163 results about "Azeotrope" patented technology

The invention discloses a water-based environment-friendly coating and local printing transfer paper thereof, and particularly relates to the technical field of water-based environment-friendly coatings. The water-based environment-friendly coating is prepared from a water-based epoxy ester dispersion, an organic silicon modified polyvinyl butyral emulsion, a gas-phase method aluminum oxide nano dispersion, a fluorocarbon surfactant, a self-crosslinking polyether thickening agent and a propylene glycol methyl ether acetate-water azeotropic quick-drying auxiliary agent. According to the coating, through cooperation of specific components and process control, the drying speed is remarkably increased, the surface drying time is shortened, meanwhile, shrinkage cavities are eliminated, the hardness of the coating is enhanced, and the edge transfer precision is improved. Corona treatment is adopted for the corresponding local printing transfer paper, gravure precise coating, infrared pre-drying and gradient hot air drying are matched, and finally clear separation and transfer of a coating are achieved through infrared laser scanning. The whole system is a water-based formula, is environment-friendly and safe, is suitable for the field of high-end printing, and has the comprehensive advantages of high drying speed, high precision, strong adhesive force, simplified process and the like.

The invention relates to an ethanol upgrading device and method, the device is used for upgrading ethanol containing a small amount of ethyl acetate, the device comprises a low-pressure rectification unit, a pumping unit and a high-pressure rectification unit which are connected in sequence, a variable-pressure rectification principle is adopted, azeotrope composition is changed only through a variable-pressure mode, reasonable process parameters are matched, and the quality of ethanol is improved. The purified ethanol is extracted from the low-pressure rectification unit, and the ethanol with higher ethyl acetate content is extracted from the high-pressure rectification unit, so that a large amount of ethanol is prevented from being evaporated to the high-pressure rectification unit, the energy consumption is obviously reduced, the production cost is reduced, and the economic benefit is improved.

Provided in the present application are a heat-absorbing material and a preparation method therefor, a heat-absorbing part, a battery assembly and an electric device. The heat-absorbing material comprises a carrier, an entrainer and a phase-change component, wherein the phase-change component and the entrainer form a negative azeotrope. The entrainer and the phase-change component in the heat-absorbing material of the present application form a negative azeotrope, such that the phase-change component undergoes phase change when the temperature is lower than the phase-change temperature of the phase-change component, thereby absorbing heat, realizing a heat-absorbing effect, improving the heat-absorbing response speed of the heat-absorbing material, and further improving the usage safety of the battery assembly.

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.

Azeotropic or azeotrope-like compositions, particularly azeotropic or azeotrope-like compositions consisting essentially of or consisting of (Z)-1-chloro-2,3,3-trifluoroprop-1-ene (HCFO-1233yd(Z)), ethanol, and each of methanol, as well as azeotropic or azeotrope-like compositions consisting essentially of or consisting of (Z)-1-chloro-2,3,3-trifluoroprop-1-ene (HCFO-1233yd(Z)), ethanol, and 1,2-trans-dichloroethylene (trans-DCE), and azeotropic or azeotrope-like compositions consisting essentially of or consisting of (Z)-1-chloro-2,3,3-trifluoroprop-1-ene (HCFO-1233yd(Z)), methanol, and 1,2-trans-dichloroethylene (trans-DCE), and solvent uses of the aforementioned compositions.

The disclosed method for recovering N-methyl pyrrolidone from complex waste liquid includes the following processes: pumping the NMP-containing waste liquid into a rectification one-effect tower after vacuum dehydration in a dehydration tower, condensing and collecting NMP at the top of the tower, and pumping the tower bottom into a rectification two-effect tower; obtaining NMP at the top of the rectification two-effect tower, sending the liquid residue to a depolymerization reactor after evaporation of the gas phase in a thin film evaporator, and condensing and condensing; performing side line extraction on the rectification two-effect tower and injecting sulfolane to extract heavy components, separating after mixing, returning the light phase to the rectification two-effect tower, and sending the heavy phase to a regeneration tower; collecting NMP-water azeotrope at the top of the regeneration tower to return to the dehydration tower, collecting sulfolane at the side line to return to the extraction cycle, and sending the concentrated residue at the bottom to the depolymerization reactor; sending the depolymerization gas obtained from the depolymerization reactor to a quenching tower, sending the cooling liquid of the quenching tower to a light-removing tower, sending the overhead product of the light-removing tower to sewage treatment, and collecting NMP at the tower bottom. The recovery treatment method has reasonable and efficient process flow, and has higher NMP yield for complex NMP-containing waste liquid.

A process of thermal management fluid reclamation is provided. The process includes collecting at least one recovered thermal management fluid including at least a first refrigerant compound and a second refrigerant compound to form a collected thermal management fluid; and forming a blend constituent from the collected thermal management fluid in the absence of distillation or substantially in the absence of distillation. The blend constituent is azeotropic, azeotrope-like, or close-boiling. The blend constituent is configured to be combined with (i) one or more refrigerant compounds, and / or (ii) one or more blends comprising two or more refrigerant compounds, for formation of a thermal management fluid product.

The utility model relates to the technical field of petrochemical engineering, and discloses a C4 integrated device which comprises a countercurrent multistage reactor, a reduced pressure rectifying tower and an azeotropic rectifying tower which are arranged on the same straight line, a mixed C4 feeding hole and a catalyst feeding hole are formed in one side of the countercurrent multi-stage reactor, the bottom end of the countercurrent multi-stage reactor is connected with a reactor discharging pipe, and one end, far away from the reduced pressure rectifying tower, of the reactor discharging pipe is connected with a feeding hole of the reduced pressure rectifying tower; through the pressure transmitter, the component analysis probe and the temperature sensor, the temperature, pressure and component change in the azeotropic rectifying tower can be monitored in real time, so that the temperature gradient in the azeotropic rectifying tower can be adjusted by controlling the flow of cooling liquid and the flow of steam, the probability of C4 azeotrope interference is reduced, and temperature capture can be carried out on key positions such as a rectifying section and a stripping section.

The invention discloses a rectification device and method for separating and purifying normal propyl alcohol-isopropyl alcohol-tetrahydrofuran-water azeotrope, relates to the field of separation and purification, and provides a novel rectification tower which is internally provided with two vertical partition plates, ethylene oxide is used as a reaction solvent, ethylene glycol is used as an extraction agent, and the normal propyl alcohol-isopropyl alcohol-tetrahydrofuran-water azeotrope is separated and purified. The separation and purification of the n-propanol-isopropanol-tetrahydrofuran-water azeotrope are realized in the rectifying tower, the process flow is short, the separation effect is good, the thermal efficiency is high, the energy consumption is low, the emission of carbon dioxide is less, the equipment investment is less, the occupied area is small, the obtained n-propanol, isopropanol and tetrahydrofuran are high in purity, the practicability is strong, and the sustainable development is favorably realized. Compared with the traditional multi-stage extractive distillation, the rectifying tower disclosed by the invention has the advantages that the heat utilization efficiency is improved, the equipment investment is reduced by about 40-50%, the occupied area is reduced by about 50-60%, and the construction cost is effectively saved.

Minimum-boiling, heterogeneous azeotropic and azeotrope-like compositions including 1,1,2,2,3-pentachloropropane (HCC-240aa) and hydrogen fluoride (HF), as well as methods for using these azeotropic or azeotrope-like compositions in the production of trifluorochloropropenes.

Specifically, a process for controlling heavies in a recycle catalyst stream for use in a continuous hydroformylation process in which olefins are converted with synthesis gas in the presence of a hydroformylation catalyst to form an aldehyde product stream, followed by separation of the catalyst for recycle to the hydroformylation step, comprises removing a crude product stream from a hydroformylation reaction zone, the crude product stream comprising one or more aldehyde products, one or more heavy by-products, a transition metal-organophosphorus ligand complex catalyst, one or more unconverted reactants, and one or more inert lights; providing a water stream; combining the water stream with the crude product stream into an azeotropic vaporizer; removing from the vaporizer an overhead gas stream comprising the one or more aldehyde products, the one or more unconverted reactants, the one or more inert lights, a portion of the water, and a portion of the heavy by-products; a liquid recycle catalyst stream to be sent to the reaction zone, the liquid recycle catalyst stream comprising the transition metal-organophosphorus ligand complex catalyst, a remainder of the aldehyde product, and a remainder of the heavy by-products, as a residue stream from the azeotropic vaporizer, wherein at least 25% of the aldehyde product recovered in the overhead gas stream from the condenser is removed as a water azeotrope.

The utility model discloses a bio-based 1, 4-butanediol production process system which comprises an esterification unit, a hydrogenation unit, a tetrahydrofuran refining unit, a gamma-butyrolactone extraction unit, an azeotrope extraction unit and a 1, 4-butanediol refining unit which are communicated in sequence. The discharge end of the azeotrope extraction unit is sequentially connected with a post-treatment unit and a gamma-butyrolactone refining unit; the discharging end of the gamma-butyrolactone refining unit is communicated with the feeding end of the hydrogenation unit. According to the utility model, the azeotrope liquid containing BDO is subjected to dehydrogenation reaction to generate post-treatment liquid containing GBL, the post-treatment liquid is mixed with the byproduct GBL crude liquid, and the GBL reuse liquid is obtained through light component removal, heavy component removal and purification. The obtained GBL reuse liquid is returned to the previous procedure, and BDO is regenerated through hydrogenation reaction, so that the total yield of BDO in the process is improved.

Disclosed is a process for the preparation of triacetonamine (TAA), the process comprising (i) reacting acetone and ammonia to produce a reaction product comprising TAA, acetone, isopropylideneacetone, and TMDP; (ii) directing the reaction product to an acetone separation column to obtain an unreacted acetone stream; and a first bottoms stream; (iii) directing the first bottoms stream to an azeotrope separation column to obtain an azeotrope distillate stream comprising an aqueous azeotrope of isopropylideneacetone and TMDP; and a second bottoms stream; (iv) directing the second bottoms stream to a medium boil substance separation column to obtain a medium boil stream; and a third bottoms stream; (v) directing the third bottoms stream to a refining column to obtain pure TAA as a distillate stream; (vi) subjecting the azeotrope distillate stream to phase separation to obtain an organic phase and an aqueous phase; directing the organic phase to a TMDP separation column to obtain a recyclable distillate stream comprising isopropylideneacetone and a bottoms stream comprising TMDP; and (vii) at least partially recycling the unreacted acetone stream, the medium boil stream and the recycle distillate stream to step (i); and discarding the TMDP bottoms stream.

The invention belongs to the technical field of separation and purification, and particularly relates to a method for separating a methanol-dimethyl carbonate azeotrope system, which adopts a system for separating a methanol-dimethyl carbonate azeotrope and adopts a eutectic solvent as an extracting agent for extractive distillation. The hydrogen bond acceptor of the deep-eutectic solvent is choline chloride, and the hydrogen bond donor of the deep-eutectic solvent is malonic acid or urea. According to the method, the choline chloride deep eutectic solvent which is lower in cost, simpler and more convenient to prepare and more environmentally friendly is selected as the extracting agent, systematic process parameter optimization and equipment configuration design are carried out according to the high-viscosity characteristic of the choline chloride deep eutectic solvent, and stable, efficient and long-period operation of the high-viscosity green solvent in the continuous extractive distillation process is successfully achieved; the target of separating the methanol and the dimethyl carbonate from the binary mixture is achieved, the final yield of the methanol and the dimethyl carbonate can reach 99% or above, the product purity can reach 99.5% or above, and compared with a traditional solvent separation method, the energy consumption is greatly reduced, the equipment cost is saved, and the method is suitable for industrial production. The strict standard of the high-end chemical industry and the fine chemical industry on the raw material purity can be reached.

Provided are azeotrope and azeotrope-like compositions between HFO-1252zc, HFC-263fb, HF, and H2O, which are present in a process for the preparation or purification of HFO-1252zc, and methods for the preparation or purification of HFO-1252zc, HFC-263fb, HF, and H2O. Also provided are methods of forming and using these azeotrope and azeotrope-like compositions.

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 provides a continuous extractive distillation separation method of a p-xylene-propanol azeotropic mixture, and belongs to the technical field of separation. According to the method disclosed by the invention, any two of dibutyl phthalate, N-methyl pyrrolidone and sulfolane are used as extracting agents. The method comprises the following steps: adding a mixed raw material solution of p-xylene and propanol into an extraction tower, then adding an extraction agent, carrying out extractive distillation, extracting a propanol product from the top of the tower, introducing an extraction tower bottom product containing the extraction agent and p-xylene into a solvent recovery tower, and after distillation, extracting a p-xylene product from the top of the tower and discharging the extraction agent from the bottom of the solvent recovery tower; and introducing the extraction agent into the extraction tower for cyclic utilization. The method provided by the invention realizes the separation of the p-xylene-propanol azeotropic mixture, has high separation efficiency, is easy to regenerate and is environment-friendly, and the mass fraction of p-xylene in the separated propanol can be greater than or equal to 99.9%.

The present application relates to a kind of methyl isopropyl ketone production device and process for floor coating, belong to methyl isopropyl ketone production device and process technical field.It includes reaction rectifying tower, first refining tower, second refining tower, third refining tower;Reaction rectifying tower includes first kettle from bottom to top, reaction rectifying tower distillation section, reaction rectifying tower reaction section, reaction rectifying tower rectification section;First refining tower includes second kettle, first distillation section, first rectification section;Second refining tower includes third kettle, second distillation section, third rectification section;Third refining tower includes fourth kettle, fourth distillation section, fourth rectification section.The present application uses reaction rectification process, reaction and separation are coupled, isobutyric acid conversion rate is more than 90%;Using double-effect distillation integrated heat, energy consumption is reduced by 40-50%;Combining azeotrope and liquid-liquid phase separation technology, product purity can reach more than 99%, with the advantages of low by-product, low investment, low energy consumption.

Cleaning solvent blends comprising an HCFO such as l-chloro-2,3,3,- trifluoropropene; trans-dichloroethylene; and a high boiling HEE such as HFE-7300; have utility as a non-flammable, low-global warming potential, azeotrope-like cleaning solvent compositions. Additional solvent ingredients may include surfactants and co-solvents. A method for cleaning articles of soiling substances comprises contacting the articles with the solvent composition by any suitable means such as a spray delivered by a propellant gas, or by contact with liquid and / or vapor solvent compositions, as in a conventional vapor degreaser apparatus, and removing the composition from the articles.

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.

The invention belongs to the technical field of rice bran wax purification, and particularly relates to rice bran wax purification equipment which comprises a centrifugal separation box, the upper end of the centrifugal separation box is hermetically covered with a box cover, and a first motor is fixedly mounted in the center of the lower end of the centrifugal separation box; the output end of the first motor penetrates through the bottom of the centrifugal separation box and is coaxially and fixedly connected with a centrifugal disc in the centrifugal separation box. The rice bran wax purification process adopts the rice bran wax purification equipment for purification, and comprises the following steps: S1, putting the wax paste to be purified and the ternary azeotrope into the stirring tank according to a certain proportion, and uniformly stirring and mixing at a certain temperature through the second motor and the stirring rod. The device has the advantages that the centrifugal layering work can be quickly and effectively completed, the centrifugal efficiency is improved, the subsequent treatment and procedure continuity are ensured, and the purification effect and efficiency are greatly improved.

The application belongs to the field of membrane separation technology, and particularly relates to a hydrophilic pervaporation membrane for separating ethanol-water azeotrope and a preparation method thereof. The method comprises the following steps: adding IU particles into a polyvinyl alcohol-chitosan blended solution, and obtaining the hydrophilic pervaporation membrane after cross-linking; and the mass percentage of the IU particles in the polyvinyl alcohol-chitosan blended solution is 20-30 wt%. The application introduces imidazole compound IU modified particles while constructing a polyvinyl alcohol-chitosan mixed matrix membrane, the particles can be well dissolved in the polyvinyl alcohol-chitosan mixed solution, the hydrophilic imidazole groups at both ends of the particles and the hydrophobic fatty chain structure in the middle can be closely arranged in the prepared membrane, so that water molecules can selectively pass through the channel between adjacent hydrophilic groups, thereby improving the separation performance of the membrane. The prepared hydrophilic pervaporation membrane has the advantages of high flux, good separation performance, high film-forming property, low cost, stable structure and performance, and the like, and is suitable for separating ethanol-water systems.

The invention discloses a heat integration heat pump assisted extractive distillation separation methanol ether water azeotrope, which is characterized in that a methanol-methyl tert-amyl ether-water mixed solution is separated through three-tower operation of an extraction reduced pressure distillation tower T1, an extraction distillation tower T2 and a solvent recovery reduced pressure distillation tower T3. Tower top steam of the extractive distillation tower T2 is used for exchanging heat for part of liquid phase of a middle plate of the extractive decompression distillation tower T1, the problem that traditional heat integration cannot be achieved due to the fact that the tower top temperature of the extractive distillation tower T2 is between the tower top temperature of the extractive decompression distillation tower T1 and the tower kettle temperature is solved, and a novel heat integration strengthening process is developed. According to the process, heat energy is fully utilized, and energy consumption and equipment cost are reduced. And the adopted extracting agent dimethyl sulfoxide is small in dosage, relatively weak in volatility, small in extracting agent loss, easy to recover and environment-friendly. The purity of separated methanol is greater than 99.9%, the yield is greater than 99.9%, the purity of methyl tert-amyl ether is greater than 99.9%, the yield is greater than 99.9%, the purity of water is greater than 99.9%, the yield is greater than 99.9%, and the purity of mixed extraction agents dimethyl sulfoxide and ethylene glycol is greater than 99.9%, and the yield is greater than 99.9%.

Disclosed is a continuous-flow process for selective mono-nitration of aromatic hydrocarbons and polyaromatic hydrocarbons without using mixed acid. The process contacts a stream of aqueous nitric acid, preferably at or near the nitric-acid / water azeotrope (about 68–69 wt.% HNO3), with a stream containing an aromatic substrate in a continuous-flow reactor under controlled temperature and back-pressure to provide a residence time sufficient to achieve high conversion while suppressing di- and poly-nitration. The reactor effluent is phase-separated to recover (i) an organic phase comprising a mono-nitro aromatic product and optionally unreacted substrate, and (ii) an aqueous phase comprising unreacted and / or diluted nitric acid. The aqueous phase is optionally reconcentrated (e.g., by distillation) to a near-azeotropic nitric acid composition for recycle to the reactor feed. The process provides high selectivity to mono-nitro products with improved safety and reduced acidic waste relative to sulfuric-acid-based mixed-acid nitration.

The invention belongs to the field of separation of multiple systems of phenol, acetone and water, and particularly relates to a system and a method for recovering phenol and acetone in a bisphenol A production device. The system comprises a buffer tank, a liquid delivery pump, a pervaporation membrane device and a normal-pressure rectifying tower which are sequentially communicated, the pervaporation membrane device comprises a retentate side and a permeation side, and the retentate side is communicated with the normal-pressure rectifying tower. According to the technical scheme provided by the invention, based on pervaporation and rectification coupling, the azeotropic point problem of phenol and water is solved, high-concentration phenol can be recovered, an entrainer does not need to be introduced, separation units are reduced, and pollution of components outside the device is avoided.

A method for processing an input waste material is disclosed. The input waste material includes at least one polymeric fraction having an initial content of inherent impurities located in the at least one polymeric fraction. The method includes pickling the input waste material with an acidic solution, followed by removing the acidic solution including at least a portion of the inherent impurities, thereby obtaining a pickled output waste material. The method further includes mixing a liquid non-solvent with the pickled output waste material in an apparatus to form an azeotrope of the non-solvent and the inherent impurities, followed by outputting at least a portion of the inherent impurities from the apparatus in a gaseous state, thereby obtaining a pickled mixed output waste material.

The application discloses a separation system of methyl chlorosilane monomer, which comprises a low-removal column overhead compressor and a binary column overhead compressor. The overhead gas phase of the low-removal column is pressurized and heated by the low-removal column overhead compressor, and then the pressurized and heated gas phase is respectively delivered to a light separation column bottom reboiler, a hydrogen-containing column bottom reboiler, a azeotrope column bottom reboiler and a trimethyl column bottom reboiler through pipelines to provide the required heat source. The overhead gas phase of the binary column is pressurized and heated by the binary column overhead compressor, and then delivered to a binary column bottom reboiler to provide the heat source for the binary column bottom reboiler. The low-removal column overhead compressor, the low-removal column, the light separation column bottom reboiler, the hydrogen-containing column bottom reboiler, the azeotrope column bottom reboiler, the trimethyl column bottom reboiler, the binary column overhead compressor, the binary column and the binary column bottom reboiler constitute a heat pump circulation system, and the operation of the whole separation system of the methyl chlorosilane monomer reduces the consumption of external steam.

The present application belongs to the technical field of ethylene cracking C4 fraction separation, and relates to a 1,3-butadiene extraction process solvent regeneration method and device based on acetonitrile. The method comprises the following steps: extracting a circulating acetonitrile solvent into the middle part of a light-removing column, obtaining an azeotrope containing organic matters at the top of the column, and obtaining the light-removed acetonitrile solvent at the bottom of the column; the light-removed acetonitrile solvent is sent into a heavy-removing column to obtain a heavy-removing column top regenerated solvent and a heavy component product at the bottom of the column, and the heavy-removing column top regenerated solvent is returned to an extraction system. The present application has the following beneficial effects: the light-removing column top organic matter waste liquid discharge device is used to inhibit the circulation accumulation of organic matters such as alcohols and ketones in the entire butadiene extraction device at the cost of a small amount of acetonitrile loss. A new circulating acetonitrile solvent is extracted for regeneration, and negative pressure operation is avoided. The continuous regeneration mode or the intermittent regeneration mode can be selected, the device operation cost is reduced, and the economic benefit of the newly added solvent regeneration system is greatly improved.

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.