30results about How to "High productivity per pass" patented technology

The invention relates to a preparation method of Z-1,1,1,4,4,4-hexafluoro-2-butene, belonging to the field of chemical synthesis. The method comprises the following steps of taking hexachlorobutadiene (HCBD) as a raw material, performing gas-phase catalytic chlorination-fluoridation separation to obtain 2,3-dichlorohexafluoro-2-butene, performing liquid-phase dechlorination to obtain hexafluoro-2-butyne, and preparing the Z-1,1,1,4,4,4-hexafluoro-2-butene (Z-HFO-1336mzz) by means of performing gas-phase catalytic hydrogenation, wherein three reactions are included totally. The Z-1,1,1,4,4,4-hexafluoro-2-butene with high selectivity is obtained by means of performing catalytic hydrogenation by adopting the hexafluoro-2-butyne, and meanwhile the product is easily separated from side products and the raw material. The method disclosed by the invention has the advantages that the original raw material is easily obtained, the activity of a catalyst is high, the service life of the catalyst is long, the raw material can be recycled, and the standard of zero emissions is reached.

The invention discloses a preparation method of E-1-halo-3,3,3-trifluoropropene. In the presence of a block catalyst, in a tubular reactor, 1,1,1,3,3-pentachloropropane Gas-phase fluorination reaction with hydrogen fluoride to obtain the main product E-1-chloro-3,3,3-trifluoropropene and a small amount of product Z-1-chloro-3,3,3-trifluoropropene; further, in the block In the presence of a catalyst, E‑1‑chloro‑3,3,3‑trifluoropropene or / and Z‑1‑chloro‑3,3,3‑trifluoropropene reacts with hydrogen fluoride to generate gas phase fluorine in a tubular reactor chemical reaction to obtain the main product E-1,3,3,3-tetrafluoropropene. The single pass yield of the method of the invention is high; especially for the second step process, only the HCl in the first step product stream needs to be removed, and the remaining substances can be directly used for fluorination reaction after adding new HF. The block catalysts in the invention all have the characteristics of high activity and long service life.

The invention discloses a preparation method of E-1, 3, 3, 3-tetrafluoropropene, which comprises the following steps: by taking 3, 3, 3-trifluoropropyne or / and an isomer 1, 3, 3-trifluoropropadiene thereof as a raw material, carrying out gas-phase selective fluorination reaction in the presence of a fluorination catalyst to obtain E-1, 3, 3, 3-tetrafluoropropene. The method provided by the invention is mainly used for producing E-1, 3, 3, 3-tetrafluoropropene in a high-efficiency and gas-phase continuous circulation manner.

The invention discloses a nickel-based methanation catalyst promoted by an in-situ grew carbon nano tube and a preparation method for the nickel-based methanation catalyst and relates to a methanation catalyst. The catalyst comprises a main component and a promoter, wherein the main component comprises Ni and Mg; the promoter is the carbon nano tube and is represented by Ni / MgO-CNTs. The preparation method comprises the steps of mixing Ni(NO3)2*6H2O and Mg(NO3)2*6H2O, and dissolving the mixture in water to prepare a solution A, dissolving NaOH and NaHCO3 in water to prepare a solution B; adding the solution A and the solution B into a reaction container for reaction, aging and filtering precipitation liquid, washing until the filtrate is neutralized, drying and roasting to obtain an Ni / MgO catalyst precursor, then performing tabletting and screening, performing mixed dilution through quartz sand, putting the precursor in a rector, heating to 873K, reducing the precursor to obtain an Ni / MgO catalyst in a reduced state, converting gas flow into CO gas reaction, growing the carbon nano tube in situ, cooling to 823K to remove carbon impurities, and cooling to 473K to obtain a product.

The invention provides a pneumatic heating and quick warming process and equipment for the process. According to the pneumatic heating and quick warming process, the high-speed liquid and the liquid to be heated are contacted to generate a shock wave, the static temperature of the high-speed liquid is rapidly raised after the shock wave is generated, then the high-speed liquid is quickly mixed with the liquid to be heated, and thus the temperature of the liquid to be heated can be quickly raised. When the liquid to be heated is the petroleum hydrocarbon liquid, the temperature of the petroleum hydrocarbon liquid is instantaneously raised, the petroleum hydrocarbon liquid is cracked in a cracking area and the ethylene is separated out, so that the standing time in the reaction is short, and the per-pass yield of the ethylene is increased; in addition, the phenomenon of coking in the furnace can be avoided by utilizing the equipment.

The invention discloses a preparation method of Z-1,3,3,3-tetrafluoropropene, which uses 1,3,3,3-tetrafluoropropyne or / and its isomer 1,1,3 ,3-tetrafluoropropadiene is used as a raw material, and Z-1,3,3,3-tetrafluoropropene is obtained through selective hydrogenation in the gas phase in the presence of a hydrogenation catalyst. The invention is mainly used for producing Z-1,3,3,3-tetrafluoropropene with high efficiency and continuous gas phase circulation.

The invention discloses a method for continuously preparing 3,3,3-trifluoro-2-(trifluoromethyl)-1-propene in gas phase, which uses octafluoroisobutene as a raw material through hydrogenation-dehydrofluorination-hydrogenation-dehydrogenation Four-step gas-phase continuous reaction of hydrogen fluoride to obtain 3,3,3-trifluoro-2-(trifluoromethyl)-1-propene. Both the hydrogenation catalyst and the dehydrofluorination catalyst of the present invention have the characteristics of high activity and long service life; and through the gas phase independent circulation process, the incompletely reacted materials can be independently circulated, so that the initial raw materials can be almost completely converted3,3, 3‑trifluoro‑2‑(trifluoromethyl)‑1‑propene, and finally the product 3,3,3‑trifluoro‑2‑(trifluoromethyl) is extracted from the process system with high efficiency and continuous gas phase circulation )‑1‑propylene, so that no liquid waste and waste gas are produced, and green production is realized.

The invention discloses a method for continuously preparing 3, 3, 3-trifluoro-2-(trifluoromethyl)-1-propylene in a gas phase, and the method comprises the following steps: by taking octafluoroisobutylene as a raw material, carrying out hydrogenation-dehydrofluorination-hydrogenation-dehydrofluorination four-step gas phase continuous reaction to obtain the 3, 3, 3-trifluoro-2-(trifluoromethyl)-1-propylene. The hydrogenation catalyst and the dehydrofluorination catalyst have the characteristics of high activity and long service life; according to the present invention, by using the gas phase independent circulation process, the incomplete reaction material is subjected to independent circulation so as to completely convert the initial raw material into the 3, 3, 3-trifluoro-2-(trifluoromethyl)-1-propylene, and finally the product 3, 3, 3-trifluoro-2-(trifluoromethyl)-1-propylene is efficiently and continuously and circularly extracted from the process system in the gas phase; therefore, liquid waste and waste gas are not generated, and green production is realized.

The invention discloses a method for synthesizing fluorinated isobutene with hexafluoropropylene as a starting material, which comprises the following steps: (1) gas phase addition reaction: in the presence of a block catalyst, hexafluoropropylene and fluoromethane CHFXY(X , Y=F or H) undergoes gas phase addition to obtain (CF 3 ) 2 CFCHXY, (2) dehydrofluorination reaction: in the presence of dehydrofluorination catalyst, (CF 3 ) 2 CFCHXY is a raw material for dehydrofluorination reaction to obtain (CF 3 ) 2 C=CXY. Both the block catalyst and the dehydrofluorination catalyst in the invention have the characteristics of high activity and long service life, and can be used to produce fluorinated isobutene with high efficiency and continuous gas phase circulation.

The invention discloses a method for producing propylene from n-butene. Under the action of a catalyst, a raw material containing n-butene is subjected to cracking reaction under the reaction temperature of 500-600 DEG C, preferably 500-550 DEG C and the total reaction pressure (the absolute pressure) is 0-0.25MPa; the weight space velocity is 1-10h<-1>, preferably 1-5h<-1>; the catalyst comprises the following components in percentage by weight: 30-60 percent of a phosphorus-modified SAPO-11 molecular sieve, 20-30 percent of a hydrogen type ZSM-5 or ZSM-22 molecular sieve and the balance of an adhesive; the load of the phosphorus-modified SAPO-11 molecular sieve is 0.2-1 percent by weight (not including phosphorus in the SAPO-11 molecular sieve). The method used in the industrial process of producing propylene from the mixed carbon-4 raw material containing n-butene has the advantage of high once-through yield of propylene.

The invention discloses a method for preparing propylene from n-butene. A raw material containing the n-butene is in contact with a cracking catalyst under a catalytic cracking reaction condition, wherein the reaction temperature is 450-550 DEG C, preferably 450-500 DEG C, the reaction total pressure (absolute pressure) is 0-0.5MPa, preferably 0-0.15MPa, the weight space velocity is 1-10h<-1>, preferably 2-4h<-1>; according to the cracking catalyst, the content of FER molecular sieve and modified ZSM-5 molecular sieve is no less than 50%, and the mass ratio of the FER molecular sieve to the modified ZSM-5 molecular sieve is (1 to 1) to (3 to 1); the modified ZSM-5 molecular sieve comprises the following components in percentage by weight: 4.5-6.0% of zirconium dioxide, 0.2-0.5% of iridium oxide, 0.15-0.45% of SO4<2->, and the remaining of ZSM-5 molecular sieve, and molar ratio of silicon to aluminum of the FER molecular sieve is 50-100. The method has the advantages of low reaction temperature and high single-pass propylene yield for use in the industrial process of producing the propylene from the raw material containing n-butene mixed C4.

The invention relates to the method for preparing 4-tert-octyl-2,6-dicumyl phenol. The method is used for solving the problems in the existing 4-tert-octyl-2,6-dicumyl phenol production processes that the reaction selectivity is poor and disproportionation occurs at high temperatures. The method comprises the steps: (1) adding 4-tert-octyl phenol, metallic aluminum and rare earth chloride into a reactor, heating to carry out reaction until no bubble is discharged, carrying out heat preservation, adding ionic liquid into the reaction product, and uniformly mixing the ionic liquid and the reaction product, thereby obtaining a mixture; (2) dropwise adding alpha-methyl styrene into the mixture, and continuing to carry out reaction after alpha-methyl styrene is dropwise added completely, so as to obtain a reaction mixture; and (3) adding dilute sulfuric acid into the reaction mixture, adding an organic solvent into the dilute sulfuric acid added reaction mixture, precipitating to separate a water layer, then, directly cooling to precipitate crystals, filtrating the precipitated crystals to obtain a crude product, and recrystallizing the crude product with an ethanol-water mixed solvent, thereby obtaining 4-tert-octyl-2,6-dicumyl phenol. According to the method, the selectivity of 4-tert-octyl-2,6-dicumyl phenol is greatly improved. 4-tert-octyl phenol is effectively prevented from being disproportionated into phenol. The method is used for preparing 4-tert-octyl-2,6-dicumyl phenol.

The invention relates to a method for simultaneously preparing dichlorohexafluorocyclopentene isomers. The method comprises the following steps: taking hydrogen fluoride and trichloropentafluorocyclopentene as reaction raw materials; carrying out gas-phase catalysis fluorine-chlorine exchange reaction in the presence of a fluorination catalyst to obtain the dichlorohexafluorocyclopentene isomers. By adopting the method provided by the invention, 1,2-dichlorohexafluorocyclopentene, 1,3-dichlorohexafluorocyclopentene and 1,4-dichlorohexafluorocyclopentene can be coproduced, wherein the single-pass yield of the 1,3-dichlorohexafluorocyclopentene and the 1,4-dichlorohexafluorocyclopentene is relatively high and the sum of the yield of the 1,3-dichlorohexafluorocyclopentene and the 1,4-dichlorohexafluorocyclopentene is greater than 57 percent; the raw materials are easy to obtain and the fluorination catalyst has stable activity, so that the method is suitable for simultaneously and continuously preparing the 1,2-dichlorohexafluorocyclopentene, the 1,3-dichlorohexafluorocyclopentene and the 1,4-dichlorohexafluorocyclopentene in a large scale in a gas phase.

The invention discloses a preparation method of E-1,3,3,3-tetrafluoropropene, which uses 3,3,3-trifluoropropyne or / and its isomer 1,3,3-trifluoropropene Fluoropropadiene is used as a raw material, and E-1,3,3,3-tetrafluoropropene is obtained through gas-phase selective fluorination in the presence of a fluorination catalyst. The invention is mainly used for producing E-1,3,3,3-tetrafluoropropene with high efficiency and continuous gas phase circulation.

The invention discloses a method for preparing 3,3,3-trifluoropropyne by gas-phase dehydrohalogenation. ‑Trifluoropropene (halogen = F or Cl or Br or I) as a raw material, in the presence of a catalyst, undergoes a gas phase dehydrohalogenation reaction to obtain 3,3,3‑trifluoropropyne. The invention is mainly used for producing 3,3,3-trifluoropropyne with conversion rate and high selectivity in gas phase continuous circulation.

The invention discloses a preparation method of Z‑1‑halo‑3,3,3‑trifluoropropene. In the presence of a block catalyst, in a tubular reactor, E‑1‑halo‑3,3,3 -Trifluoropropene undergoes gas phase isomerization reaction to obtain Z-1-halo-3,3,3-trifluoropropene, wherein halogen=fluorine or chlorine, the present invention uses 1,1,1,3,3-pentachloro Propane is used as the starting material, and Z-1-chloro-3,3,3-trifluoropropene or Z-1,3,3,3-tetrafluoropropene are prepared by gas-phase fluorination reaction and isomerization reaction Products, the present invention independently circulates the incompletely reacted materials through the gas phase independent circulation process, so that the initial raw materials can be almost completely converted into the target product, and finally the target product is extracted from the process system, so that no liquid waste and waste gas are generated, and the realization of Green production.

The invention discloses a method for preparing E-1,1,1,4,4,4-hexafluoro-2-butene by gas-phase fluorination, namely: in the presence of a fluorination catalyst, tetrafluorobutatriene or tetrafluorobutatriene Chloroprene, fluorinated with hydrogen fluoride to give E-1,1,1,4,4,4-hexafluoro-2-butene. The invention is mainly used for producing E-1,1,1,4,4,4-hexafluoro-2-butene with high efficiency and continuous circulation.