74 results about "Catalytic distillation" patented technology

The utility model relates to a low-temperature decompression continuous catalytic rectifying tower for synthesizing diacetone alcohol, which comprises a catalytic rectifying tower, a condenser and a built-in reboiler, the catalytic rectifying tower comprises a reaction section and a stripping section, and a feed port of the catalytic rectifying tower is positioned between the reaction section and the stripping section. The external condenser is arranged at the tower top of the catalytic rectifying tower, the inlet end of the condenser is connected with a tower top outlet of the catalytic rectifying tower, the outlet end of the condenser is connected with a tower top side inlet of the catalytic rectifying tower, the built-in reboiler is arranged at the tower bottom of the catalytic rectifying tower, and a tower kettle extraction port is formed in the bottom of the catalytic rectifying tower. According to the utility model, not only is the reaction conversion rate (gt: 99.9%) obviously improved, but also the reaction selectivity reaches 100%, the generation of byproducts and the decomposition of diacetone alcohol are avoided, the reaction energy consumption is reduced, in addition, the product does not need to be subsequently separated, and the catalyst does not need to be separated and recycled.

The utility model relates to an energy-saving production device for preparing methyl tert-butyl ether by an isobutane dehydrogenation method. A raw material gasifier is arranged between the catalytic distillation tower feeding and discharging heat exchanger and the catalytic distillation tower, a temperature sensor is arranged on a feeding pipeline from the raw material gasifier to the catalytic distillation tower, a gas phase at the top of the catalytic distillation tower is divided into two pipelines, a compressor is additionally arranged on one pipeline, and an automatic flow regulating valve is additionally arranged on the other pipeline; a cold-side material outlet of the distillation tower feeding and discharging heat exchanger is connected with a cold-side material inlet of the raw material gasifier, a cold-side material outlet of the raw material gasifier is connected with a feeding hole in the middle lower part of the catalytic distillation tower, and a tower top discharging pipeline of the catalytic distillation tower is respectively connected with an inlet of the compressor and a hot-side material inlet of the condenser; an outlet pipeline of the compressor is connected with a hot measuring material inlet of the raw material gasifier, and a hot measuring material outlet of the raw material gasifier is connected with a liquid inlet of the return tank. According to the utility model, a heat pump technology is adopted, so that the heating power of the tower kettle reboiler is reduced, and the steam consumption is reduced; and the method is more economical.

The invention discloses a gasoline catalytic distillation desulfurization device and a gasoline catalytic distillation desulfurization method, relates to the technical field of hydrogenated gasoline processing, and aims to solve the problems that although various oil resources can be fractionated at different temperatures, the existing distillation desulfurization device is single in function and low in desulfurization efficiency due to limitation of gas retention time; the technical problem that the processing safety and quality are affected due to local hot spots and coking easily caused by distillation depending on the gas floating characteristic in the prior art is solved, and the device comprises a sealing assembly, a driving assembly connected with the sealing assembly and a collecting assembly located in the sealing assembly. By designing the collecting assembly and the isolating assembly, gasoline steam can be ensured to be in uniform contact with a solid catalyst, the desulfurization effect is guaranteed, on the other hand, gas can be in uniform contact with the isolating assembly and the collecting assembly in cooperation with operation of the motor, hot spot areas formed by overhigh local temperature in the initiation tower and the coking phenomenon are avoided, and the desulfurization efficiency is improved. And the use safety of the device and the quality of processed gasoline are ensured.

The application provides a continuous hydrogenation-isomerization method capable of meeting the treatment requirements of biological oils, especially waste oils, using a homogeneous hydrogenation process with strong adaptability to raw materials as a raw material pretreatment process, and matching a high-activity nanometer transition metal sulfide catalyst. On this basis, a catalytic distillation process is used for selective cracking of long-chain alkanes to improve the yield of medium and long-chain alkanes; an ultramicro flow hydrogen gas mixer and a reduced non-noble metal hydrogenation-isomerization catalyst are used to reduce the hydrogen / oil ratio and the energy consumption of the circulating hydrogen system, and to reduce the production cost of the catalyst, so as to finally realize efficient and low-carbon conversion of waste oils, and low-cost and high-selectivity preparation of biological aviation kerosene.

The present invention discloses a high-efficiency catalytic distillation tower for esterification of ethylene glycol and acetic acid: the interior of the tower includes three parts from top to bottom: the upper part is a distillation section, the middle part is a catalytic reaction section, and the lower part is a stripping section. The distillation section and the stripping section are filled with tower internals, and the catalytic reaction section is filled with a combined structured packing filled with catalyst. A gas phase outlet is provided at the top of the tower, a reflux port is provided at the upper part of the tower wall, an excess monomer inlet I is provided at the middle and upper part of the tower wall and is connected to the bottom of the distillation section, or an excess monomer inlet II is provided at the middle and lower part of the tower wall and is connected to the top of the stripping section; an inlet for a mixture of ethylene glycol, acetic acid, ethylene glycol monoacetate, and ethylene glycol diacetate is provided at the middle part of the tower wall and is connected to the lower part of the catalytic reaction section, and a discharge port is provided at the bottom of the tower; a gas phase outlet is connected to a condenser, and the outlet of the condenser is connected to a phase separation tank. The present invention solves the technical problem of insufficient catalytic and separation capacity of a catalytic distillation tower for esterification of ethylene glycol and acetic acid.

The invention relates to the technical field of MTBE production, in particular to a high-yield MTBE catalytic distillation device. The problem that the temperature of a reaction section in an existing device can only be roughly monitored is solved. Comprising a fixing shell, the fixing shell is rotationally connected with a partition part, the partition part is provided with storage modules which are vertically distributed at intervals, the storage modules are used for storing catalysts, flow guide folded plates which are evenly distributed in the circumferential direction are fixedly connected into the fixing shell, and the flow guide folded plates are located between every two adjacent storage modules. A temperature sensor is arranged at the bent position of the flow guide folded plate, a temperature control module is arranged on the lower portion of the flow guide folded plate, a motor is installed on the fixing shell, and an output shaft of the motor is in transmission with the partition piece through a gear set. The flow direction of materials is guided through the flow guide folded plate, so that most of the materials pass through the temperature sensor in the downward flowing process, and the monitoring precision of the device on the temperature of the materials at different positions is improved.

The application discloses a system and method for preparing 1-butene by using catalytic C4, and belongs to the technical field of 1-butene production. The technical scheme is that the system comprises an etherification reactor, a catalytic distillation column, a deep etherification reactor, a light component removal column and a heavy component removal column which are sequentially connected. The application uses catalytic C4 as raw material to prepare 1-butene, widens the raw material source for preparing 1-butene, improves the utilization rate of catalytic C4, and has a good application prospect.

The present application includes a production process, device and method of cyclopentanol. The process includes pyrolyzing a raw material containing dicyclopentadiene to obtain a material A containing cyclopentadiene, mixing it with hydrogen and contacting it with a bimetallic catalyst to undergo a hydrogenation reaction to obtain a material B containing cyclopentene, cyclopentadiene and cyclopentane, mixing it with an acid and a solid acid catalyst to undergo a catalytic esterification reaction to obtain a material C containing fatty acid cyclopentyl ester and fatty acid cyclopentenyl ester, and mixing the material C with hydrogen and then mixing it with a copper-based hydrogenation catalyst to undergo a hydrogenation reaction to obtain a product containing cyclopentanol. The device includes a pyrolysis unit, a selective hydrogenation unit, a catalytic distillation unit and a catalytic hydrogenation unit connected in series in a pipeline; the route has low raw material cost, mild reaction conditions, simple operation, low separation energy consumption, and is suitable for continuous and stable large-scale production. Adding an inhibitor prolongs the life of the catalyst and improves the yield. The yield of cyclopentanol is more than 95% based on cyclic olefins as raw materials.

The utility model provides a heavy component recycling system in an isobutene preparation process, which comprises a tertiary butanol catalytic distillation tower, an isobutene heavy component removal tower and a tertiary butanol extraction tower, the top of the tertiary butanol catalytic distillation tower is sequentially connected with a catalytic distillation tower condenser, a catalytic distillation tower return tank and an isobutene compressor; an outlet of the isobutene compressor is connected with an inlet in one side of the isobutene heavy component removal tower through a pipeline, the bottom of the isobutene heavy component removal tower is connected with the bottom of the tertiary butanol extraction tower through a pipeline, and the top of the isobutene heavy component removal tower is used for extracting high-purity isobutene; a return pipe of the tertiary butanol catalytic distillation tower is connected with an outlet of a demineralized water tank; an inlet of the demineralized water tank is connected with the bottom of the tertiary butanol extraction tower; demineralized water or sewage at the bottom of the tert-butyl alcohol catalytic distillation tower is collected from an inlet at the top of the tert-butyl alcohol extraction tower, and a purifier is arranged when the sewage at the bottom of the tower is collected. The system has the advantages of short flow, low investment, no additional energy consumption and high tertiary butanol recovery rate.

The invention relates to the field of chemical engineering, in particular to a catalytic distillation method for removing impurities in isooctane reaction raw materials, which comprises the following steps: S1, separating a C4 raw material and butadiene: treating the C4 raw material with desalted water to obtain a washed C4 raw material; carrying out coalescence dehydration treatment on the washed C4 raw material to obtain a dehydrated C4 raw material; the dehydrated C4 raw material is subjected to catalytic rectification treatment, a rectified C4 raw material is obtained, a catalyst for catalytic rectification treatment is a La-Ce / ZSM-5 catalyst, and the rectified C4 raw material is subjected to membrane separation, so that the C4 raw material and butadiene are obtained; and S2, pumping the C4 raw material into an alkylation reactor, and carrying out an alkylation reaction on the C4 raw material and isobutane under the action of a solid superacid catalyst to prepare isooctane. Compared with the prior art, the method has the advantages that impurities in the C4 raw material are removed, the byproduct butadiene and the C4 raw material are extracted, the service life of a catalyst in the isooctane preparation process can be prolonged by using the C4 raw material, the solid superacid catalyst is improved at the same time, and the C4 conversion rate and the isooctane yield are improved.

The utility model discloses a superimposed etherification co-production device and a co-production method. The device comprises a superimposed etherification reactor, a catalytic distillation tower, a methanol extraction tower, a methanol recovery tower, an MTBE (Methyl Tert-Butyl Ether) product tower and a superimposed oil product tower, wherein the superimposed etherification reactor is connected with the catalytic distillation tower; the top of the catalytic distillation tower is connected with the methanol extraction tower; the methanol extraction tower is circularly connected with the methanol recovery tower; a tower kettle of the catalytic distillation tower is sequentially connected with the MTBE product tower and the superimposed oil product tower; and the methanol recovery tower is also connected with the superimposed etherification reactor. The utility model provides a full-flow process for producing superimposed oil and methyl tert-butyl ether from mixed C4, so that the superimposed oil and the methyl tert-butyl ether are produced after the mixed C4 is subjected to the processes of superimposed etherification, catalytic distillation, methanol recovery, rectification separation and the like, and the mixed C4 can be continuously used as a raw material of a subsequent device after isobutene is completely converted.

The invention relates to a synthesis process of cyclopentyl methyl ether CPME, which firstly depolymerizes dicyclopentadiene DCPD to cyclopentadiene CPD through a depolymerization kettle at high temperature, then mixes the cyclopentadiene CPD with hydrogen and enters a hydrogenation catalytic distillation tower to generate cyclopentene CPE through a selective hydrogenation reaction, and then etherifies the cyclopentene CPE with methanol to obtain cyclopentyl methyl ether CPME, and the etherification reaction adopts a fixed bed and catalytic distillation combined process. The process of the invention is simple, energy-saving, and highly feasible; the hydrogenation and etherification catalysts have high conversion rates and good selectivity, and the process has the characteristics of high total conversion rate and good selectivity; through the selective hydrogenation of raw material C5, dienes are removed, which is conducive to extending the service life of the etherification catalyst, and the catalytic distillation process is adopted to make the temperature distribution of the reaction temperature area stable, the reaction heat is fully utilized, and the heat consumption is reduced.

The present invention discloses a catalytic distillation device and application for heat recovery of raw coke oven gas and coal tar pretreatment, comprising: a catalytic distillation column; the lower part of the catalytic distillation column is a washing area for mechanical impurities of raw coke oven gas; the upper part of the catalytic distillation column is a suspension bed catalytic distillation area, and a gas-phase material outlet is arranged in the catalytic distillation area. The gas-phase material outlet is connected to a heat exchanger through a pipeline. After being cooled by the heat exchanger, the material is connected to the material inlet in the middle of a gas-liquid separator through a pipeline. A gas-phase discharge port is arranged at the top of the gas-liquid separator, and a liquid-phase discharge port is arranged at the bottom of the gas-liquid separator. The liquid-phase discharge port is connected to the upper reflux port of the catalytic distillation column and an external discharge pipeline; the upper reflux port of the catalytic distillation column is connected to an oil-soluble suspension bed hydrogenation catalyst addition device. The device of the present invention can recover the heat of high-temperature raw coke oven gas while effectively pretreating coal tar, laying a foundation for subsequent processing.

The invention discloses a production device and a production method of dimethyl adipate, and belongs to the technical field of organic chemical synthesis. According to the scheme, efficient conversion of part of adipic acid is realized in the pre-reactor, so that the reaction load of a subsequent catalytic distillation tower is reduced; cyclohexane is adopted as an azeotropic water-carrying agent in a catalytic distillation tower, water generated by reaction is removed in real time through azeotropic distillation, the equilibrium limitation of esterification reaction is broken, complete conversion of adipic acid is realized, and the reaction efficiency is remarkably improved. According to the method, methanol and cyclopentane are efficiently separated through the washing step, cyclic utilization of cyclopentane is achieved, and raw material consumption is greatly reduced; meanwhile, resource utilization of methanol is achieved through the methanol recovery system, and waste emission is reduced. The method can effectively reduce energy consumption and production cost, improves product quality, and solves the problems of easy catalyst deactivation, severe equipment corrosion, high three-waste treatment cost and the like in the prior art.

The invention discloses a preparation method for improving the purity of BDO, which comprises the following steps: S1, putting sulfonic acid type ion exchange resin into a vacuum drying oven, and then cooling to room temperature to form a solid acid catalyst; s2, filling a reaction section of a catalytic distillation reactor with a solid acid catalyst, and introducing reaction raw materials into the reactor; s3, sequentially carrying out high-temperature, medium-temperature and low-temperature stepped cooling catalytic distillation by using a catalytic distillation reactor, adding an inhibitor at a low-temperature stage, and forming a reaction mixture when the temperature fluctuates within a range of + / -1 DEG C; s4, discharging the reaction mixture to a gas-liquid separator, recovering unreacted hydrogen through a recovery device, and collecting low-boiling-point byproducts through a condensing device to obtain residual liquid; s5, enabling the residual liquid to enter a rectifying tower for rectification; by adopting a stepped cooling catalytic distillation mode, the BDO purity can be improved, the impurity content can be reduced, the physical property can be optimized, and the stability can be enhanced.

The present invention discloses a gasoline catalytic distillation desulfurization device and method, which relates to the technical field of hydrogenated gasoline processing, and aims to solve the technical problems that the existing distillation desulfurization device can fractionate a variety of oil resources through different temperatures, but has a single function, and is limited by the gas retention time, resulting in low desulfurization efficiency, and distillation that relies on the gas floating characteristics is also prone to cause local hot spots and coking, affecting processing safety and quality, including a sealing component, a driving component connected to the sealing component, and a collection component located in the sealing component. The present invention can ensure that gasoline vapor is uniformly in contact with the solid catalyst to ensure the desulfurization effect by designing the collection component and the isolation component. On the other hand, in conjunction with the operation of the motor, the gas can be uniformly in contact with the isolation component and the collection component, avoiding the formation of hot spots and coking caused by excessively high local temperatures in the tower, thereby ensuring the safety of the device and the quality of the processed gasoline.

The utility model discloses DMMn production equipment, and relates to the technical field of chemical production equipment. The DMMn production equipment comprises a formaldehyde concentration separator, a formaldehyde absorption tower, a pre-reactor and a reactive distillation tower, and the formaldehyde concentration separator is used for concentrating a formaldehyde solution to prepare a concentrated formaldehyde solution and dilute formaldehyde steam; the formaldehyde absorption tower is used for absorbing dilute formaldehyde steam and preparing a dilute formaldehyde solution; the pre-reactor is used for enabling part of formaldehyde to react with methanol to generate methylal; and feeding the pre-reaction material into an upper reaction section of the reactive distillation column, feeding a concentrated formaldehyde solution into a lower reaction section, and generating a DMMn crude product under the action of catalytic distillation. The two formaldehyde solutions react in different areas, and redundant water is extracted in the reaction process, so that the influence of water on the whole reaction system is reduced, the conversion rate of formaldehyde is increased, and self-polymerization of formaldehyde is avoided.

The invention relates to the technical field of compound synthesis, in particular to an efficient continuous catalytic distillation synthesis method of aryl methyl ether, which comprises the following steps: feeding a saturated nitrogen heterocyclic compound as a catalyst into a reactive distillation tower, continuously pumping a mixed raw material of aryl phenol and dimethyl carbonate into the reactive distillation tower, and carrying out methylation reaction under normal pressure; the generated reaction product aryl methyl ether, unreacted dimethyl carbonate, methanol and other reaction byproducts enter a first rectifying tower from the tower top of the reactive rectifying tower for separation, the reaction product aryl methyl ether is obtained at the tower bottom of the first rectifying tower, and tower top components enter a second rectifying tower for further separation; the saturated nitrogen heterocyclic compound is 1, 3-dimethyl-2-imidazolinone and / or 1, 3-dimethyl-tetrahydro-2-pyrimidinone, and the saturated nitrogen heterocyclic compound is 1, 3-dimethyl-2-imidazolinone and / or 1, 3-dimethyl-tetrahydro-2-pyrimidinone; the molar ratio of aryl phenol to dimethyl carbonate exceeds 1: 2; the raw materials are simple in variety, continuous production can be achieved, the product yield is at least 96%, and the product purity is at least 99%.

The invention discloses a phenol separation coupling catalysis purification method, and relates to the technical field of fine chemical separation and purification. According to the method, a metal oxide modified H-ZSM-5 molecular sieve is used as a catalyst, a coupling reaction and a separation process are carried out in a catalytic rectifying tower, and two core processes are synchronously completed: 1, impurities such as phenol and o-cresol in raw materials are subjected to a targeted O-alkylation reaction with methanol, and the impurities difficult to separate are efficiently converted into an alkylate easy to rectify; and 2, precise fractionation is synchronously realized, heavy ether products are extracted and removed from a side line, and target products mainly comprising high-purity 2, 6-xylenol and 2, 4-xylenol are obtained in a tower kettle. Through integrated design of targeted conversion and synchronous separation, key impurities are removed with high selectivity, the process is simplified, equipment investment and energy consumption are reduced, non-target side reactions are avoided, and high selectivity, high yield, process economy and product quality of target xylenol are considered.

The invention relates to the technical field of production of dimethyl maleate, and discloses a device and a method for preparing dimethyl maleate. Comprising the following steps: (1) introducing a first raw material containing first liquid methanol and maleic anhydride into a plate tower reactor for first reaction to obtain a first liquid-phase product; in the process system of the first reaction, the molar ratio of the cyclically refluxed methanol to the first liquid methanol is (0.2-0.5): 1; (2) introducing second liquid methanol and the first liquid-phase product into a catalytic distillation tower reactor containing a catalyst, and carrying out a second reaction to obtain a second liquid-phase product; controlling the water content in a gas phase in a catalytic distillation tower in a reaction system in which the second reaction is carried out to be not higher than 30wt% through methanol steam stripping; and (3) carrying out refining treatment on the second liquid phase product to obtain dimethyl maleate. The purity of the dimethyl maleate product obtained in one pass by the method provided by the invention can reach 99% or above.

This invention discloses a high-yield MTBE catalytic distillation apparatus, specifically relating to the field of catalytic equipment technology. It includes a base on which a collection assembly is mounted. The collection assembly includes a catalytic tank housed within the base, with an inner liner in the center of the catalytic tank. The inner liner is equipped with several separation filter covers, all used for filtration. This invention creates a separation chamber between the inner liner and the catalytic tank. Utilizing the stacked separation filter covers on the inner liner, and taking advantage of the higher boiling point of MTBE compared to the feedstock, the unreacted low-boiling-point feedstock rapidly rises to the separation chamber during distillation, while the MTBE product flows downwards after being filtered through the separation filter covers. This achieves efficient separation of the two, solving the problem of difficulty in separating MTBE from low-boiling-point feedstocks in existing technologies.

This invention provides a catalyst for the direct continuous synthesis of dimethyl carbonate from carbon dioxide and methanol, its preparation method, and its application, belonging to the field of catalyst preparation technology. The catalytically active components are firmly loaded onto the surface of a network support using a cyclic high- and low-pressure electrophoretic deposition method, forming a multi-level layered structure with alternating loose and dense layers. When used in a fixed-bed reactor or catalytic distillation reaction section, this catalyst achieves catalytic function while ensuring uniform mixing of reactants in the fixed bed, effectively improving the contact efficiency between reactants and active sites, reducing bed pressure drop, resulting in high dimethyl carbonate yield and selectivity, and also facilitating catalyst recovery and reuse.

The present invention relates to the technical field of catalyst preparation, and in particular to a rapid soaking method for catalysts used in MTBE production, the method comprising: periodically acquiring the actual reflux water level rise rate with a preset initial duration, calculating the water level rise rate change between the actual reflux water level rise rates at any two adjacent acquisition moments, judging whether to start an abnormality inspection mode according to the water level rise rate change, and performing an abnormality inspection on each preparation link according to the abnormality inspection mode, and judging to start an extraction mode based on the fact that each preparation link is qualified. The present invention avoids a large amount of methanol remaining in the catalyst by replacing methanol with carbon four after ether, reduces the unqualified MTBE product caused by methanol accumulation at the bottom of the catalytic distillation tower, and improves the overall operating efficiency of the device; water is pressed out of the catalyst by pressure, thereby improving the soaking replacement efficiency and thus improving the overall production efficiency.

The invention provides a continuous hydrogenation-isomerization method capable of meeting the treatment requirements of biological oil and fat, especially waste oil and fat, a homogeneous hydrogenation process with strong raw material adaptability is used as a raw material pretreatment process, and meanwhile, a high-activity nano transition metal sulfide catalyst is matched. On the basis, the long-chain alkane is selectively cracked by adopting a catalytic distillation process, so that the yield of the medium-chain and long-chain alkane is increased; an ultramicro-flow hydrogen mixer and a reduction-state non-noble metal hydroisomerization catalyst are adopted, so that the production cost of the catalyst is reduced while the hydrogen-oil ratio and the energy consumption of a circulating hydrogen system are reduced, and finally, high-efficiency and low-carbon conversion of waste grease and low-cost and high-selectivity preparation of biological aviation kerosene are realized.

The utility model relates to an MTBE (methyl tert-butyl ether) production heat recovery system which comprises an etherification reaction device, a catalytic distillation device and a reboiler arranged at the bottom of the catalytic distillation device. A first heat exchange device and a second heat exchange device are sequentially arranged on a pipeline for connecting a discharge port of the etherification reaction device and a feed port of the catalytic distillation device, and an outlet in the bottom of the catalytic distillation device is connected with a hot side inlet of the first heat exchange device through a pipeline; and a shell pass outlet of the reboiler is connected with a hot side inlet of the second heat exchange device through a pipeline. According to the MTBE production heat recovery system, the energy consumption of the catalytic distillation tower can be reduced, the production cost is reduced, and the economic benefit is improved.

The utility model provides a device for co-production of tert-butyl alcohol and MTBE (Methyl Tert-Butyl Ether), which comprises a tert-butyl alcohol device and an MTBE device, and the tert-butyl alcohol device is connected with the MTBE device through a C4 circulating pipeline; the tertiary butanol device comprises a multi-stage hydration reaction assembly and a fourth decarburization tower; a first mixed C4 pipeline is arranged on one side of the multi-stage hydration reaction assembly, the multi-stage hydration reaction assembly is connected with a C4 removal tower through a pipeline, and the MTBE device comprises an etherification reactor, a catalytic distillation tower and a methanol washing recovery assembly; the etherification reactor is connected with the catalytic distillation tower through a pipeline, and the catalytic distillation tower is connected with the methanol washing recovery assembly through a pipeline; the methanol washing recovery assembly is connected with the etherification reactor through a pipeline, the first mixed C4 pipeline is connected with the etherification reactor through a second mixed C4 pipeline, and an MTBE output pipeline is arranged at the bottom of the catalytic distillation tower. The residual C4 produced by the C4 removal tower is sent to the etherification reactor of the MTBE device for further processing, so that the utilization rate of the effective component isobutene in the raw material C4 is increased.

The application belongs to the field of catalytic synthesis of trioxane, and particularly relates to a catalytic synthesis process and device of trioxane. The process comprises the following steps: step one, a mixture of methylal and methanol is mixed with oxygen-containing gas as raw material, and reacts to generate formaldehyde under the action of a first catalyst; step two, formaldehyde is dissolved and absorbed by water to obtain concentrated formaldehyde; step three, the concentrated formaldehyde is subjected to catalytic synthesis reaction under the action of a second catalyst to generate trioxane. The device comprises, in sequence in the feeding direction, an oxidation reactor, a heat exchanger, a formaldehyde absorption tower, a fixed bed reactor and a catalytic distillation tower; compared with pure methanol or pure methylal, the raw material of the application is easier to obtain and has lower production cost; the application obtains higher formaldehyde concentration through improved catalyst, and does not need to prepare high-concentration formaldehyde again by negative pressure concentration, so that the single-pass utilization rate of formaldehyde is improved, and various technical problems in the prior art are properly optimized.

A method for producing diisobutylene and triisobutylene based on isobutylene, first, a metal ion modified strong acid cation exchange resin is placed in a polymerization reactor and a catalytic distillation column; then fresh isobutylene raw material, a part of the reaction product output from the polymerization reactor and a part of the unreacted isobutylene output from the catalytic distillation column are jointly fed into the polymerization reactor for polymerization reaction, a part of the obtained reaction product enters the catalytic distillation column for polymerization reaction, and finally the obtained reaction product is transported to a diisobutylene rectification column, diisobutylene is obtained at the top of the column, and the bottom material is transported to a triisobutylene rectification column, triisobutylene is obtained at the top of the column. The method uses a metal ion modified strong acid cation exchange resin as a catalyst, reduces the activity of the catalyst, makes the polymerization reaction of isobutylene more easily controllable, does not need to add an inhibitor during the reaction process, saves the separation device of the inhibitor, is simple to operate, and produces triisobutylene as a byproduct while producing diisobutylene.

The invention belongs to the technical field of waste plastic resource recovery and heterogeneous catalytic distillation, and discloses a process for preparing an oil product by degrading waste plastic through molten salt distillation. Polyolefin waste plastic is used as a raw material, directional cracking of polyolefin is realized through a distillation degradation reaction under the catalysis and heat transfer synergistic effect of a molten salt system, and segmented separation of an oil product is synchronously completed. According to the process disclosed by the invention, by virtue of high-efficiency catalytic activity and excellent heat transfer performance of a molten salt system, high-efficiency degradation of the polyolefin waste plastics can be realized under relatively mild reaction conditions, and high-quality oil products can be directionally prepared; meanwhile, the preparation process of the molten salt system is simple, convenient and controllable, cyclic regeneration can be realized, the process cost is greatly reduced, and large-scale production is easy to realize. The method provides a brand new technical path for resource conversion of polyolefin waste plastics, has dual values of environmental protection treatment and resource recovery, and has an important application prospect in the fields of solid waste treatment and energy chemical industry.

The invention provides a method for preparing 1-pentene and co-producing isopentene and tert-amyl alcohol from C5 in the coal chemical industry, and relates to the technical field of comprehensive utilization of mixed C5. The method comprises the following steps: carrying out heavy component removal treatment on the coal chemical C5 fraction, carrying out light component removal treatment on the tower top fraction, mixing the tower kettle material with water and a solvent, feeding into a fixed bed filled with strong acid cation exchange resin, carrying out hydration reaction, rectifying the hydration product, and introducing the tower top material into a catalytic distillation tower filled with a double-bond isomerization catalyst, a material rich in 2-methyl-2-butene is obtained from the tower kettle, 2-methyl-2-butene is obtained through rectification, the tower kettle material obtained after the hydration product is rectified is subjected to azeotropic rectification, an entrainer and tert-amyl alcohol on the upper layer participate in reflux, and tert-amyl alcohol and a solvent are obtained from the tower kettle. According to the method disclosed by the invention, three products of 1-pentene, isopentene and tert-amyl alcohol can be obtained at one time, the price of the used catalyst is low, the reaction conditions are mild, and qualified products can be obtained by adopting a common distillation mode for most of the products.