CN1269726C - Process for preparing chlorine gas - Google Patents
Process for preparing chlorine gas Download PDFInfo
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- CN1269726C CN1269726C CN 98115029 CN98115029A CN1269726C CN 1269726 C CN1269726 C CN 1269726C CN 98115029 CN98115029 CN 98115029 CN 98115029 A CN98115029 A CN 98115029A CN 1269726 C CN1269726 C CN 1269726C
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- hydrogenchloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
- C01B7/04—Preparation of chlorine from hydrogen chloride
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Abstract
The present invention relates to a chlorine production method which comprises the oxidation of hydrogen chlorine in a composite gas containing hydrogen chlorine and impurities as a raw material, using oxygen, said method comprising an absorption step, a washing step and an oxidation step.
Description
The present invention relates to a kind of method for preparing chlorine.More particularly, the present invention relates to a kind ofly contain hydrogenchloride and impurity prepare chlorine as the hydrogenchloride in the mixed gas of raw material method with the oxygen oxidation, this raw material is divided into and contains hydrogenchloride and water as the solution of main component and the impurity gas as main component in this method, be to be undertaken by the hydrogen chloride absorption in the raw material is entered in water or the undersaturated hydrochloric acid, the component that discharges from solution generates and contains the gas of hydrogenchloride as main component, and generate chlorine with oxygen oxidation chlorination hydrogen, this method generates chlorine by the stable and high place of production of catalyzer that employing has stabilizing active, it can be simplified or eliminate the chlorine of preparing, unreacted oxygen and the various complex separations that is contained in the impurity in the former hydrogen chloride gas, therefore, from the cost of catalyzer, the aspect of the cost of equipment and the cost of processing all is very useful.
As everyone knows, the chlorine by the oxidation of hydrogen chloride preparation is commonly used for vinylchlorid, the raw material of phosgene etc.For example, by preparing in the method for chlorine, it has been generally acknowledged that the copper containing catalyst that is called as Deacon catalyst has good activity this with molecular oxygen catalysis oxidation chlorination hydrogen.Recommended manyly to contain cupric chloride, Repone K and as the catalyzer of ternary various additional compounds.Also the oxide compound of chromium or its compound are adopted in suggestion, or the oxide compound of ruthenium or its compound replace Deacon catalyst as catalyzer.When making raw material, adopt pyrolysis or the phosgenation of combustion reactions, organic compound etc. or the by product of chlorization of chlorine-containing compound usually, but they contain impurity owing to the method for front with hydrogenchloride.For example, therein the hydrogenchloride that produces of the isocyanate (pentyl ester) that reacts of amine photoreactive gas contain carbon monoxide, carbon oxysulfide, such as neighbour-dichlorobenzene, impurity such as the organic compound that mono chloro benzene is such etc. and nitrogen.Yet problem is the deactivation that the impurity in these hydrogenchloride can cause catalyzer, and can to send out dirty smelly for test tube in the separating step of the gas that forms in reaction, and assembles etc. being used for the round-robin unreacting oxygen.
For example, JP-A-62-270404 discloses the method that reduces carbon monoxide content, a kind of method is that burning carbon monoxide generation carbonic acid gas in the presence of the palladium catalyst that is carried in aluminum oxide is being arranged, a kind of method be in the waste gas hydrogenchloride by liquefaction and evaporate separated with the gas in supplying raw materials, a kind of method is to use the Cupric Chloride Solution scrubbing exhaust gas, can make the catalyzer deactivation and increase the vaporization losses of the chromium component in the catalyzer because be contained in as a large amount of carbon monoxide in the hydrogenchloride of raw material.
Again, JP-A-63-45102 discloses the method that reduces organic compound content, comprising liquefaction-distillment, with the higher solvent wash of boiling degree, low ternperature separation process or use sorbent material, because using the hydrogenchloride contain organic compound to be used for oxidizing reaction as raw material can cause the chlorination of said organic compound or part chlorination and form polychloride, polychloride is deposited in the surface of catalyzer, and the problem that the result causes is: catalyzer deactivation and form in the step of gas test tube at separating reaction to send out dirty smelly.
In addition, in all catalyzed reactions, the sulfide frequent is the surperficial of catalyzer and make the catalyzer deactivation.Yet the way known to also not having can be removed the sulfide in the de-chlorine hydride effectively.
In addition, the transformation efficiency of also knowing hydrogen chloride oxidation reaction is subjected to the restriction of chemical equilibrium and when the chemistry amount with hydrogenchloride of adding was the benchmark excess of oxygen, this was reflected under such condition and carries out usually.In this case, unreacted oxygen after separating from chlorine loops back reaction.If do not have contaminated words of active volatile impunty resemble nitrogen, they are difficult to separate with oxygen and to accumulate in the system with higher concentration by circulation, the problem that causes thus is: reduced the relative concentration of hydrogenchloride in the reaction vessel and oxygen and reduced the speed of reaction.Therefore, at the chlorine after separating that comes out from system, need to clean and contain the portion gas of unreacted oxygen as main component, but this has just caused other problem: the chlorine of valuable oxygen and association is dropped and runs off.
Under these circumstances, a kind ofly contain hydrogenchloride and impurity with dioxygen oxidation and prepare the chlorine method as the hydrogenchloride in the mixed gas of raw material and solve this problem by provided by the invention, activity stabilized and high productivity prepares chlorine to this method by stable catalyst, can simplify or eliminate the chlorine of preparing, unreacted oxygen and the various complex separations that is contained in the impurity in the former hydrogen chloride gas, therefore, from the cost of catalyzer, the aspect of the cost of equipment and the cost of processing all is very useful.
In other words, the present invention relates to a kind ofly prepare the chlorine method with the oxygen oxidation as the hydrogenchloride that contains in hydrogenchloride and the impurity mixed gas of raw material, wherein said method may further comprise the steps:
Absorption step: this step is with the hydrogen chloride absorption in raw material in water or in the undersaturated hydrochloric acid, forms to contain hydrogenchloride and water as the solution of main component with contain the gas of impurity as main component;
Extraction step: this step is to extract component from the solution that obtains in absorption step, produces to contain the gas of hydrogenchloride as main component;
Oxidation step: the hydrogen chloride in gas that this step obtains in extraction step with dioxygen oxidation is to generate chlorine.
Fig. 1 is the schema of expression embodiment of the present invention; With
Fig. 2 is the schema of expression embodiment of the present invention;
The mist that contains hydrogen chloride and impurity can be contain hydrogen chloride and in chlorine-containing compound pyrolysis or combustion reaction, or the phosgenation of organic compound or chlorination, any mist that the burning in combustion furnace etc. produce. The mist that contains hydrogen chloride and impurity can be 10 % (volume) or higher with containing hydrogen cloride concentration, and preferred concentration is 50% (volume) or higher and more preferably 80% (volume) or higher gas. When the concentration of hydrogen chloride is lower than 10% (volume), be difficult to suppress the loss of hydrogen chloride, impurity is removed in absorption step with lower level simultaneously.
The impurity that is contained in the hydrogen chloride comprises such as neighbour-dichloro-benzenes, the chlorination aromatic hydrocarbon that monochloro-benzene etc. are such, the aromatic hydrocarbon that toluene, benzene etc. are such, resemble vinyl chloride, 1, such chlorohydrocarbons such as 2-dichloroethanes, chloromethane, chloroethanes, the hydrocarbon that weevil alkane, acetylene, ethene, propylene etc. are such and resemble such inorganic gas such as nitrogen, argon gas, carbon dioxide, carbon monoxide, phosgene, hydrogen, carbonyl sulfide.
In the present invention, impurity is by removing selectively in absorbing hydrogen chloride entry or the undersaturated hydrochloric acid. In the middle of them, the inorganic gas that can effectively remove has carbonyl sulfide, carbon monoxide, carbon dioxide, phosgene, hydrogen, nitrogen, argon gas etc., and they are difficult to be dissolved in the hydrochloric acid. The concentration that is used for the unsaturated hydrochloric acid of absorption step can be any concentration that is lower than saturated concentration under the temperature of carrying out absorption step and pressure, preferred 0-25% (weight). Preferred 0 ℃-150 ℃ of the temperature that absorbs, more preferably 35 ℃-100 ℃, and the preferred 0.05MPa-2MPa of pressure that absorbs, more preferably 0.1MPa-1MPa.
Because the absorption of hydrogen chloride can be carried out under lower temperature and pressure, acid resistance material at a low price can be used for this operation. In addition, the feature of this operation is the compound that can remove more selectively resemble the carbonyl sulfide, and owing to the boiling point of its boiling point close to hydrogen chloride, they are difficult to remove up hill and dale by the absorption of liquefaction-distillation or hydrogen chloride.
In the present invention, with the preparation of hydrogen chloride chlorine that absorbs that hydrogen chloride in entry or the undersaturated hydrochloric acid discharges and come oxidation to obtain with oxygen. When the hydrogen chloride that extraction is obtained is used for preparing chlorine by dioxygen oxidation, make moisture in the gas and hydrogen chloride condensed reduce moisture in the gas thereby extract gas by cooling, the gas available oxygen oxidation of not condensing then prepares chlorine. Moreover, by cooling extract extraction gas that gas obtains or not noncondensing gas can contact with the concentrated sulfuric acid etc., remove moisture, prepare chlorine with dioxygen oxidation then.
The preferred 0.03MPa-1MPa of pressure that extracts, more preferably 0.1MPa-0.5MPa.To the concentration of the hydrochloric acid in bottoms without limits, as long as its is higher than concentration of hydrochloric acid of the maximum azeotrope azeotropic mixture of hydrogenchloride and water under operation pressure, be lower than the concentration of the original solution hydrogenchloride that is used for extracting.Enter extraction gas in order to reclaim hydrogenchloride as much as possible, preferably its concentration approaches the hydrogen cloride concentration of maximum azeotrope azeotropic mixture.Be preferably 95% (volume) or bigger by the hydrogen chloride in gas concentration (except the water) that extract to obtain, more preferably 98% (volume) or bigger, preferred especially 99% (volume) or bigger.The structure of extraction element can comprise that independent being used to provides the heating unit that extracts institute's heat requirement.Yet in order to reclaim greater amount at the raw material hydrogenchloride that is used for extracting, preferably the concentration of hydrochloric acid is being higher than in the scope of maximum azeotrope azeotropic mixture low as much as possible under operating pressure in bottoms.On the contrary, when the water-content in the extraction gas that is obtained is low, can reduce operation energy consumption, when gas carried out drying before reaction, the vitriolic amount can reduce.Therefore, preferred heating unit (reboiler) is to have one or more theoretical trays, the tower of preferred 3-9 theoretical tray, and the difference of extracting like this between the concentration of the concentration of the hydrogenchloride in the gas and the hydrogenchloride in the bottoms becomes greatly.
Because hydrogenchloride and water form the maximum azeotrope azeotropic mixture in extraction step, hydrogenchloride is deposited in the solution after extracting.But, because this undersaturated hydrochloric acid can be used as sorbent circulation to as the step that is used for absorbing hydrogen chloride of step formerly, absorb and the hydrogenchloride of extraction step loss very little.
When the theoretical chemistry metering mol ratio of oxygen and hydrogenchloride is 1/4, know that reaction process is more effective when the amount that adds oxygen surpasses stoichiometry (is benchmark with hydrogenchloride), this is because hydrogen chloride oxidation reaction is a balanced reaction.For this reason, common every mole hydrogenchloride uses the oxygen of 1/4-1 mole.Unreacted oxygen is separated with chlorine and be recycled in the reaction usually.In the present invention, because resembling such indifferent gas physical efficiencys such as nitrogen, argon gas, hydrogen, carbonic acid gas removes from the hydrogenchloride that is used for oxidizing reaction, carbon monoxide and organic compound also can be removed from the hydrogenchloride that is used for oxidizing reaction, just do not resemble the such gas of carbonic acid gas that forms by burning carbon monoxide and organic compound and produce in oxidation reaction process.Therefore, when the stoichiometry (is benchmark with hydrogenchloride) of oxygen in the oxidizing reaction is excessive, from reactant gases with hydrochloric acid isolated in form unreacted hydrogen chloride with after generating water, in gas, except oxygen and chlorine, almost do not have other material to become impurity, therefore compare separating and circulate and to carry out easily of unreacting oxygen with conventional art.
In the present invention, the heat of the solution that absorbing hydrogen chloride produces can extract the thermal source of preheating effectively as raw material before release hydrogenchloride comes out from solution, and also can reclaim heat from bottoms after extracting.
For the catalyzer that is used for oxidizing reaction in the present invention, any catalyzer in the available known catalyzer of method for preparing chlorine by oxidation chlorination hydrogen.The example of this class catalyzer comprises and contains cupric chloride, Repone K and as the catalyzer of ternary various additional compounds, contain the catalyzer of chromic oxide as main component, or contains ruthenium oxide as catalyzer of main component etc.In the middle of them, preferably contain the catalyzer of ruthenium oxide as main component.
Said oxidation system comprises flow systems such as resembling fixed bed, fluidized-bed.
The temperature of reaction is generally 100 ℃-500 ℃, and more preferably 200 ℃-400 ℃, the pressure of reaction is generally 0.1MPa-5MPa.
The preferred embodiment of the inventive method will be described with reference to appended schema.
Fig. 1 represents schema 1: water or undersaturated hydrochloric acid (b) absorb handles the mixed gas that contains hydrogenchloride and impurity (a).Be insoluble in that impurity in the hydrochloric acid is removed from the top of resorber and obtain hydrochloric acid (c) from its bottom.Discharge the hydrogenchloride in institute's hydrochloric acid that obtains (c), from cat head acquisition hydrogenchloride (d).Prepare chlorine by the hydrogenchloride that oxidation obtained.The part or all of unsaturated hydrochloric acid (e) that obtains at the bottom of the tower in extraction step is used as the unsaturated hydrochloric acid (b) the hydrogen chloride absorption step.
Fig. 2 represents schema 2: prepare chlorine with the oxygen oxidation by removing with the hydrogenchloride that moisture was obtained (f) in the hydrogenchloride that mode was obtained (d) that is similar to Fig. 1.
The invention provides a kind of method for preparing chlorine with dioxygen oxidation as the hydrogenchloride in the mixed gas that contains hydrogenchloride and impurity of raw material, this method can stably prepare chlorine with high productivity by the stabilizing active of catalyzer, can simplify or eliminate the chlorine of preparing, unreacted oxygen and the various complex separations step that is contained in the impurity in the former hydrogen chloride gas, therefore, the viewpoint from the cost of the cost of the cost of catalyzer, equipment and processing all is very useful.
Below, absorption step and extraction step are to estimate by calculating, oxidation step is a result of experiment.
Embodiment 1
Absorption step: the concentration that the mixed gas that contains 85% (volume) hydrogenchloride and 15% (volume) nitrogen is absorbed into 3.75 times (weight) of gas gross weight is in the hydrochloric acid of situation of 20% (weight), is that 0.15MPa and column bottom temperature are that cooling is the hydrochloric acid of 35% (weight) to obtain concentration under 30 ℃ the situation at the tower top pressure on absorption tower simultaneously.
Extraction step: the concentration that will obtain in absorption step is that the hydrochloric acid of 35% (weight) feeds continuously from cat head and has 5 theoretical stages, and cat head has the extraction column that reboiler is arranged at the bottom of condenser and the tower.Extraction column operation is to be 0.101MPa at tower top pressure, and the temperature of condensator outlet place gas is that the temperature of 40 ℃ and tower bottom are to operate under 109 ℃ the condition, obtains to contain the gas of moisture of the hydrogenchloride and 1.1% (volume) of 98.9% (volume) from cat head.The sulfuric acid of this gas and 98% (weight) contacts removes moisture to obtain the hydrogenchloride of＞99.5% (volume).
Oxidation step: reaction uses the catalyzer by following method preparation to carry out.The metal Ru catalyst that is carried on the spherical tio2 that diameter is 1-2mm (being produced by N.E.Chemcat) of 5% (weight) is flooded up to catalyst surface by till moistening, then with the air drying of catalyzer at 60 ℃ with potassium chloride solution.It is 1: 1 that the calculated amount of regulating Repone K makes the mol ratio of itself and ruthenium atom.Then with this catalyzer 60 ℃ air drying 4 hours, heating is 1 hour to 350 ℃ under the temperature of air at room temperature, and same temperature lower calcination 3 hours to obtain globular solids.The solid that is obtained is handled and filtering catalyst with pure water.Till the silver nitrate aqueous solution that this step repeats to add 0.2mol/l up to filtrate 5 times does not form white casse in the time more than 5 hours altogether.Then with the solid that obtained 60 ℃ air drying 4 hours to obtain the ruthenium oxide catalysts on the titanium dioxide of loading on of 6.6% (weight).At internal diameter the ruthenium oxide catalysts on the titanium dioxide of loading on of 6.6% (weight) that 12.2g obtained of packing in the glass reaction tube of 12mm, with salt bath (saltpetre: SODIUMNITRATE=1: 1) from indirect heating to 330 ℃.With the speed of 200NmL/min feed in absorption step, obtained＞hydrogenchloride of 99.5% (volume), with the speed aerating oxygen of 100NmL/min.Because reaction heat, the temperature distribution of catalyst bed becomes 328 ℃-350 ℃.
Gas sample in the exit is passed in the KI solution of 30% (weight).The water of the chlorine that is produced, unreacted hydrogen chloride and generation is absorbed in the KI solution, and the amount of the chlorine of generation and the amount of unreacted hydrogen chloride are measured with iodometry and neutralisation respectively.
According to following formula, the activity of the generation chlorine of resulting unit weight catalyzer is 2.65 * 10
-4The mol/ming catalyzer.Remaining gas after the chlorine that separation is produced, the velocity of flow of the water of unreacted hydrogen chloride and generation is 64NmL/min, oxygen composition＞99% (volume).The velocity of flow of survival gas is measured by gas meter.Analyze this composition by vapor-phase chromatography.
The activity (mol/ming catalyzer) of the chlorine that the unit weight catalyzer produces
The weight (g) of amount (the mol/min)/catalyzer of the chlorine that=exit unit time is produced
The comparative example 1
Except feeding with the speed of 200NmL/min, the mixed gas of the nitrogen of the hydrogenchloride and 15% (volume) that will contain 85% (volume) omits the operation that absorption step and extraction step repeat embodiment 1 oxidation step.Because reaction heat, the temperature distribution of catalyst bed becomes 327 ℃-348 ℃.The activity of the chlorine that the unit weight catalyzer produces is 2.52 * 10
-4The mol/min.g catalyzer.The flow velocity that separates the water of chlorine survival gas, unreacted hydrogen chloride and the generation afterwards that produces is 99NmL/min, and oxygen is 68% (volume) in the composition, and nitrogen is 35% (volume).
Table 1
| Embodiment 1 | The comparative example 1 | |
| Reaction conditions hydrogenchloride, (% volume), (NmL/min) oxygen, (NmL/min) outside salt bath, (℃) activity of the chlorine that produces of reaction result 1)Survival gas (NmL/min) (% volume) | ＞99.5 200 100 330 2.65 64 oxygen＞99 | 85 200 100 330 2.52 99 oxygen/nitrogen 68/35 |
1)Unit: mol/min.g catalyzer (* 10
-4)
Absorption step: the concentration that the mixed gas that contains the nitrogen of hydrogenchloride, 9.5% (volume) of 90.2% (volume) and 0.3% carbon oxysulfide is absorbed in 3.96 times (weight) of gas gross weight is in the hydrochloric acid of 20% (weight), and is that 0.15MPa and column bottom temperature are that cooling is the hydrochloric acid of 35% (weight) to obtain concentration under 30 ℃ the condition at the cat head pressure on absorption tower.
Extraction step: the concentration that will obtain in absorption step is that the hydrochloric acid of 35% (weight) is continuously from having 5 theoretical stages, condenser being arranged and have the cat head of the extraction column of reboiler to feed at the bottom of tower at cat head.The operation of extraction column is to be 0.101MPa at tower top pressure, the temperature of condensator outlet place gas is that the temperature of 40 ℃ and tower bottom are to carry out under 109 ℃ the condition, with the gas of the moisture of the hydrogenchloride and 1.1% (volume) that obtains to contain 98.9% (volume) from cat head.The sulfuric acid of this gas and 98% (weight) contacts removes moisture to obtain the hydrogenchloride of＞99.5% (volume).
Oxidation step: be the ruthenium oxide catalysts on the titanium dioxide of loading on of 6.6% (weight) that 3.8g obtains in similarly to Example 1 mode of packing in the glass reaction tube of 12mm at internal diameter, with its with salt bath from indirect heating to 310 ℃.To in absorption step, be obtained＞hydrogenchloride of 99.5% (volume) with the speed of 302NmL/min feed, oxygen feeds with the speed of 164NmL/min.Because reaction heat, the temperature distribution of catalyst bed becomes 319 ℃-328 ℃.
Gas sample in the exit is passed in the KI solution of 30% (weight).The water of the chlorine that is produced, unreacted hydrogen chloride and generation is absorbed in the KI solution, and the amount of the chlorine of generation and the amount of unreacted hydrogen chloride are measured with iodometry and neutralisation respectively.
The weight of the activity/catalyzer of the chlorine that is produced is 4.32 * 10
-4The mol/min.g catalyzer.
The comparative example 2
Except the mixed gas of the carbon oxysulfide of the nitrogen and 0.3% (volume) of the hydrogenchloride, 9.5% (volume) that will contain 90.2% (volume) speed with 307NmL/min feeds the oxidation step, omit the operation that absorption step and extraction step repeat embodiment 2.Because reaction heat, the temperature distribution of catalyst bed becomes 313 ℃-317 ℃.The weight of the activity/catalyzer of the chlorine that is produced is 1.07 * 10
-4The mol/min.g catalyzer.
Table 2
| | The comparative example 2 | |
| Reaction conditions hydrogenchloride, (% volume), (NmL/min) oxygen, (NmL/min) outside salt bath, (℃) activity of the chlorine that produces of reaction result 1) | ＞99.5 302 164 310 4.32 | 90.2 307 164 310 1.07 |
1)Unit: mol/min.g catalyzer (* 10
-4)
Claims (7)
1. method for preparing chlorine comprises that with dioxygen oxidation as the hydrogenchloride in the mixed gas that contains hydrogenchloride and impurity of raw material, wherein said method may further comprise the steps:
Absorption step: this step makes in the hydrogen chloride absorption entry in raw material or in the undersaturated hydrochloric acid, forms to contain hydrogenchloride and water as the solution of main component with contain the gas of impurity as main component;
Extraction step: this step is to extract component from the solution that obtains absorption step, to obtain to contain the gas of hydrogenchloride as main component; With
Oxidation step: this step is that the hydrogen chloride in gas that obtains in extraction step with dioxygen oxidation is to obtain chlorine.
2. contain hydrogenchloride as feeding oxidation step after the moisture of gas in removing gas of main component according to the process of claim 1 wherein with what in extraction step, obtain.
3. according to the process of claim 1 wherein that raw material is the raw material that contains 10% (volume) or higher hydrogenchloride.
4. according to the process of claim 1 wherein that impurities in raw materials is to be selected from a kind of in chlorinated aromatic hydrocarbons, aromatic hydrocarbons, hydrochloric ether, hydrocarbon and the inorganic gas at least.
5. according to the process of claim 1 wherein that the concentration of hydrogenchloride in the gas that extraction step obtains is 95% (volume) or higher outside dewatering.
6. according to the process of claim 1 wherein that raw material contains 50% (volume) or higher hydrogenchloride.
7. according to the process of claim 1 wherein that the hydrogenchloride in the raw material is produced by the isocyanic ester method that amine photoreactive gas wherein reacts.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14544897 | 1997-06-03 | ||
| JP145448/97 | 1997-06-03 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1201013A CN1201013A (en) | 1998-12-09 |
| CN1269726C true CN1269726C (en) | 2006-08-16 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 98115029 Expired - Lifetime CN1269726C (en) | 1997-06-03 | 1998-06-03 | Process for preparing chlorine gas |
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|---|---|
| CN (1) | CN1269726C (en) |
| BE (1) | BE1011944A4 (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10234908B4 (en) * | 2002-07-31 | 2013-10-24 | Basf Se | Process for the production of chlorine from a (chlorine) hydrocarbons containing hydrogen chloride stream |
| JP4785515B2 (en) | 2005-12-08 | 2011-10-05 | 住友化学株式会社 | Chlorine production method |
| CN101130428B (en) * | 2007-02-02 | 2010-09-01 | 清华大学 | Technique for producing chlorine by hydrogen chloride catalytic oxidation |
| DE102007020146A1 (en) * | 2007-04-26 | 2008-10-30 | Bayer Materialscience Ag | Process for the purification and oxidation of a gas containing hydrogen chloride |
| DE102007020148A1 (en) * | 2007-04-26 | 2008-10-30 | Bayer Materialscience Ag | Process for the production of chlorine from HCI |
| JP5315578B2 (en) * | 2008-12-22 | 2013-10-16 | 住友化学株式会社 | Chlorine production method |
| CN102602892B (en) * | 2012-04-11 | 2015-04-01 | 万华化学集团股份有限公司 | Method for preparing chlorine gas through catalytic oxidation of hydrogen chloride |
| PT2949622T (en) * | 2014-05-27 | 2022-05-02 | Covestro Intellectual Property Gmbh & Co Kg | Method for processing hydrogen chloride from isocyanate production |
| CN107952432B (en) * | 2017-11-29 | 2021-03-05 | 西安元创化工科技股份有限公司 | Preparation method of hydrogen chloride oxidation catalyst |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3526801A1 (en) * | 1985-07-26 | 1987-02-05 | Hoechst Ag | METHOD FOR PURIFYING HYDROGEN CHLORINE GAS |
| IL81532A (en) * | 1986-02-19 | 1990-06-10 | Mitsui Toatsu Chemicals | Process for production of chlorine |
| DE59306526D1 (en) * | 1993-04-08 | 1997-06-26 | Ct Umwelttechnik Ag | Process and device for producing hydrogen chloride from waste containing chlorine |
| WO1996039264A1 (en) * | 1995-06-05 | 1996-12-12 | Startec Ventures, Inc. | On-site manufacture of ultra-high-purity hydrochloric acid for semiconductor processing |
| DE19533659A1 (en) * | 1995-09-12 | 1997-03-13 | Basf Ag | Process for the production of chlorine from hydrogen chloride |
| US5908607A (en) * | 1996-08-08 | 1999-06-01 | Sumitomo Chemical Co., Ltd. | Process for producing chlorine |
-
1998
- 1998-06-03 BE BE9800423A patent/BE1011944A4/en not_active IP Right Cessation
- 1998-06-03 CN CN 98115029 patent/CN1269726C/en not_active Expired - Lifetime
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| BE1011944A4 (en) | 2000-03-07 |
| CN1201013A (en) | 1998-12-09 |
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