RU97121285A - METHOD FOR PRODUCING ALLYL CHLORIDE AND REACTOR USED IN THIS METHOD - Google Patents

METHOD FOR PRODUCING ALLYL CHLORIDE AND REACTOR USED IN THIS METHOD

Info

Publication number
RU97121285A
RU97121285A RU97121285/04A RU97121285A RU97121285A RU 97121285 A RU97121285 A RU 97121285A RU 97121285/04 A RU97121285/04 A RU 97121285/04A RU 97121285 A RU97121285 A RU 97121285A RU 97121285 A RU97121285 A RU 97121285A
Authority
RU
Russia
Prior art keywords
zone
reactor
hpc
volume
preceding paragraphs
Prior art date
Application number
RU97121285/04A
Other languages
Russian (ru)
Other versions
RU2162459C2 (en
Inventor
М.Тиртауиджоджо Макс
К.Бекетт Пол
Ф.Бэйкер Джон
Original Assignee
Дзе Дау Кемикал Компани
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US08/449,635 external-priority patent/US5504266A/en
Application filed by Дзе Дау Кемикал Компани filed Critical Дзе Дау Кемикал Компани
Publication of RU97121285A publication Critical patent/RU97121285A/en
Application granted granted Critical
Publication of RU2162459C2 publication Critical patent/RU2162459C2/en

Links

Claims (11)

1. Способ получения аллилхлорида посредством реакции пропилена с молекулярным галогеном при молярном отношении, по крайней мере, 2,5:1 при температуре реакции 400-525oС, отличающийся тем, что (1) пропилен и молекулярный галоген вначале реагируют в зоне "непрерывно действующего реактора смешения" (НРС) при температуре реакции 400-525oС, с частичным превращением пропилена и молекулярного галогена в аллилгалогенид; и (2) реакционная смесь со стадии (1) поступает в зону реактора идеального вытеснения, где реакция продолжается при температуре 400-525oС до практически полного исчерпания молекулярного галогена.1. A method of producing allyl chloride by reacting propylene with a molecular halogen at a molar ratio of at least 2.5: 1 at a reaction temperature of 400-525 ° C. , characterized in that (1) propylene and molecular halogen initially react in the “continuously” zone active mixing reactor "(LDC) at a reaction temperature of 400-525 o C, with a partial conversion of propylene and molecular halogen to allyl halide; and (2) the reaction mixture from step (1) enters the zone of the ideal displacement reactor, where the reaction continues at a temperature of 400-525 o C until the molecular halogen is almost exhausted. 2. Способ по п.1, отличающийся тем, что молекулярный галоген представляет собой хлор. 2. The method according to claim 1, characterized in that the molecular halogen is chlorine. 3. Способ по любому из предыдущих пунктов, отличающийся тем, что зона НРС является приблизительно сферической, овальной или яйцевидной, а зона реактора идеального вытеснения является приблизительно трубчатой. 3. The method according to any one of the preceding paragraphs, characterized in that the LDC zone is approximately spherical, oval or ovoid, and the zone of the ideal displacement reactor is approximately tubular. 4. Способ по п.1, отличающийся тем, что молярное отношение пропилена к галогену, подаваемых в реактор, составляет не более 5:1. 4. The method according to claim 1, characterized in that the molar ratio of propylene to halogen supplied to the reactor is not more than 5: 1. 5. Способ по любому из предыдущих пунктов, отличающийся тем, что температура в зоне НРС составляет 425-500oС.5. The method according to any one of the preceding paragraphs, characterized in that the temperature in the zone of the LDCs is 425-500 o C. 6. Способ по любому из предыдущих пунктов, отличающийся тем, что отношение объема зоны НРС к суммарному объему зоны HPC и зоны реактора идеального вытеснения составляет от 0,4:1 до 0,85:1. 6. The method according to any of the preceding paragraphs, characterized in that the ratio of the volume of the LDC zone to the total volume of the HPC zone and the zone of the ideal displacement reactor is from 0.4: 1 to 0.85: 1. 7. Способ по любому из предыдущих пунктов, отличающийся тем, что интервал концентраций непрореагировавшего хлора в реакционной смеси, выходящей из зоны HPC, составляет 10-50% от концентрации в исходных реагентах. 7. The method according to any one of the preceding paragraphs, characterized in that the range of concentrations of unreacted chlorine in the reaction mixture leaving the HPC zone is 10-50% of the concentration in the starting reagents. 8. Способ по любому из предыдущих пунктов, отличающийся тем, что общее время пребывания реагентов в реакторе составляет в среднем 0,3-7 с. 8. The method according to any one of the preceding paragraphs, characterized in that the total residence time of the reactants in the reactor is on average 0.3-7 s. 9. Реакционный сосуд, содержащий: корпус со стенками, образующими камеру, указанная камера содержит зону непрерывно действующего реактора смешения (HPC), соединенную с зоной трубчатого реактора, причем указанная зона HPC имеет заданный объем, и указанная зона трубчатого реактора имеет заданный объем, в котором отношение объема зоны HPC к суммарному объему зоны HPC вместе с зоной трубчатого реактора составляет от примерно 0,1:1 до примерно 0,9:1; один или более входов в реактор, расположенных на зоне HPC, для ввода газообразных реагентов в зону HPC; средства для пропускания газового потока из зоны HPC в зону трубчатого реактора; и один или более выходов из реактора, расположенных на зоне трубчатого реактора, для отвода газообразного продукта из зоны трубчатого реактора. 9. A reaction vessel comprising: a vessel with walls forming a chamber, said chamber comprising a continuous mixing reactor (HPC) zone connected to a tubular reactor zone, said HPC zone having a predetermined volume, and said tubular reactor zone having a predetermined volume, wherein the ratio of the volume of the HPC zone to the total volume of the HPC zone together with the tubular reactor zone is from about 0.1: 1 to about 0.9: 1; one or more reactor inlets located in the HPC zone for introducing gaseous reactants into the HPC zone; means for passing a gas stream from the HPC zone to the zone of the tubular reactor; and one or more exits from the reactor located in the zone of the tubular reactor, for removal of the gaseous product from the zone of the tubular reactor. 10. Реакционный сосуд по п.9, отличающийся тем, что отношение объема зоны HPC к суммарному объему зоны HPC и зоны реактора идеального вытеснения составляет от 0,4:1 до 0,85:1. 10. The reaction vessel according to claim 9, characterized in that the ratio of the volume of the HPC zone to the total volume of the HPC zone and the zone of the ideal displacement reactor is from 0.4: 1 to 0.85: 1. 11. Реакционный сосуд по п.9, отличающийся тем, что зона НРС является приблизительно сферической, яйцевидной или овальной. 11. The reaction vessel according to claim 9, characterized in that the LDC zone is approximately spherical, ovoid or oval.
RU97121285/04A 1995-05-24 1996-02-27 Method of producing allyl halide and reactor for its embodiment RU2162459C2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US08/449,635 US5504266A (en) 1995-05-24 1995-05-24 Process to make allyl chloride and reactor useful in that process
US08/449,635 1995-05-24

Publications (2)

Publication Number Publication Date
RU97121285A true RU97121285A (en) 1999-10-27
RU2162459C2 RU2162459C2 (en) 2001-01-27

Family

ID=23784905

Family Applications (1)

Application Number Title Priority Date Filing Date
RU97121285/04A RU2162459C2 (en) 1995-05-24 1996-02-27 Method of producing allyl halide and reactor for its embodiment

Country Status (12)

Country Link
US (1) US5504266A (en)
EP (2) EP0837841B2 (en)
JP (1) JP4047381B2 (en)
KR (1) KR100415889B1 (en)
CN (1) CN1080712C (en)
CZ (1) CZ291902B6 (en)
DE (2) DE69631493T2 (en)
ES (1) ES2170224T5 (en)
PL (1) PL192831B1 (en)
RU (1) RU2162459C2 (en)
TW (1) TW334417B (en)
WO (1) WO1996037450A1 (en)

Families Citing this family (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5552131A (en) * 1994-06-30 1996-09-03 Arco Chemical Technology, L.P. Oxidation of secondary alcohols
US6004517A (en) * 1995-05-24 1999-12-21 The Dow Chemical Company Process to make allyl chloride and reactor useful in that process
CA2252703A1 (en) * 1996-04-26 1997-11-06 Exxonmobil Chemical Patents Inc. Process for the manufacture of hydroxycarbonyl compounds
WO1998049125A1 (en) * 1997-04-25 1998-11-05 Shell Internationale Research Maatschappij B.V. Process for manufacturing allylhalide and equipment to be used therefor
US5986022A (en) 1998-04-01 1999-11-16 Witco Corporation Continuous manufacture of silicone coploymers
CA2739924C (en) 2008-10-13 2017-03-07 Dow Global Technologies Llc Process for the production of chlorinated and/or fluorinated propenes
KR20120093857A (en) 2009-10-09 2012-08-23 다우 글로벌 테크놀로지스 엘엘씨 Process for the production of chlorinated and/or fluorinated propenes
EP2485833A2 (en) 2009-10-09 2012-08-15 Dow Global Technologies LLC Adiabatic plug flow reactors and process for producing a chlorinated and/or fluorinated propene and higher alkene
JP5782038B2 (en) 2009-10-09 2015-09-24 ダウ グローバル テクノロジーズ エルエルシー Isothermal multitubular reactor and process incorporating the reactor
JP5767231B2 (en) 2009-10-09 2015-08-19 ダウ グローバル テクノロジーズ エルエルシー Process for producing chlorinated and / or fluorinated propenes and higher alkenes
JP5918358B2 (en) 2011-05-31 2016-05-18 ブルー キューブ アイピー エルエルシー Method for producing chlorinated propene
CN103562164B (en) 2011-05-31 2016-04-20 陶氏环球技术有限责任公司 Produce the method for propylene dichloride class
AU2012268669B2 (en) 2011-06-08 2017-06-08 Dow Global Technologies Llc Process for the production of chlorinated and/or fluorinated propenes
US9475739B2 (en) 2011-08-07 2016-10-25 Blue Cube Ip Llc Process for the production of chlorinated propenes
CA2844207A1 (en) 2011-08-07 2013-02-14 Max Markus Tirtowidjojo Process for the production of chlorinated propenes
US9067855B2 (en) 2011-11-21 2015-06-30 Dow Global Technologies Llc Process for the production of chlorinated alkanes
US9199899B2 (en) 2011-12-02 2015-12-01 Blue Cube Ip Llc Process for the production of chlorinated alkanes
CA2856717A1 (en) 2011-12-02 2013-06-06 Dow Global Technologies Llc Process for the production of chlorinated alkanes
JP6170068B2 (en) 2011-12-13 2017-07-26 ブルー キューブ アイピー エルエルシー Method for producing chlorinated propane and propene
WO2013096311A1 (en) 2011-12-22 2013-06-27 Dow Global Technologies, Llc Process for the production of tetrachloromethane
US9512049B2 (en) 2011-12-23 2016-12-06 Dow Global Technologies Llc Process for the production of alkenes and/or aromatic compounds
WO2014046970A1 (en) 2012-09-20 2014-03-27 Dow Global Technologies, Llc Process for the production of chlorinated propenes
CA2884435A1 (en) 2012-09-20 2014-03-27 Dow Global Technologies Llc Process for the production of chlorinated propenes
JP6272878B2 (en) 2012-09-30 2018-01-31 ブルー キューブ アイピー エルエルシー Cough quench and method incorporating it
WO2014066083A1 (en) 2012-10-26 2014-05-01 Dow Global Technologies, Llc Mixer and reactor and process incorporating the same
JP6247311B2 (en) 2012-12-18 2017-12-13 ブルー キューブ アイピー エルエルシー Method for producing chlorinated propene
US9475740B2 (en) 2012-12-19 2016-10-25 Blue Cube Ip Llc Process for the production of chlorinated propenes
JP2016507590A (en) 2013-02-27 2016-03-10 ブルー キューブ アイピー エルエルシー Method for producing chlorinated propene
EP2964597B1 (en) 2013-03-09 2017-10-04 Blue Cube IP LLC Process for the production of chlorinated alkanes
CN103724157A (en) * 2013-12-19 2014-04-16 山东海益化工科技有限公司 Chlorination process in chloropropene production
CN103724155B (en) * 2013-12-19 2015-08-19 山东海益化工科技有限公司 A kind of production technique of propenyl chloride
CN103664505B (en) * 2013-12-24 2015-06-24 山东海益化工科技有限公司 Chloropropene production technology
US9416073B2 (en) * 2014-10-06 2016-08-16 Honeywell International Inc. Method to improve halogenation reactions
CN104876792A (en) * 2015-05-21 2015-09-02 山东海益化工科技有限公司 Method for producing high-purity chloropropene
CN104876793A (en) * 2015-05-21 2015-09-02 山东海益化工科技有限公司 Chloropropene refining process
KR102371372B1 (en) * 2017-12-01 2022-03-04 한화솔루션 주식회사 Vapor chlorinated reactor apparatus for propylene
CN110003962B (en) * 2019-05-06 2021-04-30 沈阳航空航天大学 Axial fixed bed methanation reactor
CN111285752A (en) * 2020-03-23 2020-06-16 山东凯泰科技股份有限公司 Multistage heat exchange reaction system for chloropropene production

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2643272A (en) * 1947-01-04 1953-06-23 Shell Dev Halo-substitution of organic compounds
BE535907A (en) * 1953-10-29
BE532862A (en) * 1953-10-29 1955-04-27
US3054831A (en) * 1958-04-10 1962-09-18 Union Carbide Corp Halogenation of organic compounds over a narrow temperature range
NL255559A (en) * 1959-10-09 1900-01-01
NL272865A (en) * 1960-12-22
GB1070891A (en) * 1963-01-01 1967-06-07 Yorkshire Tar Distillers Ltd Improvements in and relating to the continuous production of hexachlorocyclopentadien
GB1066219A (en) * 1963-05-02 1967-04-26 Pullman Inc Process for extraction of hydrogen halides from mixtures containing same
US3409408A (en) * 1963-10-04 1968-11-05 Ballestra Mario Column reactor with series reaction chambers
FR1412183A (en) * 1963-10-23 1965-09-24 Inventor Credit Anstalt Process and preparatory treatment for the initiation, activation and acceleration of physico-chemical processes or reactions on solid, liquid or gaseous substances, mixtures of these substances or solutions, in particular process and devices for purifying the air and decontaminating flue gases from enginesotto and diesel engines
FR1603831A (en) * 1968-12-20 1971-06-07 Reactor for halogenated hydrocarbon prodn
RO57828A2 (en) † 1971-02-23 1975-04-15
DE2115094B2 (en) * 1971-03-29 1981-07-23 Basf Ag, 6700 Ludwigshafen Process for the continuous production of an aqueous choline chloride solution
JPS4826732A (en) * 1971-08-09 1973-04-09
US3849075A (en) * 1972-05-08 1974-11-19 Union Carbide Corp Cracking reactor
US3865886A (en) * 1973-06-20 1975-02-11 Lummus Co Production of allyl chloride
US4319062A (en) * 1976-08-02 1982-03-09 The Dow Chemical Company Allyl chloride process
JPS60252434A (en) * 1984-05-25 1985-12-13 Sumitomo Chem Co Ltd Production of allyl chloride
JPS6140232A (en) * 1984-08-02 1986-02-26 Sumitomo Chem Co Ltd Production of allyl chloride
FR2609718B1 (en) * 1987-01-20 1989-03-31 Atochem PROCESS FOR THE MASS PREPARATION OF VINYL CHLORIDE POLYMERS AND COPOLYMERS
JP2813100B2 (en) * 1992-10-23 1998-10-22 株式会社トクヤマ Method and apparatus for producing allyl chloride
US5518700A (en) † 1994-06-25 1996-05-21 Shell Oil Company Cyclonic reactor

Similar Documents

Publication Publication Date Title
RU97121285A (en) METHOD FOR PRODUCING ALLYL CHLORIDE AND REACTOR USED IN THIS METHOD
RU2162459C2 (en) Method of producing allyl halide and reactor for its embodiment
DZ1544A1 (en) Process for the preparation of ethylene and mixtures containing ethylene.
US4310502A (en) Singlet delta oxygen generator and process
EP0024851B1 (en) Process for preparing chlorine dioxide
JPH10259003A (en) Production of chlorine dioxide
EA200000072A1 (en) METHOD OF MANUFACTURE MELAMINE
IE61630B1 (en) Process for the synthesis of ferric chloride
US5196618A (en) Method for the preparation of methyl chloride from carbon tetrachloride and methyl alcohol
US6004517A (en) Process to make allyl chloride and reactor useful in that process
RU1801963C (en) Method of monochloroacetic acid synthesis
JPS57142927A (en) Preparation of chloromethane
AU679388B2 (en) Method of purifying pentafluoroethane
SU876633A1 (en) Method of producing trichloroethylene and methyl chloride
JPS601288B2 (en) Method for producing 1,1,2-trichloroethane from 1,2-dichloroethane and chlorine
RU93043915A (en) METHOD FOR PRODUCING ETHYLENE OR A MIXTURE OF ETHYLENE AND VINYL CHLORIDE
SU437756A1 (en) The method of obtaining disubstituted cyanamides
RU2187491C1 (en) Method of synthesis of ethyl alcohol and acetic acid (variants)
SU1685916A1 (en) Method for obtaining monochloroacetic acid
SU724492A2 (en) Method of preparing freon-11 and freon-12
SU1237657A1 (en) Method of producing chloromethanes
Golodov et al. Kinetics of oxidative sulfonation of butylamine in the presence of CuCl 2
JPH06316404A (en) Preparation of chloramine
GB1503987A (en) Process for preparing 1,1,1-trichloro-ethane
CA2123033A1 (en) Process and apparatus for supplying alkali chlorate and acid to a reactor for producing chlorine dioxide