The method for producing chlorine by oxidation of hydrogen chloride with oxygen in the presence of a catalyst in a fixed-bed reactor, wherein [I] a material containing hydrogen chloride and oxygen is allowed to contact a catalyst in a temperature range of 280 to 370° C., and [II] the material containing hydrogen chloride and oxygen has an oxygen concentration of 45 to 75 vol %.

The invention relates to a method for flexibly controlling the use of hydrochloric acid having an HCl concentration of at least 10 wt %, in particular at a volume flow rate of at least 1 m.sup.3/h, obtained from a continuous chemical production process (A). In the method, purified hydrochloric acid (54) from a hydrochloric acid store (E) is optionally fed to a dispatch station (H), an HCl electrolysis station (F) and a chloralkali electrolysis station (L), which are consumption points for the hydrochloric acid, or to a neutralisation station (G) in that if one or more of said consumption points (H, F, L) is not available or if there are bottlenecks at the consumption points (H, F, L), the hydrochloric acid (54) is fed to the neutralisation station (G) and neutralised with concentrated alkali solution (55), in particular with concentrated sodium hydroxide solution, and the resulting salt solution (56) is fed either to the chloralkali process station (L) or to a disposal station (M).

The invention relates to a method for flexibly controlling the use of hydrochloric acid having an HCl concentration of at least 10 wt %, in particular at a volume flow rate of at least 1 m.sup.3/h, obtained from a continuous chemical production process (A). In the method, purified hydrochloric acid (54) from a hydrochloric acid store (E) is optionally fed to a dispatch station (H), an HCl electrolysis station (F) and a chloralkali electrolysis station (L), which are consumption points for the hydrochloric acid, or to a neutralisation station (G) in that if one or more of said consumption points (H, F, L) is not available or if there are bottlenecks at the consumption points (H, F, L), the hydrochloric acid (54) is fed to the neutralisation station (G) and neutralised with concentrated alkali solution (55), in particular with concentrated sodium hydroxide solution, and the resulting salt solution (56) is fed either to the chloralkali process station (L) or to a disposal station (M).

Disclosed is a method and a device for the continuous neutralization of hydrochloric acid at an industrial scale.

Disclosed is a method and a device for the continuous neutralization of hydrochloric acid at an industrial scale.

A method for producing phosgene directly from the directly combined raw products, preferably only dried raw products, of a combined CO.sub.2 chloride electrolysis. A first gaseous product of CO is produced from CO.sub.2 on the cathode side in at least one electrolysis cell for a CO.sub.2 conversion into CO, and a second gaseous product of at least Cl.sub.2 is produced from HCl and/or a metal chloride on the anode side, wherein phosgene is produced from the gaseous products.

A method for producing phosgene directly from the directly combined raw products, preferably only dried raw products, of a combined CO.sub.2 chloride electrolysis. A first gaseous product of CO is produced from CO.sub.2 on the cathode side in at least one electrolysis cell for a CO.sub.2 conversion into CO, and a second gaseous product of at least Cl.sub.2 is produced from HCl and/or a metal chloride on the anode side, wherein phosgene is produced from the gaseous products.

A process is described for regenerating a catalyst comprising ruthenium or ruthenium compounds, which has been poisoned by sulfur compounds, in which the catalyst, optionally at elevated temperature, is subjected to treatment with a hydrogen halide, particularly a gas stream comprising hydrogen chloride, under non-oxidative conditions and additionally, optionally at reduced temperature, to an at least two-stage oxidative post-treatment.

A catalyst for preparing chlorine gas by hydrogen chloride oxidation, comprising the following components calculated according to mass content based on the total weight of the catalyst: 0.5-20 wt % copper; 2-10 wt % manganese; 0.05-2 wt % boron; 0.01-3 wt % chromium; 0.1-10 wt % rare earth metal; 0.1-10 wt % potassium; and 3-15 wt % titanium; also comprising 0.02-1.1 wt % phosphorus; and 0.03-1.9 wt % iron; the carrier content is 55-90 wt %. In the case of a fluidized bed reactor, the present catalyst can achieve a one-way hydrogen chloride conversion rate of 80-85%. Almost all of the 0-1000 mg/kg of chlorinated benzene contained in hydrogen chloride gas can be converted into CO.sub.2 and H.sub.2O without generating polychlorinated benzene.

A catalyst for preparing chlorine gas by hydrogen chloride oxidation, comprising the following components calculated according to mass content based on the total weight of the catalyst: 0.5-20 wt % copper; 2-10 wt % manganese; 0.05-2 wt % boron; 0.01-3 wt % chromium; 0.1-10 wt % rare earth metal; 0.1-10 wt % potassium; and 3-15 wt % titanium; also comprising 0.02-1.1 wt % phosphorus; and 0.03-1.9 wt % iron; the carrier content is 55-90 wt %. In the case of a fluidized bed reactor, the present catalyst can achieve a one-way hydrogen chloride conversion rate of 80-85%. Almost all of the 0-1000 mg/kg of chlorinated benzene contained in hydrogen chloride gas can be converted into CO.sub.2 and H.sub.2O without generating polychlorinated benzene.