Wacker-chemie Gmbh

Degussa Aktiengesellschaft

Hoechst Aktiengesellschaft

Degussa - Huls Ag

Ludwig Schmidhammer

Rudolf Strasser

Gerhard Dummer

Klaus Haselwarter

Hermann Klaus

Peter Hirschmann

Dominik Dempf

Klaus-Peter Mohr

Klaus Deller

Helmfried Krause

Ernst Selbertinger

Franz Haunberger

Gunter Roscher

Karl-Heinz Schmidt

Rudolf Knabl

Albin Frank

Eduard Pichl

Willibald Dafinger

Gerhard Stettner

Rudolf Straszer

Herbert Patsch

Hellmuth Frey

Wilhelm Mack

Otto Fruhwirth

Otto Fruhwirt

Stefan Bosing

Willi Dafinger

A supported catalyst includes: a) 0.5-15 wt. % of one or more Cu-II compounds, the quantitative amounts referring to copper metal; b) 0.1-8 wt. % of one or more alkali metal compounds, the quantitative amounts referring to alkali metal; c) 0.1-10 wt. % of an oxide mixture including; c1) 80-95 mole % of oxides of cerite rare earths with atomic Nos. 57 to 62, except promethium, and c2) 5-20 mole % of zirconium dioxide, where c1) and c2) must together total 100 mole % and the quantitative amount of c) refers to the oxides of the mixture, and d) the remainder up to 100 wt. % being .gamma. and/or .alpha.-aluminum oxide as support material, wherein e) the support material d) has a total pore volume in the range from 0.65 to 1.2 cm.sup.3 /g, and wherein f) the supported catalyst is present in the form of cylindrical hollow bodies having at least one passage channel, the ratio of height h to external diameter d.sup.e being less than 1.5 for diameters d.sub.e of up to 6 mm, and the ratio h/d.sub.e being less than 0.6 for diameter d.sub.e greater than 6 mm. A process for producing the supported catalyst is also described.

Supported catalyst, process for its production as well as its use in the

A process is provided for the hydrogenation of chloromethanes of the formula CH.sub.n Cl.sub.m, where n=0 to 3 and m=4-n, with hydrogen at a temperature of 150.degree. to 250.degree. C. and under an absolute pressure of 1 to 10 bar, by means of a supported catalyst comprising an activated charcoal support with a BET surface area of more than 500 m.sup.2 /g, 0.5 to 20% by weight of copper in elemental or chemically bonded form and 0.01 to 1.0% by weight of rhodium or palladium in elemental or chemically bonded form, and with 0.1 to 10.0% by weight of a water-soluble phosphonium halide.

Process for the hydrogenation of chloromethanes

A catalyst system for the preparation of 1,2-dichloroethane by reacting ethylene and chlorine in a solvent, if desired, in the presence of an inhibitor for reducing the formation of byproducts. The catalyst system comprises a phenolate/chlorine complex. The invention also relates to a process for the chlorination of ethylene using indicated catalyst system.

Catalyst system and use for the preparation of 1,2-dichloroethane

A carrier catalyst containing copper and alkali ions on an annular carrier of surface-active material is defined by the dimensions of the carrier body and the porosity of the finished catalyst. Its total pore volume is 0.6-1.0 ml/g, pores smaller than 4 nm diameter are not present, pores of 8-20 nm diameter constitute at least 80% of the total pore volume and the remainder consists of macropores with a diameter greater than 20 nm (i.e., up to 200 nanometers). The catalyst is suitable for the production of 1,2-dichloroethane by means of the oxychlorination of ethylene.

Cylindrically formed catalyst for the oxychlorination of ethylene

The use of hitherto known supported catalysts in chlorination processes and oxychlorination processes leads to high pressure drops and to the formation of hot spot temperatures in the reactor. When honeycomb monolithic catalyst supports provided with a multiplicity of channels open at both ends and parallel to the longitudinal axis are used, both the heat dissipation is improved and the pressure drops across the reactor are lowered drastically. This leads ultimately to an increase in the selectivity of the reaction and to a minimization of the combustion rate.

Chlorination reactions and oxychlorination reactions in the presence of

The invention relates to a process for purifying unreacted 1,2-dichloroethane from a 1,2-dichloroethane pyrolysis process by chlorinating the benzene produced as a by-product and removing the chlorination products by distillation.

Process for purifying unreacted 1,2-dichloroethane from a

The invention is a multi-stage process for purifying hydrogen chloride containing acetylene and ethylene, from pyrolysis of 1,2-dichloroethane to provide highly pure hydrogen chloride for use in the preparation of silicon compounds. In the first stage, unsaturated by-products are chlorinated by reaction with an excess of chlorine gas. In the second stage, the unreacted chlorine gas remaining in the hydrogen chloride is reacted with an excess of defined olefins or chloroolefins and the hydrogen chloride is separated from the chlorination products and the excess olefins or chloroolefins by low-temperature rectification under pressure.

Process for purifying hydrogen chloride from pyrolysis of

In a process for the purification of hydrogen chloride from the pyrolysis of 1,2-dichloroethane, optionally after a preceding step of acetylene removal by selective hydrogenation under specific conditions followed by rectification of the resulting mixture to obtain hydrogen chloride containing at most 5 ppm of unsaturated hydrocarbons and at most 5 ppm of chlorinated hydrocarbons.

Process for purification of HCl from pyrolysis of EDC

In a method of treating the reaction product of pyrolysis of 1,2-dichloroethane to form vinyl chloride and hydrogen chloride with multiple stage cooling and distillation separation of the reaction product and recycle of unreacted 1,2-dichloroethane to the pyrolysis step, the improvement comprising direct cooling of the reaction product immediately after leaving the pyrolysis step, within 1 sec from a temperature range of 480.degree. to 540.degree. C. down to 150.degree. to 250.degree. C., charging the cooled product into a quench column, recovering the vapors from the head of the quench column and indirectly cooling the same by heat exchange to at least its condensation point, the heat exchange media being at least one member of the group consisting of (a) 1,2-dichloroethane to be fed in heated condition to the pyrolysis unit, (b) air used as combustion air to fire the pyrolysis zone, (c) the sump of the hydrogen chloride column as defined above, (d) liquid hydrogene chloride to be evaporated and, (e) water, to dissipate heat not used within the measures according to the present invention.

Heat recovery in production of vinyl chloride by pyrolysis of

An improved method of producing vinyl chloride by pyrolysis of purified 1,2-dichloroethane at temperatures from 480.degree. C. to 540.degree. C. at a pressure of 10 to 36 bar absolute with partial utilization of the heat content of the flue gases from the pyrolysis furnace firing to preheat liquid 1,2-dichloroethane almost to its boiling temperature utilizing the flue gas waste heat to generate steam, cool the pyrolysis gas mixture in several stages and separate the hydrogen chloride from the pyrolysis gas mix in a hydrogen chloride column as well as separate vinyl chloride from the pyrolysis gas mix in a vinyl chloride monomer column.

Vinyl chloride production

In a process for preparation of 1,2-dichloroethane by chlorination of ethylene-containing reaction vent gases from the oxychlorination of ethylene in the presence of a catalyst carrier impregnated with metal compounds wherein the waste from the oxychlorination stage are chlorinated, the improvement comprising preheating the ethylene-containing waste gases to at least 50.degree. C. and then chlorinating the ethylene at 100.degree. to 300.degree. C. at a pressure of 1 to 7 bar with a space velocity of 100 to 5000 h.sup.-1 related to standard conditions in the presence of at least one metal compound selected from the group consisting of chlorides and oxides of manganese, nickel and cobalt supported on a catalyst carrier with reduced formation of oxychlorinated by-products.

Process for oxychlorination of ethylene

An improved process for the preparation of vinyl chloride from 1,2-dichloroethane (EDC) wherein 0.10 to 0.15 % by weight of carbon tetrachloride based on EDC, is used as a cracking promoter and the CHCl.sub.3 content is limited to less than 200 ppm. Before being fed to the cracking zone, the EDC is brought almost to the boiling point at 15 to 31 bar and then expanded to 10 to 16 bar with flashing EDC vapors and the fraction which has remained liquid is vaporized externally, and the combined EDC gas streams are heated, after being fed into the cracking furnaces, so that the energy required for cracking is already supplied in the first 75 to 85% of the reaction zone, whereby a conversion of 60 to 70% is obtained at residence time from 10 to 25 seconds and the exit temperature from the reaction zone is 485.degree. to 510.degree. C.

Process for thermal cracking of 1,2-dichloroethane to form vinyl chloride

In a method of recovering heat from flue gas resulting from the combustion of chlorinated organic compounds at 900.degree. to 1300.degree. C. at a pressure of 0.9 to 1.5 bar absolute whereby the flue gas is cooled with the recovery of heat and hydrogen chloride is processed, the improvement comprising (a) cooling the flue gas in a first step to a temperature of 250.degree. to 350.degree. C. with a contact time of 0.05 to 0.15 seconds, (b) cooling the flue gas in a second step to a minimum of 140.degree. C. with a contact time of 1.3 to 2.0 seconds, the cooling medium in both stages being water flowing at an initial temperature of 100.degree. to 140.degree. C. in step (b) counter to the flue gas flow direction and added to cooling stage (a) at a temperature of 200.degree. to 220.degree. C. and (c) cooling the flue gas in a third stage to its dew point and scrubbing it with water to recover the hydrogen chloride therein in solution.

Novel heat recovery process

A process of upgrading hydrogen chloride which contains chlorine, iron-III-chloride, acetylene and/or ethylene, for use in an oxichlorination process, wherein water in a gaseous state is added to the hydrogen chloride at temperatures between 120.degree. and 180.degree. C. within a time period of maximally 0.9 seconds after the acetylene and/or ethylene is present in the hydrogen chloride, together with chlorine and iron-III-chloride.

Process for upgrading hydrogen chloride containing chlorine,

A process for the work-up of chlorination residues by dissolving the same at temperatures between 100.degree. and 180.degree. C. in chlorine- and oxygen-containing hydrocarbons having a ratio by weight of hydrogen to chlorine of 0.028-0.06:1, a ratio by weight of oxygen:carbon of 0.0038-0.0089:1, and an atomic ratio of carbon:hydrogen of 1:1.1-1.9 and/or in hydrocarbons, boiling between 160.degree. and 380.degree. C. at one bar abs. and having an atomic ratio carbon:hydrogen of 1:1.85-2.0 so as to obtain a liquid preparation having a ratio by weight of hydrogen:chlorine of 0.028-0.05:1.

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Haiming, Germany

Ludwig Schmidhammer