-friendly and energy-saving production of carbon tetrachloride is realized; the problem that the production raw material carbon tetrachloride of the fourth-generation refrigerant is insufficient is solved, the production cost is reduced, and the production efficiency is improved.

The invention provides novel azeotrope-like compositions and separation processes utilizing the same. An azeotrope-like composition comprising 1,2-difluoroethylene (HFO-1132) and hydrogen fluoride. An azeotrope-like composition comprising 1,1,2-trifluoroethylene (HFO-1123) and hydrogen fluoride. A separation process for a composition comprising at least one member selected from the group consisting of trans-1,2-difluoroethylene (HFO-1132(E)), cis-1,2-difluoroethylene (HFO-1132(Z)), and 1,1,2-trifluoroethylene (HFO-1123) and hydrogen fluoride.

A production system, production method and application of general-purpose high-purity chemicals are disclosed. The production system includes a raw material tank, and an adsorption system, a crystallizer, a first light-impurity removal tower, a first heavy-impurity removal tower, a second light-impurity removal tower, a motorized tower, a second heavy-impurity removal tower, a vapor permeation device, a membrane separation system and a filling system connected with the raw material tank in sequence. The high-purity chemicals produced by the above system have high purity and excellent quality. Compared with the prior art, the system and method designed by the present disclosure have more pertinence, integrity, progressiveness, energy-saving, precision, high safety coefficient and great industrial promotion value. And the products produced are of excellent quality, which can meet the standards applied to the manufacturing of integrated circuit electronic components and meet the high-end needs of the semiconductor industry market.

The utility model provides an azeotropic-phenomenon-based rectifying tower high-efficiency dewatering device which comprises an azeotropic rectifying tower, a liquid inlet pipe is fixedly communicated with the upper position of the surface of the azeotropic rectifying tower, a gas inlet pipe is fixedly communicated with the lower position of the surface of the azeotropic rectifying tower, and the azeotropic-phenomenon-based rectifying tower high-efficiency dewatering device is arranged in the azeotropic rectifying tower and is used for full contact of gas and liquid. Raw materials are guided into the material mixing box from the feeding pipe and enter the upper position in the azeotropic rectifying tower through the liquid inlet pipe, entrainer enters the material mixing box through the feeding cover and the feeding opening, the cavity dividing blades rotate along the rotating shaft under the action of the raw materials, the interior of the material mixing box is divided into a plurality of cavities through the cavity dividing blades, and the entrainer enters the azeotropic rectifying tower through the liquid inlet pipe. The added entrainer uniformly falls into each cavity, so that the entrainer is prevented from being accumulated, the mixing effect is improved, and the mixing effect and the water blowing efficiency are further improved under the stirring rods of the cavity dividing blades.

This disclosure provides a method for efficiently purifying difluoromethane (HFC-32).Specifically, the present disclosure provides a method for producing a purified HFC-32, the method including:an extractive distillation step of contacting a composition containing difluoromethane (HFC-32) and a component X with a solvent A to obtain a composition containing a reduced component X from the composition,wherein the component X is at least one selected from the group consisting of pentafluoroethane (HFC-125), 1, 1, 1-trifluoroethane (HFC-143a), and dichlorodifluoromethane (CFC-12), andwherein the solvent A is at least one of an amine and a fluorinated ether.

The invention discloses a separation system and a separation method of a dichloromethane, ethanol and methanol aqueous solution multi-element azeotropic system. The separation system comprises three stages of rectifying towers connected in series; a reflux pipeline with a condenser is connected to a tower top extraction port of each stage of rectifying tower, and the reflux pipeline corresponding to the first stage of rectifying tower is also connected with a mixer for mixing tower top extraction substances of the first stage of rectifying tower with water and a phase splitter for separating oil and water in the mixer; a water phase outlet of the phase splitter and a tower kettle extraction opening of the first-stage rectifying tower are respectively connected with a feeding opening of the second-stage rectifying tower; a methanol extraction opening is formed in the side line of the second-stage rectifying tower; a tower kettle extraction opening of the second-stage rectifying tower is connected with a feeding opening of the third-stage rectifying tower; and a device for separating ethanol and water is connected to a tower top extraction port of the third-stage rectifying tower. The method provided by the invention can effectively separate the dichloromethane, ethanol and methanol aqueous solution multi-element azeotropic system, and the obtained dichloromethane, ethanol and methanol products have high purity.

The invention relates to a method and installation for recycling a mixture comprising at least one fluorinated fluid, the mixture comprising one or more fluorinated chemical components and one or more contaminants selected from one or more hydrocarbons and / or one or more fluorinated contaminants, including a double membrane filtration step to reduce the contaminant content of the mixture. Figure for the abstract: Figure 1

The utility model provides a kind of for perchloromethylmercaptan purification azeotropic distillation device, belong to captan production technical field, including: distillation kettle and azeotropic rectification tower;The feed inlet of distillation kettle is connected with perchloromethylmercaptan storage tank, and the distillation outlet of distillation kettle upper portion is connected with carbon tetrachloride storage tank by vacuum pump, and the discharge port of distillation kettle bottom is connected with the feed inlet of azeotropic rectification tower by feed pump;The feed inlet of azeotropic rectification tower is also connected with dichloroethane storage tank;The bottom discharge port of azeotropic rectification tower is connected with captan synthesis kettle, and the top discharge port of azeotropic rectification tower is connected with azeotrope storage tank.This device can significantly reduce carbon tetrachloride content, process and simple operation, and the azeotrope used can be reused, and the carbon tetrachloride content in perchloromethylmercaptan after purification is reduced to below 100ppm, which can be directly sent into captan synthesis kettle to participate in synthesis reaction, so that it meets export standard.

This invention discloses a separation system for ethanol and acetal, comprising an acetal separation tower. The acetal separation tower has a raw material inlet and an azeotropic agent inlet on its wall. The raw material inlet is located in the middle of the tower wall, and the azeotropic agent inlet is positioned lower than the raw material inlet. An azeotropic agent recovery tower is connected to the top of the acetal separation tower, and both the acetal separation tower and the azeotropic agent recovery tower have outlets at their bottoms. This invention also discloses a method for separating ethanol and acetal using the aforementioned separation system. This invention uses acetonitrile as an azeotropic agent, obtaining high-purity acetal through one-step azeotropic distillation, and then separating the acetonitrile and ethanol through pressure swing distillation.

An object of the present invention is to provide a novel azeoropic or azeotrope-like composition that is effective for the separation of HF from 1,1,2-trichloroethane (HCC-140), trans-1,2-dichloroethylene (HCO-1130(E)), or cis-1,2-dichloroethylene (HCO-1130(Z)). The object can be achieved by an azeotropic or azeotrope-like composition comprising HCC-140, HCO-1130(E), or HCO-1130(Z), and hydrogen fluoride.

According to the method for recovering the PGME and the PGIE from the HPPO process wastewater, the HPPO process wastewater is concentrated through the membrane separation device, the content of the PGME and the PGIE in the wastewater is greatly increased, and compared with the prior art, the energy consumption can be greatly reduced, the recovery efficiency can be improved, and the recovery cost can be reduced; 2-pentanone or 3-pentanone and a mixture of 2-pentanone and 3-pentanone are used as an azeotropic solvent to replace benzene, and the solvent circulation amount in the dehydration process can be reduced by 50% under the same pressure, so that the dehydration energy consumption is remarkably reduced, and the green and environment-friendly process requirements are met; the water layer of the dehydrated fraction is recycled into the HPPO process wastewater and then is subjected to membrane separation, so that the loss of trace PGME entrained in the dehydrated fraction can be avoided, and the yield of the PGME is increased; according to the technical scheme, the recovery rates of the PGME and the PGIE can reach 99%.

The utility model belongs to the technical field of separation, and particularly relates to an ethyl acetate and butanone separation device, which comprises a butanone separation tower, an ethanol separation tower and an ethyl acetate separation tower which are connected in sequence, in the utility model, the tower top produced liquid of the ethyl acetate separation tower returns to the butanone separation tower, so that the purity of the product can be further improved; the gas phase of the butanone separating tower is used as a heat source of a reboiler at the bottom of the ethyl acetate separating tower, the gas phase at the top of the ethyl acetate separating tower is used as a heat source of a reboiler at the bottom of the ethanol separating tower, heat coupling can be realized between the rectifying towers with different operating pressures, the energy consumption in the rectifying and separating process is further reduced, and the method has higher operability.

The invention relates to the technical field of chemical engineering, and particularly discloses an anhydrous organic peroxy acid production system and method.The anhydrous organic peroxy acid production system comprises a peroxidation reaction distiller, a first oil-water separator, an azeotropic distillation tower and a second oil-water separation and light component removal tower, and moisture is brought out of a reaction system through two times of azeotropy and two times of oil-water separation; and the solvent and the entrainer are respectively recovered through the azeotropic distillation tower and the light component removal tower, and the recovered materials can be recycled. According to the present invention, with the method, the hydrogen peroxide conversion rate and the organic peroxy acid selectivity are high, the prepared anhydrous organic peroxy acid has characteristics of excellent quality and water content of less than 0.01%, and the process has advantages of short reaction time, high raw material utilization rate, high heat energy utilization rate and good economy.

The present disclosure relates to a method and a system for continuous regeneration of high-proof ethanol in a dry mill ethanol plant by a dual-rectification process that uses waste heat from the vacuum system, including routing azeotrope vapor comprising ethanol and water from the first rectifier to a molecular sieve vessel to produce pure, dry ethanol and routing the resulting regenerant to a second rectifier to produce a high-proof condensate that can be directly injected back into the MS vessel for an additional dehydration. The present invention also allows for simultaneous direct injection of azeotrope vapor from the first rectifier to the second rectifier to produce additional condensates that can be directly injected into the second rectifier for a continuous and cyclical feed-and-regeneration cycle for the production of pure, high-proof dry ethanol.

A process apparatus for a distillation process comprises a distillation column (100) that processes material (104) of a mixture of water, at least acetic acid and formic acid and furfural, furfural being used as a former of azeotrope and an extractant in the mixture. A flowing material channel (102) is located between a lower section (106) of the column (100) and an upper section (108) of the column (100), the flowing material channel (102) comprising a solid material remover (110). A feed arrangement (112) is connected with the flowing material channel (102) between the lower section of the column (100) and the solid material remover (110). The flowing material channel (102) receives a stream of the processed material (104) from the lower section (106) of the column (100), a stream of precipitant from the feed arrangement (112), precipitation effect of the precipitant being based on water, and directs the mixture of the streams of precipitant and processed material (104) to the solid material remover (110), which removes solid material caused by the precipitant from the mixture. The flowing material channel (102) feeds a stream of the mixture, from which the solid material has been at least partly removed, to the upper section (108) of the column (100).

A method of purifying ethylenediamine includes the steps as follows. A phenyl compound is added into an ethylenediamine mixture solution, so as to obtain a mixture to be distilled, wherein the ethylenediamine mixture solution includes at least one of a first organic amine compound with a boiling point higher than ethylenediamine and a second organic amine compound with a boiling point lower than ethylenediamine, and the phenyl compound, ethylenediamine and water form an azeotrope. The mixture to be distilled is distilled under a distillation pressure, so as to obtain a low boiling point mixture, wherein the distillation pressure equals to or is smaller than a normal pressure. The low boiling point mixture is phase-separated and water is removed, so as to obtain a purified ethylenediamine product. A purity of the purified ethylenediamine product is larger than 99.5%.

The invention belongs to the technical field of chemical synthesis processes, and particularly relates to a continuous batching method for preparing polyphenylene sulfide, and the method comprises the specific steps of reactive monomer batching, azeotropic agent mixing, azeotropic distillation, azeotropic agent recovery and product delivery. The method has the advantages that the method is simple in process, high in production efficiency, stable in dehydration product quality and simple in process control, and a binary azeotropic system is formed by the aid of the method and a water phase, so that process energy consumption and NMP (N-methyl pyrrolidone) loss are reduced, batches have good uniformity, and continuous burdening is realized. The method has the advantages of simple procedures, high production efficiency, stable dehydration product quality and simplicity in process control.

Impurities such as sulfur dioxide (SO2) are removed from trifluoroacetyl chloride (TFAC) through distillation, adsorption, or a combination thereof, and / or including the formation of an azeotrope or azeotrope-like composition including effective amounts of sulfur dioxide (SO2) and trifluoroacetyl chloride (TFAC). The trifluoroacetyl chloride (TFAC) thus purified may then be used in the manufacture of trifluoroiodomethane (CF3I). Also disclosed are azeotropes and azeotrope like compositions of sulfur dioxide (SO2) and trifluoroacetyl chloride (TFAC).

This disclosure provides a method for efficiently purifying difluoromethane (HFC-32). Specifically, the present disclosure provides a method for producing a purified HFC-32, the method including: an extractive distillation step of contacting a composition containing difluoromethane (HFC-32) and a component X with a solvent A to obtain a composition containing a reduced component X from the composition, wherein the component X is at least one selected from the group consisting of pentafluoroethane (HFC-125), 1,1,1-trifluoroethane (HFC-143a), and dichlorodifluoromethane (CFC-12), and wherein the solvent A is at least one of an amine and a fluorinated ether.

To provide compositions and methods that may be used to prepare iodide-containing compounds, such as trifluoroiodomethane, of high purity.SOLUTION: Provided is a composition comprising an azeotropic or azeotrope-like composition, comprising 0.5 wt.% to 35.5 wt.% of trifluoroacetyl chloride (CF3COCl) and 64.5 wt.% to 99.5 wt.% of trifluoroiodomethane (CF3I).SELECTED DRAWING: Figure 1

The present invention provides a composition containing 1, 1, 1, 3, 3, 3-hexafluoroisopropyl methyl ether and water, a dehydrating agent containing the composition, and a dehydration method of a compound to be treated, the dehydration method comprising distilling off the 1, 1, 1, 3, 3, 3-hexafluoroisopropyl methyl ether from a composition containing the compound to be treated, 1, 1, 3, 3, 3-hexafluoroisopropyl methyl ether, and water. And a step for adding 1, 1, 1, 3, 3, 3, 3-hexafluoroisopropyl methyl ether and the water.

This invention relates to the field of purification equipment technology, and more particularly to a purification equipment and control method for crude α-pyrrolidone. The technical solution includes a tower body, multiple trays fixedly installed inside the tower body, and a liquid storage plate fixedly installed inside the tower body and above the trays. The liquid storage plate stores liquid. Multiple air holes are provided on the trays. Floating valves, corresponding to the air holes and rising and falling according to the air pressure, are installed on the trays. Drainage holes, corresponding to the air holes and coaxially arranged, are provided on the liquid storage plate. A variable valve mechanism is fixedly installed on the drainage holes. This invention, through intelligent linkage between the float valve lift and the drainage hole diameter, allows for real-time liquid replenishment under high-speed gas impact, completely eliminating dry zones on the trays, ensuring uniform gas-liquid contact, improving mass transfer efficiency, and featuring a design that adjusts the drainage flow rate to avoid flooding caused by excessive liquid replenishment. This expands operational flexibility and is particularly suitable for the thermosensitive characteristics of α-pyrrolidone.

This invention discloses a differential pressure coupled distillation apparatus for methanol production, comprising a frame and a reaction tank mounted on the frame. The reaction tank is connected to a cooling tank via a pipe to a cold liquid inlet. The cooling tank's cold liquid outlet is connected to a dimethyl carbonate distillation column via a pipe. The dimethyl carbonate distillation column is connected to a dimethyl carbonate refining column via a pipe. The dimethyl carbonate distillation column is connected to the cooling inlet of the cooling tank via a pipe. The cooling outlet of the cooling tank is connected to a low-pressure distillation column via a pipe. The low-pressure distillation column is connected to the dimethyl carbonate distillation column via a pipe. The low-pressure distillation column is connected to a low-pressure thermal circulation box and a high-pressure heating box via pipes. The top of the low-pressure thermal circulation box is connected to the low-pressure distillation column via a pipe. The high-pressure heating box is connected to the high-pressure distillation column via a pipe. The high-pressure distillation column is connected to the top pipe of the low-pressure thermal circulation box via a pipe. During the entire cycle, phenol, methanol, and dimethyl carbonate undergo multiple distillations.

In the presence of alcoholic solvents, 1 -C(O)-NH-NH-C(O)-R 2 R 3 -CH2-CH2-O-CH2-CH2-R 4 a compound of formula (I) comprising reacting with: A method for preparing JPEG2025515318000016.jpg48160, comprising the steps of: 1 and R 2 are independently selected from linear or branched alkyl groups or are joined to form a 4-, 5-, or 6-membered heterocycle; R 3 and R 4 is independently selected from a halide or a sulfate.

The application discloses a kind of multistage series reaction and constant boiling rectification water removal coupling 2,5-furan dicarboxylic acid continuous preparation device and method.The continuous preparation device is by 2-6 gap reaction kettle of coupling constant boiling rectification water removal series connection composition.The steps of the method are as follows:1) single gap reaction kettle stable operation;2) multistage series reaction kettle stable continuous operation;3) continuously adding hexahydroxydicarboxylic acid and / or hexahydroxydicarboxylic acid salt to the first stage gap reaction kettle, reaction at 100~140 ℃;4) the reaction product from the last stage gap reaction kettle is obtained after cooling, crystallization, recrystallization 2,5-furan dicarboxylic acid product.The application realizes 2,5-furan dicarboxylic acid continuous production, substrate concentration can be increased to 30%, reaction selectivity is good, space-time yield is high, product uniformity is good, suitable for large-scale industrial application, with good industrial application prospect.

The invention discloses a preparation method of a hydroxylamine aqueous solution applicable to the field of semiconductors, which comprises the following steps: (1) adding an inorganic alkali aqueous solution into a hydroxylamine salt aqueous solution until the pH value of the hydroxylamine salt aqueous solution reaches 9-11 to obtain a hydroxylamine aqueous solution crude product; (2) adding an organic solvent into the hydroxylamine aqueous solution crude product, so that the solubility of a salt-containing component is changed, further crystallizing and separating out, and carrying out solid-liquid separation to remove a salt-containing solid, so as to obtain a desalted hydroxylamine solution; (3) carrying out reduced pressure distillation on the desalted hydroxylamine solution to remove the organic solvent, and increasing the concentration of hydroxylamine by azeotropy of the organic solvent and water to obtain a hydroxylamine aqueous solution without the organic solvent; and (4) purifying the hydroxylamine aqueous solution from which the organic solvent is removed through ion exchange resin, and removing trace metal ion impurities and anion impurities in the solution to obtain the hydroxylamine aqueous solution applicable to the semiconductor field.

A heteroazeotropic extractive distillation method is performed using two-stage heteroazeotropic extractive distillation within at least one distillation column (100, 102). A first stage (10) comprising distilling a first mixture (104) of water, at least acetic acid and formic acid and entrainer inside a temperature range difference 5°C to 20°C for separating water from the first mixture (104), which has a first percentage of said entrainer and a first percentage of water. A second stage (12) receives a bottom product of water, at least acetic acid and formic acid and said entrainer from a bottom section (108) of the first stage (10). The second stage (12) has a second percentage of said entrainer and a second percentage of water, wherein the second percentage of said entrainer being greater than the first percentage of said entrainer, and / or the first percentage of water being greater than the second percentage of water. At least a part of overhead vapor of at least one of the first stage (10) and the second stage (12) is pressurized by vapor recompression. At least a part of the first mixture (104) is circulated back to the first stage (10), and heat of the overhead vapor to first mixture (104) is circulated to the first stage (10).

The utility model provides a kind of azeotrope rectification system, comprising: first rectifying tower, with the preheater of liquid inlet being connected to the middle part of first rectifying tower, with the heat exchanger of exhaust port being connected to the top end of first rectifying tower, with the first condenser of one end of heat exchanger intercommunication, with the first layered tank of first condenser outlet end intercommunication, with the reflux liquid inlet of first layered tank one end connection being located in the upper portion lateral wall of first rectifying tower, with the first reboiler of first rectifying tower bottom circulation intercommunication;Through above-mentioned scheme, preheater is preheated to the material entering rectifying tower, preheated material enters tower after can faster reach suitable rectification temperature, speed up the progress of rectification process, while the addition of reflux liquid can adjust the gas-liquid equilibrium in tower, increase the mass transfer driving force in tower, further optimize rectification process, improve rectification efficiency, help more efficiently realize the separation of azeotrope.

The application relates to the field of wastewater treatment processes, in particular to a nitrile-containing wastewater treatment process and application thereof. The nitrile-containing wastewater treatment process comprises the following steps: (1) azeotropic distillation of the nitrile-containing wastewater; (2) hydrolysis treatment of the nitrile-containing wastewater in a pressure kettle. The nitrile-containing wastewater treatment process provided in the application can solve the problems in the existing nitrile-containing wastewater treatment process, the cost is lower than that of the oxidation method and the electrolysis method, the problem that the biological method is not suitable for industrialization is avoided, the operation is simple, and the process has excellent market prospect.