WO2024077949A1 - 一种用于生产1,1,1,2,3-五氯丙烷的催化剂及其制备方法和应用 - Google Patents

一种用于生产1,1,1,2,3-五氯丙烷的催化剂及其制备方法和应用 Download PDF

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WO2024077949A1
WO2024077949A1 PCT/CN2023/094750 CN2023094750W WO2024077949A1 WO 2024077949 A1 WO2024077949 A1 WO 2024077949A1 CN 2023094750 W CN2023094750 W CN 2023094750W WO 2024077949 A1 WO2024077949 A1 WO 2024077949A1
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pentachloropropane
supported catalyst
reaction
producing
molecular sieve
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PCT/CN2023/094750
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English (en)
French (fr)
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周黎旸
童超丽
洪江永
任亚文
杨波
张彦
赵阳
余慧梅
周华东
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浙江衢化氟化学有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
    • B01J29/14—Iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/18—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type
    • B01J29/20—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type containing iron group metals, noble metals or copper
    • B01J29/24—Iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/46—Iron group metals or copper
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/013—Preparation of halogenated hydrocarbons by addition of halogens
    • C07C17/04—Preparation of halogenated hydrocarbons by addition of halogens to unsaturated halogenated hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C19/00—Acyclic saturated compounds containing halogen atoms
    • C07C19/01—Acyclic saturated compounds containing halogen atoms containing chlorine
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates to the technical field of hydrofluorochlorocarbons, and in particular to a supported catalyst for producing 1,1,1,2,3-pentachloropropane, and a preparation method and application thereof.
  • the first step is the polymerization reaction, using carbon tetrachloride and ethylene as raw materials to synthesize 1,1,1,3-tetrachloropropane:
  • the second step is chlorination reaction, using 1,1,1,3-tetrachloropropane and chlorine as raw materials to synthesize 1,1,1,2,3-pentachloropropane:
  • the third step is fluorination reaction, using 1,1,1,2,3-pentachloropropane and hydrogen fluoride as raw materials to synthesize 2-chloro-3,3,3-trifluoropropene:
  • the fourth step is fluorination reaction, using 2-chloro-3,3,3-trifluoropropene and hydrogen fluoride as raw materials to synthesize 2,3,3,3-tetrafluoropropene:
  • the second step reaction is generally divided into two steps. 1,1,1,3-tetrachloropropane is first dehydrochlorinated to obtain 1,1,3-trichloropropene and/or 3,3,3-trichloropropene. 1,1,3-trichloropropene and/or 3,3,3-trichloropropene are then reacted with chlorine.
  • the catalyst used is mainly ferric chloride, and the reaction is completed in the liquid phase.
  • CN109809959A discloses a method for preparing 1,1,1,2,3-pentachloropropane, in which anhydrous ferric chloride is used as a catalyst, 1,1,1,3-tetrachloropropane is first dehydrochlorinated at 80°C to obtain 1,1,3-trichloropropene, and then chlorine gas is continuously introduced when the temperature drops to 10°C to finally obtain the product 1,1,1,2,3-pentachloropropane.
  • the method of preparing 1,1,1,2,3-pentachloropropane with 1,1,1,3-tetrachloropropane and chlorine as raw materials has the following main shortcomings: on the one hand, the traditional 1,1,1,2,3-pentachloropropane synthesis process adopts dehydrochlorination first, and then adds chlorine to react after the dehydrochlorination reaction is completed or dehydrochlorinated to a certain extent, and the reaction temperatures of the two are inconsistent (dehydrochlorination The reaction temperature of hydrogen chloride needs to be higher than the chlorination temperature), which is difficult to control in actual operation.
  • the purpose of the present invention is to provide a supported catalyst for producing 1,1,1,2,3-pentachloropropane and a preparation method and application thereof in view of the deficiencies in the prior art.
  • the catalyst of the present invention has the advantages of simple preparation process, high product selectivity, and recyclability.
  • a supported catalyst for producing 1,1,1,2,3-pentachloropropane wherein the supported catalyst uses a molecular sieve as a carrier and loads 5 to 20 wt% (wt%, mass percentage) of iron as an active component, and the molecular sieve is at least one of a ZSM-5 molecular sieve, a HY molecular sieve, a H-MOR molecular sieve, and a 13X molecular sieve.
  • the present invention also provides a method for preparing the supported catalyst for producing 1,1,1,2,3-pentachloropropane, comprising the following steps:
  • step (3) filtering the reaction solution obtained in step (2), washing, drying, calcining and reducing the obtained filter cake to obtain a supported catalyst.
  • the iron salt is at least one of ferric nitrate, ferrous nitrate, ferric chloride and ferrous chloride.
  • the precipitant is at least one of sodium hydroxide, ammonia water, sodium carbonate and urea.
  • the stirring speed is 800-1200 r/min.
  • the drying temperature is 50-150° C., and the time is 12-36 hours; the calcination temperature is 400-800° C., and the time is 8-20 hours.
  • the reduction method is hydrogen reduction
  • the reduction temperature is 300-600° C.
  • the time is 10-24 hours.
  • the precipitation reaction is carried out at a temperature of 60 to 90° C. and for a time of 5 to 10 hours.
  • the present invention also provides a method for producing 1,1,1,2,3-pentachloropropane using the supported catalyst.
  • chlorinated hydrocarbons and chlorine are subjected to a catalytic reaction to obtain 1,1,1,2,3-pentachloropropane.
  • the catalytic reaction temperature is 30 to 60° C.
  • the pressure is 0.1 to 1.5 MPa
  • the reaction time is 5 to 24 hours.
  • the supported catalyst and chlorinated hydrocarbons are reacted to obtain 1,1,1,2,3-pentachloropropane.
  • the mass ratio of hydrocarbons is 0.002-0.008:1, and the molar ratio of chlorine gas to chlorinated hydrocarbons is 0.5-2.0:1.
  • the chlorinated hydrocarbon is 1,1,1,3-tetrachloropropane and/or trichloropropylene.
  • the invention adopts a precipitation method to prepare a supported iron-based catalyst, the catalyst preparation process is simple, and the reaction conditions are mild; when used for producing 1,1,1,2,3-pentachloropropane, the catalyst has good catalytic activity and high product yield, and has broad industrial application prospects; in actual production, the obtained product can be subjected to conventional purification operations such as distillation in the art as needed to obtain a 1,1,1,2,3-pentachloropropane product with higher purity.
  • the present invention has the following advantages:
  • the post-treatment is simple. Under the catalysis of the supported iron-based catalyst of the present invention, 1,1,1,3-tetrachloropropane and/or trichloropropylene and chlorine can react in one step to obtain 1,1,1,2,3-pentachloropropane. Compared with the traditional process using ferric chloride catalyst, the problem of separation of product and catalyst is completely solved. Moreover, the supported iron-based catalyst of the present invention can be recycled by solid-liquid separation, which further reduces the production cost.
  • 1,1,1,3-tetrachloropropane and/or trichloropropylene and chlorine can react in one step to obtain 1,1,1,2,3-pentachloropropane, that is, the product after dehydrochlorination of 1,1,1,3-tetrachloropropane directly undergoes chlorination reaction with chlorine. Since the dehydrochlorination reaction is an endothermic reaction, a certain amount of energy must be provided before the reaction, and the chlorination reaction is an exothermic reaction, and the released heat can be used by the dehydrochlorination reaction, thereby promoting the reaction rate. The two have a synergistic effect, significantly reduce the reaction temperature, and reduce the polymerization of trichloropropylene at the same time. The process is more reasonable and the reaction efficiency is significantly improved.
  • the catalyst has good activity. Under the catalysis of the supported iron-based catalyst of the present invention, 1,1,1,3-tetrachloropropane and/or trichloropropylene can react with chlorine under mild conditions.
  • the conversion rate of 1,1,1,3-tetrachloropropane is above 93.3%, and can reach up to 96.4%.
  • the selectivity of 1,1,1,2,3-pentachloropropane is above 94.1%, and can reach up to 98.2%.
  • the catalyst preparation process is simple.
  • the present invention adopts a precipitation method to prepare a supported iron-based catalyst.
  • the catalyst preparation process is simple and the reaction conditions are mild.
  • the obtained system was placed in an oil bath at 80°C and heated and stirred for 6h, cooled to room temperature, filtered, and the obtained filter cake was washed with deionized water until neutral, and then placed in a 100°C oven for drying for 24h.
  • the dried filter cake was placed in a muffle furnace and calcined at 500°C for 12h to obtain an oxidized iron-based catalyst.
  • the filter cake was placed in a tubular furnace and passed H 2
  • the reaction mixture was reduced at 300°C for 18 h (flow rate: 50 mL/min) to finally obtain a supported iron-based catalyst. Analysis showed that the iron content in the catalyst was 9.5 wt%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,1,3-tetrachloropropane (the mass ratio of the supported iron-based catalyst to 1,1,1,3-tetrachloropropane is 0.005:1) are added to a reactor with a volume of 2 L. Chlorine is added to the reactor through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube is inserted below the liquid level. The molar ratio of the added chlorine to 1,1,1,3-tetrachloropropane is 0.7:1.
  • the reaction temperature is maintained at 50° C. and the pressure is 0.1 MPa. After reacting for 5 hours, the reaction liquid is collected and sampled for gas chromatography analysis. It is obtained that the conversion rate of 1,1,1,3-tetrachloropropane in this embodiment is 94.5%, and the selectivity of 1,1,1,2,3-pentachloropropane is 95.9%.
  • the obtained system was placed in an oil bath at 80°C and heated and stirred for 6h, cooled to room temperature, filtered, and the obtained filter cake was washed with deionized water until it was neutral, and then placed in a 70°C oven for drying for 30h.
  • the dried filter cake was placed in a muffle furnace and calcined at 400°C for 20h to obtain an oxidized iron-based catalyst.
  • the filter cake was placed in a tubular furnace and passed H 2
  • the reaction mixture was reduced at 500°C for 10 h (flow rate: 50 mL/min) to finally obtain a supported iron-based catalyst. Analysis showed that the iron content in the catalyst was 4.9 wt%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,1,3-tetrachloropropane (the mass ratio of the supported iron-based catalyst to 1,1,1,3-tetrachloropropane is 0.008:1) are added to a reaction kettle with a volume of 2 L. Chlorine is added to the reaction kettle through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube is inserted below the liquid level. The added chlorine is reacted with The molar ratio of 1,1,1,3-tetrachloropropane was 0.9:1, the reaction temperature was maintained at 60°C, the pressure was 0.5 MPa, and the reaction liquid was collected after 6 hours of reaction.
  • the obtained system was placed in an oil bath at 85°C and heated with stirring for 7h, cooled to room temperature, filtered, and the obtained filter cake was washed with deionized water until it was neutral, and then placed in an oven at 100°C and dried for 24h.
  • the dried filter cake was placed in a muffle furnace and calcined at 800°C for 8h to obtain an oxidized iron-based catalyst.
  • the catalyst was then placed in a tubular furnace and passed H 2
  • the reaction mixture was reduced at 600°C (flow rate: 50 mL/min) for 24 h to finally obtain a supported iron-based catalyst. Analysis showed that the iron content in the catalyst was 19.8 wt%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,1,3-tetrachloropropane (the mass ratio of the supported iron-based catalyst to 1,1,1,3-tetrachloropropane is 0.002:1) are added to a reactor with a volume of 2 L. Chlorine is added to the reactor through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube is inserted below the liquid surface. The molar ratio of the added chlorine to 1,1,1,3-tetrachloropropane is 1:1.
  • the reaction temperature is maintained at 30° C. and the pressure is 1.0 MPa. After reacting for 8 hours, the reaction liquid is collected and sampled for gas chromatography analysis. It is obtained that the conversion rate of 1,1,1,3-tetrachloropropane in this embodiment is 96.4%, and the selectivity of 1,1,1,2,3-pentachloropropane is 95.7%.
  • the obtained system was placed in an oil bath at 70°C and heated with stirring for 8h, cooled to room temperature, filtered, and the obtained filter cake was washed with deionized water until neutral, and then placed in an oven at 120°C for drying for 18h.
  • the dried filter cake was placed in a muffle furnace and calcined at 500°C for 15h to obtain an oxidized iron-based catalyst.
  • the filter cake was placed in a tubular furnace and reduced at 500°C for 20h with H 2 (flow rate of 50mL/min) to finally obtain a supported iron-based catalyst.
  • the iron content in the catalyst was 8.5 wt%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,1,3-tetrachloropropane (the mass ratio of the supported iron-based catalyst to 1,1,1,3-tetrachloropropane is 0.005:1) are added to a reactor with a volume of 2 L. Chlorine is added to the reactor through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube is inserted below the liquid surface. The molar ratio of the added chlorine to 1,1,1,3-tetrachloropropane is 1.2:1.
  • the reaction temperature is maintained at 50° C. and the pressure is 0.1 MPa. After reacting for 8 hours, the reaction liquid is collected and sampled for gas chromatography analysis. It is obtained that the conversion rate of 1,1,1,3-tetrachloropropane in this embodiment is 95.3%, and the selectivity of 1,1,1,2,3-pentachloropropane is 97.4%.
  • the obtained system was placed in an oil bath at 70°C and heated and stirred for 9h, cooled to room temperature, filtered, and the obtained filter cake was washed with deionized water until neutral, and then placed in a 100°C oven for drying for 24h.
  • the dried filter cake was placed in a muffle furnace and calcined at 700°C for 10h to obtain an oxidized iron-based catalyst.
  • the filter cake was placed in a tubular furnace and passed H2
  • the catalyst was reduced at 600°C for 20 h (flow rate: 50 mL/min) to finally obtain a supported iron-based catalyst. Analysis showed that the iron content in the catalyst was 12.2 wt%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,1,3-tetrachloropropane (the mass ratio of the supported iron-based catalyst to 1,1,1,3-tetrachloropropane is 0.005:1) are added to a reactor with a volume of 2 L. Chlorine is added to the reactor through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube is inserted below the liquid level. The molar ratio of the added chlorine to 1,1,1,3-tetrachloropropane is 1.6:1.
  • the reaction temperature is maintained at 50° C. and the pressure is 1.5 MPa. After reacting for 10 hours, the reaction liquid is collected and sampled for gas chromatography analysis. It is obtained that the conversion rate of 1,1,1,3-tetrachloropropane in this embodiment is 95.4%, and the selectivity of 1,1,1,2,3-pentachloropropane is 94.1%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,3-trichloropropene (the mass ratio of the supported iron-based catalyst to 1,1,3-trichloropropene is 0.006:1) were added to the reactor with a volume of 2 L. Chlorine was added to the reactor through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube was inserted below the liquid surface. The molar ratio of the added chlorine to 1,1,3-trichloropropene was 0.8:1.
  • the reaction temperature was maintained at 50° C. and the pressure was 0.5 MPa. After 15 hours of reaction, the reaction liquid was collected and sampled for gas chromatography analysis. It was found that the conversion rate of 1,1,3-trichloropropene in this embodiment was 94.9%, and the selectivity of 1,1,1,2,3-pentachloropropane was 96.6%.
  • the obtained filter cake was washed with deionized water until it was neutral, and then dried in an oven at 100°C for 24 h.
  • the dried filter cake was placed in a muffle furnace and calcined at 500°C for 12 h to obtain an oxidized iron-based catalyst.
  • the catalyst was then placed in a tubular furnace and reduced at 400°C for 16 h with H 2 (flow rate of 50 mL/min) to finally obtain a supported iron-based catalyst. Analysis showed that the iron content in the catalyst was 14.4 wt%.
  • the supported iron-based catalyst prepared in step (1) and 1,1,3-trichloropropene (the mass ratio of the supported iron-based catalyst to 1,1,3-trichloropropene is 0.005:1) were added to a reaction kettle with a volume of 2 L. Chlorine was added to the reaction kettle through a polytetrafluoroethylene tube for reaction. The polytetrafluoroethylene tube was inserted below the liquid surface. The molar ratio of the added chlorine to 1,1,3-trichloropropene was 1.1:1. The reaction temperature was maintained at 50° C. and the pressure was 0.1 MPa. After reacting for 24 h, the reaction solution was collected and sampled for gas chromatography analysis. It was found that the conversion rate of 1,1,3-trichloropropene in this embodiment was 96.2%. The selectivity for 2,3-pentachloropropane was 95.1%.
  • the supported iron-based catalyst prepared in Example 4 was subjected to a cyclic experiment test: the reaction solution obtained in step (2) of Example 4 was separated by filtration, and the supported iron-based catalyst after the reaction was collected and used for the synthesis of 1,1,1,2,3-pentachloropropane.
  • the implementation method and reaction parameters were the same as those in step (2) of Example 4.
  • the results of the cyclic experiment are shown in Table 1.

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Abstract

本发明公开了一种用于生产1,1,1,2,3-五氯丙烷的负载型催化剂及其制备方法和应用，该催化剂以分子筛为载体，负载5～20wt％的铁为活性组分。在本发明的催化剂作用下，1,1,1,3-四氯丙烷和/或三氯丙烯与氯气可一步反应制备1,1,1,2,3-五氯丙烷，具有工艺简单，反应温和，对产物选择性高，催化剂可以循环使用等优点。

Description

一种用于生产1,1,1,2,3-五氯丙烷的催化剂及其制备方法和应用 技术领域
本发明涉及氢氟氯烃技术领域，具体涉及一种用于生产1,1,1,2,3-五氯丙烷的负载型催化剂及其制备方法和应用。
背景技术
近年来，2,3,3,3-四氟丙烯作为第四代新型制冷剂备受关注，其中以四氯化碳为原料出发的工艺路线较具商业优势，主要化学反应如下：
第一步调聚反应，以四氯化碳和乙烯为原料合成1,1,1,3-四氯丙烷：
第二步氯化反应，以1,1,1,3-四氯丙烷和氯气为原料合成1,1,1,2,3-五氯丙烷：
第三步氟化反应，以1,1,1,2,3-五氯丙烷和氟化氢为原料合成2-氯-3,3,3-三氟丙烯：
第四步氟化反应，以2-氯-3,3,3-三氟丙烯和氟化氢为原料合成2,3,3,3-四氟丙烯：
其中，第二步反应一般分成两步进行，1,1,1,3-四氯丙烷先脱氯化氢得到1,1,3-三氯丙烯和/或3,3,3-三氯丙烯，1,1,3-三氯丙烯和/或3,3,3-三氯丙烯再与氯气反应，所用催化剂以氯化铁为主，在液相中反应完成。
如CN109809959A公开了一种1,1,1,2,3-五氯丙烷的制备方法，以无水三氯化铁为催化剂，1,1,1,3-四氯丙烷先在80℃温度下脱氯化氢得到1,1,3-三氯丙烯，然后温度降至10℃时开始连续通入氯气，最终得到产物1,1,1,2,3-五氯丙烷。
现有制备技术中，以1,1,1,3-四氯丙烷和氯气为原料制备1,1,1,2,3-五氯丙烷的方法主要存在以下几点不足：一方面是传统的1,1,1,2,3-五氯丙烷合成工艺采用先脱氯化氢，待脱氯化氢反应结束或脱到一定程度时再加入氯气反应，两者反应温度不一致(脱 氯化氢反应温度需高于氯化温度)，实际操作过程中难以控制。另一方面，反应过程中三氯丙烯容易产生高沸物/聚合物，使催化剂失活、降低产物收率，造成后续分离提纯困难，不利于工业化生产与操作。
发明内容
本发明的目的是针对现有技术的不足，提供一种用于生产1,1,1,2,3-五氯丙烷的负载型催化剂及其制备方法和应用，本发明的催化剂具有制备过程简单，对产物选择性高，可以循环使用等优点。
为了解决上述技术问题，本发明是通过以下技术方案实现的：一种用于生产1,1,1,2,3-五氯丙烷的负载型催化剂，所述负载型催化剂以分子筛为载体，负载5～20wt％(wt％，质量百分含量)的铁为活性组分，所述分子筛为ZSM-5分子筛、HY分子筛、H-MOR分子筛、13X分子筛中的至少一种。
本发明还提供该用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，包括以下步骤：
(1)将铁盐、分子筛用去离子水配制成悬浊液，所述铁盐与分子筛的质量比为0.3～1.5:1，所述悬浊液中Fe3+的浓度为0.05～0.3mol/L；
(2)搅拌下，向上述悬浊液中加入沉淀剂进行沉淀反应，所述悬浊液中的Fe3+与沉淀剂的摩尔比为0.05～0.8:1，反应结束后冷却至室温，得到反应液；
(3)将步骤(2)得到的反应液过滤，将得到的滤饼洗涤、干燥、焙烧、还原，得到负载型催化剂。
优选的，所述铁盐为硝酸铁、硝酸亚铁、氯化铁、氯化亚铁中的至少一种。
优选的，所述沉淀剂为氢氧化钠、氨水、碳酸钠、尿素中的至少一种。
优选的，所述搅拌的转速为800～1200r/min。
优选的，所述干燥的温度为50～150℃，时间为12～36h；所述焙烧的温度为400～800℃，时间为8～20h。
优选的，所述还原方式为氢气还原，所述还原的温度为300～600℃，时间为10～24h。
优选的，所述沉淀反应的温度为60～90℃，时间为5～10h。
本发明还提供该负载型催化剂用于生产1,1,1,2,3-五氯丙烷的方法，在所述负载型催化剂的存在下，氯代烃和氯气进行催化反应得到1,1,1,2,3-五氯丙烷，所述催化反应的温度为30～60℃，压力为0.1～1.5MPa，反应时间为5～24h，所述负载型催化剂与氯代 烃的质量比为0.002～0.008:1，氯气与氯代烃的摩尔比为0.5～2.0:1。
优选的，所述氯代烃为1,1,1,3-四氯丙烷和/或三氯丙烯。
本发明采用沉淀法制备负载型铁基催化剂，催化剂制备工艺简单，反应条件温和；用于生产1,1,1,2,3-五氯丙烷时，催化活性好，产物收率高，具有广泛的工业化应用前景；实际生产中，可根据需要对所得产物采用本领域常规的精馏等提纯操作得到更高纯度的1,1,1,2,3-五氯丙烷产品。
相对于现有技术，本发明具有以下优点：
1、后处理简单，在本发明的负载型铁基催化剂催化下，1,1,1,3-四氯丙烷和/或三氯丙烯和氯气可一步反应得到1,1,1,2,3-五氯丙烷，相对于采用氯化铁催化剂的传统工艺，彻底解决了产物与催化剂分离的问题，且本发明的负载型铁基催化剂可通过固液分离进行回收利用，进一步降低了生产成本。
2、效率高，在本发明的负载型铁基催化剂催化下，1,1,1,3-四氯丙烷和/或三氯丙烯和氯气可一步反应得到1,1,1,2,3-五氯丙烷，即1,1,1,3-四氯丙烷脱氯化氢后产物直接与氯气进行氯化反应，由于脱氯化氢反应是吸热反应，反应前须有一定的能量提供，而氯化反应是放热反应，放出的热量刚好可以被脱氯化氢反应利用，从而促进了反应速率，两者具有协同作用，显著降低了反应温度，同时降低三氯丙烯的聚合，工艺更加合理，显著提高了反应效率。
3、催化剂活性好，在本发明的负载型铁基催化剂催化下，1,1,1,3-四氯丙烷和/或三氯丙烯与氯气可在温和条件下反应，1,1,1,3-四氯丙烷的转化率在93.3％以上，最高可达96.4％，1,1,1,2,3-五氯丙烷的选择性在94.1％以上，最高可达98.2％。
4、催化剂制备工艺简单，本发明采用沉淀法制备负载型铁基催化剂，催化剂制备工艺简单，反应条件温和。
具体实施方式
下面将结合本发明中的实施例，对本发明中的技术方案进行清楚、完整地描述。显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
实施例1
(1)负载型铁基催化剂的制备
将36g Fe(NO3)3·9H2O置于烧杯中，加入500mL去离子水，搅拌至Fe(NO3)3·9H2O完全溶解，然后加入50g的ZSM-5分子筛，搅拌使其分散均匀得到悬浊液；然后在1000r/min搅拌转速下向悬浊液中加入25wt％氨水溶液，悬浊液中的Fe3+与加入的氨的摩尔比为0.05:1，室温搅拌20min后，将所得体系置于80℃的油浴锅中加热搅拌6h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于100℃烘箱中干燥24h；将干燥后的滤饼置于马弗炉中，在500℃下焙烧12h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)300℃还原18h，最终得到负载型铁基催化剂，经分析，催化剂中铁含量为9.5wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,1,3-四氯丙烷(负载型铁基催化剂与1,1,1,3-四氯丙烷的质量比为0.005:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与1,1,1,3-四氯丙烷的摩尔比为0.7:1，反应温度保持在50℃，压力为0.1MPa，反应5h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,1,3-四氯丙烷的转化率为94.5％，1,1,1,2,3-五氯丙烷的选择性为95.9％。
实施例2
(1)负载型铁基催化剂的制备
将18g Fe(NO3)3·9H2O置于烧杯中，加入500mL去离子水，搅拌至Fe(NO3)3·9H2O完全溶解，然后加入50g的13X分子筛，搅拌使其分散均匀得到悬浊液；然后在1000r/min搅拌转速下向悬浊液中加入25wt％氨水溶液，悬浊液中的Fe3+与加入的氨的摩尔比为0.1:1，室温搅拌20min后，将所得体系置于80℃的油浴锅中加热搅拌6h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于70℃烘箱中干燥30h；将干燥后的滤饼置于马弗炉中，在400℃下焙烧20h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)500℃还原10h，最终得到负载型铁基催化剂，经分析，催化剂中铁含量为4.9wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,1,3-四氯丙烷(负载型铁基催化剂与1,1,1,3-四氯丙烷的质量比为0.008:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与 1,1,1,3-四氯丙烷的摩尔比为0.9:1，反应温度保持在60℃，压力为0.5MPa，反应6h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,1,3-四氯丙烷的转化率为93.3％，1,1,1,2,3-五氯丙烷的选择性为98.2％。
实施例3
(1)负载型铁基催化剂的制备
将72g Fe(NO3)3·9H2O置于烧杯中，加入600mL去离子水，搅拌至Fe(NO3)3·9H2O完全溶解，然后加入50g的HY分子筛，搅拌使其分散均匀得到悬浊液；然后在800r/min搅拌转速下向悬浊液中加入尿素，悬浊液中的Fe3+与加入的尿素的摩尔比为0.3:1，室温搅拌20min后，将所得体系置于85℃的油浴锅中加热搅拌7h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于100℃烘箱中干燥24h；将干燥后的滤饼置于马弗炉中，在800℃下焙烧8h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)600℃还原24h，最终得到负载型铁基催化剂，经分析，催化剂中铁含量为19.8wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,1,3-四氯丙烷(负载型铁基催化剂与1,1,1,3-四氯丙烷的质量比为0.002:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与1,1,1,3-四氯丙烷的摩尔比为1:1，反应温度保持在30℃，压力为1.0MPa，反应8h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,1,3-四氯丙烷的转化率为96.4％，1,1,1,2,3-五氯丙烷的选择性为95.7％。
实施例4
(1)负载型铁基催化剂的制备
将24g FeCl3·6H2O置于烧杯中，加入500mL去离子水，搅拌至FeCl3·6H2O完全溶解，然后加入50g的ZSM-5分子筛，搅拌使其分散均匀得到悬浊液；然后在900r/min搅拌转速下向悬浊液中加入氢氧化钠，悬浊液中的Fe3+与加入的氢氧化钠的摩尔比为0.5:1，室温搅拌20min后，将所得体系置于70℃的油浴锅中加热搅拌8h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于120℃烘箱中干燥18h；将干燥后的滤饼置于马弗炉中，在500℃下焙烧15h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)500℃还原20h，最终得到负载型铁基催化剂，经分析， 催化剂中铁含量为8.5wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,1,3-四氯丙烷(负载型铁基催化剂与1,1,1,3-四氯丙烷的质量比为0.005:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与1,1,1,3-四氯丙烷的摩尔比为1.2:1，反应温度保持在50℃，压力为0.1MPa，反应8h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,1,3-四氯丙烷的转化率为95.3％，1,1,1,2,3-五氯丙烷的选择性为97.4％。
实施例5
(1)负载型铁基催化剂的制备
将26g FeCl2·4H2O置于烧杯中，加入550mL去离子水，搅拌至FeCl2·4H2O完全溶解，然后加入50g的H-MOR分子筛，搅拌使其分散均匀得到悬浊液；然后在1200r/min搅拌转速下向悬浊液中加入25wt％氨水溶液，悬浊液中的Fe3+与加入的氨的摩尔比为0.8:1，室温搅拌20min后，将所得体系置于70℃的油浴锅中加热搅拌9h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于100℃烘箱中干燥24h；将干燥后的滤饼置于马弗炉中，在700℃下焙烧10h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)600℃还原20h，最终得到负载型铁基催化剂，经分析，催化剂中铁含量为12.2wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,1,3-四氯丙烷(负载型铁基催化剂与1,1,1,3-四氯丙烷的质量比为0.005:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与1,1,1,3-四氯丙烷的摩尔比为1.6:1，反应温度保持在50℃，压力为1.5MPa，反应10h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,1,3-四氯丙烷的转化率为95.4％，1,1,1,2,3-五氯丙烷的选择性为94.1％。
实施例6
(1)负载型铁基催化剂的制备
将16g Fe(NO3)2置于烧杯中，加入500mL去离子水，搅拌至Fe(NO3)2完全溶解，然后加入50g的ZSM-5分子筛，搅拌使其分散均匀得到悬浊液；然后在1000r/min搅拌 转速下向悬浊液中加入氢氧化钠，悬浊液中的Fe3+与加入的氢氧化钠的摩尔比为0.3:1，室温搅拌20min后，将所得体系置于75℃的油浴锅中加热搅拌6h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于100℃烘箱中干燥24h；将干燥后的滤饼置于马弗炉中，在500℃下焙烧12h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)350℃还原18h，最终得到负载型铁基催化剂，经分析，催化剂中铁含量为9.7wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,3-三氯丙烯(负载型铁基催化剂与1,1,3-三氯丙烯的质量比为0.006:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与1,1,3-三氯丙烯的摩尔比为0.8:1，反应温度保持在50℃，压力为0.5MPa，反应15h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,3-三氯丙烯的转化率为94.9％，1,1,1,2,3-五氯丙烷的选择性为96.6％。。
实施例7
(1)负载型铁基催化剂的制备
将24g Fe(NO3)2置于烧杯中，加入500mL去离子水，搅拌至Fe(NO3)2完全溶解，然后加入50g的ZSM-5分子筛，搅拌使其分散均匀得到悬浊液；然后在1000r/min搅拌转速下向悬浊液中加入碳酸钠，悬浊液中的Fe3+与加入的碳酸钠的摩尔比为0.3:1，室温搅拌20min后，将所得体系置于80℃的油浴锅中加热搅拌6h，冷却到室温，过滤，将所得滤饼用去离子水洗涤至中性后，置于100℃烘箱中干燥24h；将干燥后的滤饼置于马弗炉中，在500℃下焙烧12h，得到氧化态的铁基催化剂；随后将其置于管式炉中通H2(流速为50mL/min)400℃还原16h，最终得到负载型铁基催化剂，经分析，催化剂中铁含量为14.4wt％。
(2)1,1,1,2,3-五氯丙烷的合成
在容积为2L的反应釜中加入步骤(1)制备得到的负载型铁基催化剂和1,1,3-三氯丙烯(负载型铁基催化剂与1,1,3-三氯丙烯的质量比为0.005:1)，通过聚四氟乙烯管将氯气加入反应釜中进行反应，所述聚四氟乙烯管插入到液面以下，加入的氯气与1,1,3-三氯丙烯的摩尔比为1.1:1，反应温度保持在50℃，压力为0.1MPa，反应24h后收集反应液，取样通过气相色谱分析，得出本实施例1,1,3-三氯丙烯的转化率为96.2％，1,1,1, 2,3-五氯丙烷的选择性为95.1％。
实施例8
对实施例4制备的负载型铁基催化剂进行循环实验测试：将实施例4步骤(2)得到的反应液通过过滤分离，收集反应后的负载型铁基催化剂用于1,1,1,2,3-五氯丙烷的合成，实施方式及反应参数同实施例4步骤(2)。循环实验结果如表1所示。
表1实施例4得到的负载型铁基催化剂循环实验测试结果
从表1可以看出，循环使用5次后，1,1,1,3-四氯丙烷的转化率和1,1,1,2,3-五氯丙烷的选择性基本不变，说明该催化剂具有良好的稳定性，能够实现催化剂循环使用。

Claims (10)

  1. 一种用于生产1,1,1,2,3-五氯丙烷的负载型催化剂，其特征在于，所述负载型催化剂以分子筛为载体，负载5～20wt％的铁为活性组分，所述分子筛为ZSM-5分子筛、HY分子筛、H-MOR分子筛、13X分子筛中的至少一种。
  2. 权利要求1所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，包括以下步骤：
    (1)将铁盐、分子筛用去离子水配制成悬浊液，所述铁盐与分子筛的质量比为0.3～1.5:1，所述悬浊液中Fe3+的浓度为0.05～0.3mol/L；
    (2)搅拌下，向上述悬浊液中加入沉淀剂进行沉淀反应，所述悬浊液中的Fe3+与沉淀剂的摩尔比为0.05～0.8:1，反应结束后冷却至室温，得到反应液；
    (3)将步骤(2)得到的反应液过滤，将得到的滤饼洗涤、干燥、焙烧、还原，得到负载型催化剂。
  3. 根据权利要求2所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，所述铁盐为硝酸铁、硝酸亚铁、氯化铁、氯化亚铁中的至少一种。
  4. 根据权利要求2所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，所述沉淀剂为氢氧化钠、氨水、碳酸钠、尿素中的至少一种。
  5. 根据权利要求2所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，所述搅拌的转速为800～1200r/min。
  6. 根据权利要求2所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，所述干燥的温度为50～150℃，时间为12～36h；所述焙烧的温度为400～800℃，时间为8～20h。
  7. 根据权利要求2所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，所述还原方式为氢气还原，所述还原的温度为300～600℃，时间为10～24h。
  8. 根据权利要求2所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的制备方法，其特征在于，所述沉淀反应的温度为60～90℃，时间为5～10h。
  9. 权利要求1所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的使用方法，其特征在于，在所述负载型催化剂的存在下，氯代烃和氯气进行催化反应得到1,1,1,2, 3-五氯丙烷，所述催化反应的温度为30～60℃，压力为0.1～1.5MPa，反应时间为5～24h，所述负载型催化剂与氯代烃的质量比为0.002～0.008:1，氯气与氯代烃的摩尔比为0.5～2.0:1。
  10. 根据权利要求9所述的用于生产1,1,1,2,3-五氯丙烷的负载型催化剂的使用方法，其特征在于，所述氯代烃为1,1,1,3-四氯丙烷和/或三氯丙烯。
PCT/CN2023/094750 2022-10-13 2023-05-17 一种用于生产1,1,1,2,3-五氯丙烷的催化剂及其制备方法和应用 WO2024077949A1 (zh)

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