WO2007073631A1 - Procede de purification catalytique de dechets gazeux contenant du trichlorethylene - Google Patents

Procede de purification catalytique de dechets gazeux contenant du trichlorethylene Download PDF

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Publication number
WO2007073631A1
WO2007073631A1 PCT/CN2006/000361 CN2006000361W WO2007073631A1 WO 2007073631 A1 WO2007073631 A1 WO 2007073631A1 CN 2006000361 W CN2006000361 W CN 2006000361W WO 2007073631 A1 WO2007073631 A1 WO 2007073631A1
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Prior art keywords
catalyst
trichloroethylene
waste gas
carrier
oxide
Prior art date
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PCT/CN2006/000361
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English (en)
Chinese (zh)
Inventor
Xingyi Wang
Dao Li
Yi Zheng
Qiguang Dai
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East China University Of Science And Technology
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Publication of WO2007073631A1 publication Critical patent/WO2007073631A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8659—Removing halogens or halogen compounds
    • B01D53/8662—Organic halogen compounds
    • 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
    • B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
    • B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
    • 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
    • B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
    • B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
    • B01J29/0316—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41 containing iron group metals, noble metals or copper
    • B01J29/0325—Noble metals
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/28—Phosphorising
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/206—Rare earth metals
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/37—Acid treatment

Definitions

  • the present invention relates to a process for treating a waste gas containing trichloroethylene, and more particularly to a process for catalytic combustion, and more particularly to a catalyst employed. Background technique
  • the hazards of chlorinated organic compounds are not only for human health, but also have a lasting, cumulative effect on biological systems, and destroy atmospheric ozone.
  • the persistent organic pollutants listed as the first are organic compounds containing chlorine [2] .
  • Chlorinated hydrocarbons are classified as aromatic hydrocarbon chlorides such as chlorobenzene, dichlorobenzene, and non-aromatic hydrocarbon chlorides such as vinyl chloride, polyvinyl chloride, chloroformam and polychloromethane, the former being derived from chlorine
  • Trichloroethylene is one of the most difficult to oxidize and decompose halogenated hydrocarbons in chlorinated hydrocarbons. Therefore, the development of catalytic purification technology for trichloroethylene has important environmental protection significance.
  • the technical problem to be solved by the present invention is to disclose a catalytic purification method of trichloroethylene exhaust gas to overcome the disadvantages of the prior art for producing polychlorinated hydrocarbons.
  • the method of the invention comprises the following steps:
  • a humid air is introduced into the exhaust gas containing trichloroethylene to carry out a reaction to convert trichloroethylene into a non-toxic gas of carbon dioxide and hydrogen chloride, thereby eliminating chlorine gas generated during the process, so that the catalyst can stably maintain oxidation activity for a long period of time.
  • the reaction temperature is 450 ° C
  • the conversion of trichloroethylene can reach more than 95%, and no polychlorinated hydrocarbons are formed.
  • the reaction pressure is 0.1-lMpa, preferably 0.1-0.5 Mpa, especially 0.1 Mpa, which is close to normal pressure, and the temperature is 300 to 600 ° C, preferably 400 to 500 ° C, especially 450 ° C.
  • Said catalyst consists of a carrier which is stable in moist air and a rare metal, rare earth oxide and phosphoric acid supported on the carrier;
  • the rare metal comprises one or more of palladium or platinum, preferably platinum, in an amount of from 0.08 to 5% by weight based on the total weight of the catalyst;
  • the rare earth oxide is one or more of an oxide of cerium or an oxide of cerium, in an amount of from 1 to 10% by weight based on the total weight of the catalyst;
  • Said carrier is a carrier well known in the art, preferably mesoporous silica, silica or he
  • the pure silicon molecular sieve material, the preferred carrier is a large surface mesoporous silica material.
  • the mesoporous silica MCM-41 can be prepared by a method disclosed in the literature (Nature, 1992, 359: 710);
  • the preferred components and weight levels of the catalyst are:
  • the preparation of the catalyst can be divided into two steps.
  • the first step is to impregnate the silica with a phosphoric acid solution, dry, and calcine.
  • the process can be carried out by an isometric impregnation method well known in the art, such as the literature (J. Mater. Chem., 2002, 12: 1582) Method of public gong;
  • the second step is to load rare metals with rare earth elements, such as the salt solution impregnation method commonly mentioned in the literature.
  • the amount of catalyst must be sufficient to convert trichloroethylene into carbon dioxide and hydrogen chloride in the presence of moist air.
  • concentration of trichloroethylene in the exhaust of trichloroethylene is 0.05-0.2 vol%, per gram of catalyst treatment.
  • the amount of exhaust gas is 10-30L per hour.
  • the humid air is air containing water vapor, and the water concentration must be such that all the chlorine gas generated by the reaction is converted into hydrogen chloride, but the water cannot be the inhibitor of the reaction.
  • the suitable water concentration is 0.1 ⁇ lvol. %;
  • the molar ratio of water to trichloroethylene is 2 ⁇ 5:1;
  • the trichloroethylene in the exhaust gas can be stably converted into carbon dioxide and hydrogen chloride for a long time, and the activity of the catalyst is not lowered.
  • the content of precious metals in the catalyst is particularly low, and the chlorine-containing hydrocarbons in the exhaust gas are eliminated in a particularly economical manner, and no polychlorinated hydrocarbon by-products are formed, which does not cause secondary pollution, and is a very effective method for treating uranium-containing hydrocarbon waste gas. , has a greater prospect of environmental protection applications.
  • CTMAB cetyltrimethylammonium bromide
  • n (TEOS): n (CTMAB): n (EDA): n (H 2 0) 1 : 0.12: 9.7: 130, stirred for 15 min, the pH of the system is adjusted to 10.5 with acetic acid. After stirring for 1.5 h, the sol mixture was transferred into a 100 ml stainless steel autoclave with a Teflon liner, and statically crystallized at 120 ° C in an oven at its own pressure for 72 h, taken out and cooled, and washed with deionized water.
  • MCM-41/P0 3 H The preparation of MCM-41/P0 3 H is prepared by the traditional impregnation method: The procedure is as follows: Weigh the above-mentioned calcined mesoporous molecular sieve MCM-41, and add 1.25, 1.5, 2.25, 4.5, 11.25 ml of H 3 P0 respectively. 4 The solution is stirred vigorously to maintain the system to quickly evaporate the water at a certain temperature. Then, it was dried at 100 ° C for 8 h and calcined at 400 ° C for 3 h to obtain MCM-41/P0 3 H to obtain a carrier carrying phosphoric acid, and the Si/P (atom) ratio was 100, 75, 50, 25, 15 respectively. , 10.
  • the acid amount of the different Si/P ratio carriers was tested according to the method H 3 -TPD well known in the art, and the results are shown in Table 1.
  • the in situ pyridine test of pyridine can confirm that the acidity caused by the phosphoric acid modification is B acid.
  • the noble metal active component is impregnated on the above carrier, firstly, chloroplatinic acid is formulated into an aqueous solution having a concentration of 0.00638 M, and then the pH is adjusted to 4.7 with aqueous ammonia, and each of the above carriers is taken as lg, and each is stirred with 2 mL of chloroplatinum.
  • the aqueous acid solution was slowly added to the carrier, and then allowed to stand overnight at room temperature in air, dried at 50 ° C, and calcined at 550 ° C for 4 hours to obtain various supported Pt catalysts.
  • the amount of Pt contained in each catalyst was determined by atomic absorption spectroscopy to be about 0.16 wt%.
  • Another series of catalysts were prepared with a concentration of 0.00319 M chloroplatinic acid aqueous solution, and the Pt content was 0.08.
  • Catalyst activity evaluation was carried out in a fixed bed reactor. All catalysts were tested for trichloroethylene (TCE) combustion activity in a U-shaped quartz micro-reverse (inner diameter 6 mm) with a catalyst dosage of 200 mg and a reaction temperature of 500 ° C. The temperature was automatically controlled by a K-type thermocouple. Trichloroethylene was injected into the vaporization chamber using a 100 series KDS120 microinjection pump from StoeMng, USA, and then mixed with humid air having a water concentration of 0.15 vd% into the reactor for combustion. The total flow of humid air is controlled by a mass flow meter.
  • TCE trichloroethylene
  • the concentration of trichloroethylene is controlled at 0.05 vol%, the amount of exhaust gas per gram of catalyst is 15 L per hour, and the gas velocity through the reactor is 120 m h.
  • the molar ratio of water to trichloroethylene is 3:1; the reaction pressure is O.lMpa, and the temperature is 450 °C.
  • the conversion of trichloroethylene is shown in Table 1.
  • the reaction products are carbon dioxide, hydrogen chloride and traces of chlorine.
  • Example 1 1 ml of a concentration of 0.00319 M chloroplatinic acid aqueous solution and 1 ml of a 0.01275 M palladium chloride aqueous solution were mixed, and each of the phosphoric acid-containing MCM-41/P0 3 H carriers prepared in Example 1 was impregnated with 2 mL of the mixed solution, respectively. Subsequent treatment According to the method of Example 1, 0.08 wt% of Pt-0.5 wt% Pd / MCM-41 / P0 3 H series catalyst was obtained.
  • Example 2 02 using a commercially available surface area of 303m 2 / g, as in Example 1 was immersed phosphate embodiment, to obtain various Si0 2 / P0 3 H phosphate content of the carrier.
  • 2 ml of a 0.00319 M aqueous solution of chloroplatinic acid was separately impregnated on various supports, and subsequent treatment was carried out in the same manner as in Example 1 to obtain a 0.08 wt% Pt/SiO 2 /PO 3 H catalyst.
  • the reaction temperature is 450 ° C
  • the reaction pressure is 0.5Mpa
  • the moisture content in humid air is 0.15vpl%
  • the concentration of trichloroethylene is 0.05vol%
  • the exhaust gas is treated per gram of catalyst per hour.
  • the amount of the reaction was 15 L, and the rest of the reaction conditions were the same as those in Example 1.
  • the conversion of trichloroethylene is shown in Table 3.
  • the reaction products were carbon dioxide, hydrogen chloride and a trace amount of chlorine.
  • the MCM-41 carrier prepared in Example 1 was excessively impregnated with 5 mL of a 0.1 M aqueous solution of cerium nitrate and cerium nitrate, and the solution was slowly added to the carrier under stirring; The mixture was dried (50 ° C) and calcined at 550 ° C for 4 h to obtain a MCM-41 carrier modified with La and Ce. The loading of La and Ce was about 10% by weight. 2 ml of a 0.00319 M aqueous solution of chloroplatinic acid was separately impregnated on the above-prepared Ce-MCM-41 and La-MCM-41 supports, and subjected to subsequent treatment in the same manner as in Example 1 to obtain 0.08 wt% of a Pt catalyst.
  • the reaction temperature is 450 ° C
  • the moisture content in humid air is 0.1 vol%
  • the concentration of trichloroethylene is 0.5ol%
  • the amount of exhaust gas per gram of catalyst per hour is 15L
  • the rest of the reaction The conditions are the same as those in Example 1.
  • the conversion of trichloroethylene is shown in Table 4.
  • the reaction product It is carbon dioxide, hydrogen chloride and traces of chlorine.
  • the MCM-41 P0 3 H series carrier prepared in Example 1 was excessively impregnated with 5 mL of a 0.1 M aqueous solution of cerium nitrate and cerium nitrate, and the solution was slowly added to the carrier under stirring; then at room temperature in air. The mixture was allowed to stand overnight, dried at a low temperature (50 ° C), and calcined at 550 ° C for 4 hours to obtain two series of carriers of MCM-41/P0 3 H modified with La and Ce. The loading of La and Ce was about 10% by weight. O. 08wt%R ⁇ The catalyst was then impregnated with a solution of 0. 08wt% R catalyst.
  • the reaction temperature is 450 ° C
  • the moisture content in humid air is 0.5 vol%
  • the concentration of trichloroethylene is 0.1 vd%
  • the amount of exhaust gas per gram of catalyst per hour is 30 L.
  • the conditions were the same as those in Example 1.
  • the conversion of trichloroethylene is shown in Table 5.
  • the reaction products were carbon dioxide, hydrogen chloride and traces of chlorine.
  • Example 2 The respective phosphoric acid content of MCM-41/P0 3 H carrier prepared in Example 1 was impregnated with 2 ml of a concentration of 0.01275 M and 0.0255 M palladium chloride aqueous solution, respectively, and the subsequent treatment was carried out according to Example 1, to obtain 0.5 wt.
  • reaction temperature is 450 ° C
  • moisture content in humid air is 0.2 vol%
  • concentration of trichloroethylene is 0.1 vol%
  • per gram of catalyst per hour The amount of waste gas was 15 L, and the rest of the reaction conditions were the same as those in Example 1.
  • the conversion of trichloroethylene is shown in Table 6.
  • the reaction products were carbon dioxide, hydrogen chloride and traces of chlorine.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Environmental & Geological Engineering (AREA)
  • Dispersion Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Catalysts (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

L'invention porte sur un procédé de purification catalytique de déchets gazeux contenant du trichloréthylène consistant à introduire de l'air humide dans le gaz pour produire des réactions en présence d'un catalyseur comportant un support stable dans l'air humide, et des métaux rares, des terres rares et de l'acide phosphorique disposés sur le support. Le trichloréthylène peut ainsi être converti de manière stable en CO2 et en HCl à basse température en présence pendant un temps long du catalyseur d'oxydation/décomposition dont l'activité ne décroît pas. La faible quantité de terres rares permet d'éliminer des déchets gazeux de manière très économique les hydrocarbures chlorés, sans produire de sous-produits ni de pollution secondaire. Le procédé est donc efficace et peut être utilisé largement pour la protection de l'environnement.
PCT/CN2006/000361 2005-12-29 2006-03-10 Procede de purification catalytique de dechets gazeux contenant du trichlorethylene WO2007073631A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113976125A (zh) * 2021-08-30 2022-01-28 郑州大学 Co掺杂ZnO催化剂及其制备方法和应用

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101185796A (zh) * 2007-12-11 2008-05-28 华东理工大学 一种氯代芳香烃废气催化净化方法
CN102211028B (zh) * 2010-04-08 2014-01-29 中化蓝天集团有限公司 合成三氟乙烯用加氢脱氯催化剂和其载体的新型预处理工艺
JP5859366B2 (ja) * 2011-09-06 2016-02-10 三井金属鉱業株式会社 排気ガス浄化用触媒及び排気ガス浄化用触媒構成体
CN103691464B (zh) * 2013-12-17 2015-10-28 华东理工大学 一种用于水中氯苯酚类化合物低温催化加氢消除的催化剂及其制备与应用
CN109603869B (zh) * 2019-01-23 2020-07-07 浙江大学 磷酸修饰的氧化铈催化剂及其制备方法和应用
CN110917871B (zh) * 2019-11-05 2022-03-25 河北科技大学 一种利用金属单质和/或金属氧化物吸收及催化氧化卤代烃的方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0852351A (ja) * 1994-08-09 1996-02-27 Sumitomo Metal Mining Co Ltd 揮発性有機塩素化合物分解用触媒
JPH0852361A (ja) * 1994-08-11 1996-02-27 Sumitomo Metal Mining Co Ltd 揮発性有機塩素化合物分解用触媒
JPH0857322A (ja) * 1994-08-19 1996-03-05 Sumitomo Metal Mining Co Ltd 揮発性有機ハロゲン化合物分解用触媒およびその製造方法
JPH0857323A (ja) * 1994-08-15 1996-03-05 Sumitomo Metal Mining Co Ltd 揮発性有機ハロゲン化合物分解用触媒およびその製造方法

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4343169A1 (de) * 1993-12-17 1995-06-22 Solvay Deutschland Katalytische Hydrodehalogenierung halogenhaltiger Verbindungen von Elementen der vierten Hauptgruppe
CN1157255C (zh) * 2000-03-22 2004-07-14 中国科学院大连化学物理研究所 一种用于卤代芳烃催化氧化消除的金属氧化物催化剂
AU2003201549A1 (en) * 2002-01-14 2003-07-24 K.U. Leuven Research And Development Catalytic destruction of halogenated hydrocarbons

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0852351A (ja) * 1994-08-09 1996-02-27 Sumitomo Metal Mining Co Ltd 揮発性有機塩素化合物分解用触媒
JPH0852361A (ja) * 1994-08-11 1996-02-27 Sumitomo Metal Mining Co Ltd 揮発性有機塩素化合物分解用触媒
JPH0857323A (ja) * 1994-08-15 1996-03-05 Sumitomo Metal Mining Co Ltd 揮発性有機ハロゲン化合物分解用触媒およびその製造方法
JPH0857322A (ja) * 1994-08-19 1996-03-05 Sumitomo Metal Mining Co Ltd 揮発性有機ハロゲン化合物分解用触媒およびその製造方法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113976125A (zh) * 2021-08-30 2022-01-28 郑州大学 Co掺杂ZnO催化剂及其制备方法和应用

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