This invention relates to a method for producing chlorine in a high yield through a hydrogen chloride oxidation reaction and more specifically, this invention is characterized in that chlorine is produced in a high yield by subjecting hydrogen chloride to an oxidation reaction in a mixed gas containing carbon oxide.

This invention relates to a method for producing chlorine in a high yield through a hydrogen chloride oxidation reaction and more specifically, this invention is characterized in that chlorine is produced in a high yield by subjecting hydrogen chloride to an oxidation reaction in a mixed gas containing carbon oxide.

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).

A process of producing chlorine gas by catalytic oxidation of hydrogen chloride including: incorporating an oxidizing agent such as ozone, hydrogen peroxide solution etc. into a gas stream of hydrogen chloride containing impurities, conducting oxidation pretreatment of the gas stream under the action of ultrasonic wave, such that the impurities contained in the gas stream are oxidized; where the gas stream obtained after the oxidation pretreatment is allowed to pass through a separating device, the oxidized impurities in the form of liquid and/or the oxidized impurities in the form of solid are removed from the gas stream so as to obtain a purified gas stream of hydrogen chloride, and thereafter the purified gas stream of hydrogen chloride is well mixed with a gas stream containing molecular oxygen, the resultant gas mixture is preheated to a reaction temperature, and then catalytically oxidized to produce chlorine gas.

A process of producing chlorine gas by catalytic oxidation of hydrogen chloride including: incorporating an oxidizing agent such as ozone, hydrogen peroxide solution etc. into a gas stream of hydrogen chloride containing impurities, conducting oxidation pretreatment of the gas stream under the action of ultrasonic wave, such that the impurities contained in the gas stream are oxidized; where the gas stream obtained after the oxidation pretreatment is allowed to pass through a separating device, the oxidized impurities in the form of liquid and/or the oxidized impurities in the form of solid are removed from the gas stream so as to obtain a purified gas stream of hydrogen chloride, and thereafter the purified gas stream of hydrogen chloride is well mixed with a gas stream containing molecular oxygen, the resultant gas mixture is preheated to a reaction temperature, and then catalytically oxidized to produce chlorine gas.

The invention relates to a process for preparation of chlorine from hydrogen chloride comprising circulating a liquid melt comprising copper ions Cu.sup.n+ with n being a number in the range from 1 to 2, alkali cations and chloride ions Cl in a reactor system comprising three bubble lift reactors I, II and III, each comprising a reaction zone i, ii and iii respectively, wherein: ?(a) in the reaction zone i of the first bubble lift reactor I, a liquid melt comprising copper ions Cu.sup.n+, alkali cations and chloride ions Cl is contacted with oxygen at a temperature in the range from 395 to 405? C. so that the molar ratio Cu.sup.n+:Cu.sup.+ in the liquid melt increases, obtaining a liquid melt having an increased molar ratio Cu.sup.n+:Cu.sup.+ ?(b) the liquid melt obtained in (a) is circulated to the reaction zone ii in the second bubble lift reactor II, where the liquid melt is contacted with hydrogen chloride at a temperature in the range from 395 to 405? C. so that water is formed, obtaining a liquid melt being enriched in chloride anions (CI-) compared to the liquid melt obtained according to (a); ?(c) circulating the liquid melt obtained in (b) to the reaction zone iii in the third bubble lift reactor III, which is operated at a temperature in the range from 420 to 430? C. so that chlorine (Cl.sub.2) is formed, wherein Cl.sub.2 is removed from the reaction zone iii and the third bubble lift reactor III respectively in gaseous form, leaving a liquid melt depleted of Cl-compared to the liquid melt obtained according to (b). The invention further relates to a reactor system comprising three bubble lift reactors I, II and III.

The invention relates to a process for preparation of chlorine from hydrogen chloride comprising circulating a liquid melt comprising copper ions Cu.sup.n+ with n being a number in the range from 1 to 2, alkali cations and chloride ions Cl in a reactor system comprising three bubble lift reactors I, II and III, each comprising a reaction zone i, ii and iii respectively, wherein: ?(a) in the reaction zone i of the first bubble lift reactor I, a liquid melt comprising copper ions Cu.sup.n+, alkali cations and chloride ions Cl is contacted with oxygen at a temperature in the range from 395 to 405? C. so that the molar ratio Cu.sup.n+:Cu.sup.+ in the liquid melt increases, obtaining a liquid melt having an increased molar ratio Cu.sup.n+:Cu.sup.+ ?(b) the liquid melt obtained in (a) is circulated to the reaction zone ii in the second bubble lift reactor II, where the liquid melt is contacted with hydrogen chloride at a temperature in the range from 395 to 405? C. so that water is formed, obtaining a liquid melt being enriched in chloride anions (CI-) compared to the liquid melt obtained according to (a); ?(c) circulating the liquid melt obtained in (b) to the reaction zone iii in the third bubble lift reactor III, which is operated at a temperature in the range from 420 to 430? C. so that chlorine (Cl.sub.2) is formed, wherein Cl.sub.2 is removed from the reaction zone iii and the third bubble lift reactor III respectively in gaseous form, leaving a liquid melt depleted of Cl-compared to the liquid melt obtained according to (b). The invention further relates to a reactor system comprising three bubble lift reactors I, II and III.

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

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.