CN106861707A - A kind of preparation method of preparing chlorine by oxidizing hydrogen chloride catalyst - Google Patents
A kind of preparation method of preparing chlorine by oxidizing hydrogen chloride catalyst Download PDFInfo
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- CN106861707A CN106861707A CN201710071510.1A CN201710071510A CN106861707A CN 106861707 A CN106861707 A CN 106861707A CN 201710071510 A CN201710071510 A CN 201710071510A CN 106861707 A CN106861707 A CN 106861707A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/86—Chromium
- B01J23/868—Chromium copper and chromium
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
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Abstract
The invention discloses a kind of preparing chlorine by oxidizing hydrogen chloride method for preparing catalyst, complex catalyst precursor weight percentage composition is：Component A：50%~60%, component B：35%~50%, component C：1%~2%, component D：3%~5%；Wherein component A is chromium oxide；Component B is cupric oxide；Component C is K+、Na+、Cs+In one or more；Component D is silica.It is characterized in that the preparation process of heavy oil hydrogenating treatment catalyst：First, it is ground with component B using component A, mixed metal oxide powders is obtained；Then, dipping is carried out to metal oxide powder using component C to be modified；Finally, add component D, granulation, it is compressing, after roasting using HF carry out fluorination pore-creating activate, so as to obtain efficient heavy oil hydrogenating treatment catalyst.
Description
Technical field
The invention belongs to catalyst field, and in particular to a kind of preparation side of catalyst for preparing chlorine by oxidizing hydrogen chloride
Method.
Background technology
Chlorine is a kind of important Elementary Chemical Industry raw material, be widely used in polyurethane, organosilicon, chlorinated hydrocabon, epoxy resin,
The new material industry such as chlorinated rubber, chlorinated high polymers, is applied to the new energy industries such as polysilicon manufacture, is applied to disinfectant, washes
Wash the life Fine Chemicals such as agent, food additives, cosmetic additive, be applied to synthetic glycerine, chlorobenzene series, monoxone,
Benzyl chloride, PCl3Deng agricultural chemicals/pharmaceuticals industry, and it is applied to the industries such as papermaking, weaving, metallurgical and petrochemical industry.
Industrial almost all of chlorine is produced by the method for electrolytic sodium chloride aqueous solution, and the method has two very
Big problem：First it is that its power consumption reaches 2760kWh/ tons, whole chlorine industry power consumption accounts for the 5% of national total electric power consumed by industry
Left and right；Next to that produce chlorine while coproduction NaOH, due to consuming the fast development of chlorine industry recent years, led
Substantial amounts of NaOH production capacity surplus is caused.Therefore a new chlorine source is found, for the further development for consuming chlorine industry
It is a necessary condition for expansion.
On the other hand, in due to major part consumption chlorine industry, chlorine is often used as the mode of reaction medium, not into most
Whole major product facade, and reaction system is discharged in the form of by-product hydrogen chloride.And with the fast development of consumption chlorine industry, hydrogen chloride
Outlet be increasingly difficult to.The added value for being made by-product hydrochloric acid is low, transport and storage cost is high, sales difficulty, and its
20~50 times of discharge of wastewater can be also produced in follow-up use, great pressure is produced to environment；And if co-producting PVC, at present
For domestic PVC production capacities it is excessive, export volume, price and the utilization of capacity allow of no optimist always.Therefore, in current situation
Under, hydrogen chloride outlet difficulty has become constraint consumption chlorine industry further one of bottleneck problem of development.
If the hydrogen chloride of by-product can be directly prepared into chlorine, then can be realized as the closed loop circulation of " chlorine ", so that
Fundamentally solving two bottlenecks of upstream and downstream of consumption chlorine industry.Chlorine is manufactured as oxidizing hydrogen chloride using oxygen or air
Gas, is a good approach.Its stoichiometric equation can be expressed as：
The industrial process of the process can be realized at present three classes, is respectively catalytic oxidation, cyclic oxidation and oxygen
Change electrolysis.The Typical Representative of wherein cyclic oxidation is E.I.Du Pont Company, and the process sulfuric acid makes as the oxide isolation of circulation
It is catalyst with nitric acid, therefore equipment is thrown, and foot very big, complex operation, operating cost is high, very flexible.Oxidization electrolysis method can
Alleviate the unbalanced problem of chlor-alkali in current chlor-alkali industry, but its power consumption well still above 1700kWh/ tons, not
Have for the power consumption high of chlorine production, and the electrolysis of relative ion film is fundamentally solved the problems, such as, the method for oxidization electrolysis hydrochloric acid
Equipment it is more complicated, economy and operability are without advantage.Although the equipment investment of the catalytic oxidation of hydrogen chloride is larger,
According to prior art, only about 230kWh/ tons of its power consumption can be estimated, and be a chemical process for environmental protection.
In the heavy oil hydrogenating treatment catalyst reported, active component is mainly using metallic elements such as copper, chromium and rutheniums.
In the patent (CN03145889.0, publication date 2004 year 2 month 18) of SUMITOMO CHEMICAL, by infusion process, by ruthenium
Compound is carried in carrier and upper acquisition catalyst, and the weight ratio of ruthenium and carrier is 0.5-20%.Industrially, it is desirable to which catalyst has
Having activity higher and per unit weight ruthenium contained in the catalyst has activity higher.However, ruthenium is expensive,
There is certain difficulty in industrialization promotion.
Cu-series catalyst gets most of the attention because of its relatively low cost.Patent (CN200710121298.1, public affairs of Tsing-Hua University
Open the date 2008 year 2 month 20) in, catalyst includes copper, phosphorus, alkali metal, the salt of rare earth metal and/or oxide and inertia
Carrier.The catalyst is applied to fluidized-bed reactor.With the passage in reaction time under high temperature, copper catalyst surface can forming portion
Point active component aggregation, and the collision between catalyst granules may make to form bridge joint between particle, in turn result in catalyst it
Between bond, cause the specific surface area of catalyst significantly to decline so that catalyst performance decline, so as to copper system is urged under causing high temperature
Agent is gradually inactivated.
Chromium-based catalysts are functional, and in the absence of the problem of high temperature deactivation, but it is certain largely to use chromium to there is environment
Pollution.The patent (WO2015109587, July 30 2015 publication date) of ten thousand China's chemistry is used containing metal systems such as chromium, copper
Into mixed slurry, slurry spray drying is made catalyst precursor particles, and calcining obtains catalyst, turns in a fluidized bed reactor
Rate is 80-85%.The preparation method improves Tsing-Hua University's catalyst preparation process, but still only can be suitably used for fluid bed, no
Promoted beneficial to large-scale industry.
Although for many years, the catalytic oxidation of hydrogen chloride process in the world to fluid bed reaction system has carried out detailed grinding
Study carefully, but still fail to reach the condition of heavy industrialization.And the specific surface area of the catalyst being applicable in fixed bed reactors
The catalyst being applicable generally less than in the fluidized-bed reactor of homogenous quantities, therefore how to expand fixed bed reactors suitable catalyst
Specific surface area be one of committed step of catalyst preparation process.
In sum, for relating to chlorine industry, catalytic oxidation of hydrogen chloride for preparing chlorine gas is an important industrial chain link.
In order to mode realizes the heavy industrialization of this process, it is necessary to the catalyst suitable for fixed bed reactors at lower cost
Preparation method is improved.And in the middle of this, crucial challenge is that a kind of cheap, environment-friendly, high-temperature stable of research and development
The method for preparing catalyst big with specific surface area, to adapt in fixed bed reactors industrialized production the need for long-term use.
The content of the invention
The technical problems to be solved by the invention are to overcome the shortcomings of above-mentioned background technology, it is therefore an objective to provide one kind and be applied to
The catalyst of the cheap, environment-friendly of fixed bed reactors, high-temperature stable and the big chloride oxidation preparing chlorine gas of specific surface area
Preparation method.
Catalyst precursor of the invention selects chromium oxide, cupric oxide.Cupric oxide wide material sources, it is cheap, under high temperature
Catalytic effect is good, but there is certain high temperature losing issue.At the same time, single chromium oxide catalyst catalytic performance is good
It is good, but there is certain problem of environmental pollution.
On the other hand, the specific surface area of chromium oxide and copper oxide catalyst is limited so that gas and oxide interface area
It is restricted, so as to have impact on reaction velocity and conversion ratio.
The present invention constitutes composite type metallic oxide catalyst using two kinds of metal oxide compoundings, overcomes monometallic
The limitation of oxidation catalyst, after cupric and chromic oxide compounding, on the one hand reduces pollution of the chrome catalysts to environment, on the other hand
Prevent and delay copper catalyst to inactivate under the high temperature conditions.Meanwhile, impregnated using auxiliary agent, adjust catalyst performance and stabilization enhancing
Catalyst life, effectively increases the activity and stability of catalyst；By adding filling pore creating material in catalyst precursor
(silica), with HF reaction generation gases (SiF after shaping of catalyst4), while a large amount of micropores are produced in preformed catalyst,
The specific surface area of catalyst is effectively raised, so as to improve catalyst performance.Pore-creating principle is as follows：
SiO2+4HF→SiF4↑+2H2O↑
Technical scheme is as follows：
A kind of preparation method of preparing chlorine by oxidizing hydrogen chloride catalyst, described complex catalyst precursor weight percentage composition
For：Component A：50%~60%, component B：35%~50%, component C：1%~2%, component D：3%~5%, wherein component A
It is chromium oxide, component B is cupric oxide, and component C is K+、Na+、Cs+In one or more, component D be silica；Its feature exists
Prepared by following methods in catalyst：
A) by component A, uniformly mix with component B, the mass ratio of component A and component B is 2~3:1, insert in mortar and grind
15min, drying；
B) solid powder obtained by step a) is added in the aqueous solution containing component C, solid powder and aqueous solution matter
Amount is than being 1:5, it is heated to backflow, stirring reaction 2h, filtering, washing, drying, 350 DEG C of calcination process 6h；
C) granulated after adding component D well mixed material obtained by step b), compressing, the catalyst precursor exists
Under the conditions of 400 DEG C of temperature, calcination process 8h；
D) catalyst precursor is fitted into fixed bed reactors, is passed through HF and N2Gaseous mixture, gaseous mass ratio be 1~
5:1, it is gradually heating to 500 DEG C and catalyst is fluorinated；
E) after fluorination certain hour, it is changed to be passed through N2, temperature is gradually reduced, obtain preparing chlorine by oxidizing hydrogen chloride catalyst.
Described component D silica uses HF as filling pore creating material in its poration process.
The present invention has advantages below：
1. the preparing chlorine by oxidizing hydrogen chloride catalyst reaction activity height for being prepared using preparation method of the present invention.In reaction 24h
Afterwards, reaction selectivity is close to 100%, conversion ratio about 98%；
2. it is of the invention compared with existing method for preparing catalyst, the precious metal chemical complexs, price such as the ruthenium of costliness are not used
It is cheap；
3. the present invention increase effectively the specific surface area of catalyst, in fixed bed reaction by the pore-creating of silica and HF
Reaction effect is good in device；
4. catalyst precursor of the present invention is compounded using chromium oxide and cupric oxide, and adds auxiliary agent, prevents copper catalyst high
Temperature inactivation, and reduce pollution of the chrome catalysts to environment.
Specific embodiment
The present invention is described in further details with reference to embodiment.
In the present invention, preparing chlorine by oxidizing hydrogen chloride catalyst activity evaluating apparatus are common fixed-bed tube reactor, instead
The device size is answered to beCatalyst packing is entered into reactor, reaction temperature, gas is heated to
Body is by pressure-reducing valve and flowmeter rear feeding, sampling analysis after stabilization reaction.
Preparing chlorine by oxidizing hydrogen chloride catalyst activity evaluation experimental condition：300-400 DEG C of reaction temperature, hydrogen chloride and oxygen
Mol ratio/mass ratio be 1:1-2, reaction pressure normal pressure or pressure-fired.
Oxidation reactor outlet is mainly the mixture of chlorine, oxygen, hydrogen chloride and water vapour, analyzes chlorine therein and contains
The growing amount of chlorine in intervals is measured and calculates, it is possible to calculate the conversion ratio of oxidation reaction, to investigate catalyst
The affecting laws of activity and oxidation reaction condition.
According to the principle that chlorine is easily absorbed by liquor kalii iodide, in other words using the reproducibility of iodide ion, determining has oxygen
The amount of the chlorine of the property changed.When gas sample is passed through liquor kalii iodide, chlorine is absorbed, and displaces iodine, and the iodine of precipitation is again with thio
Sulfuric acid sodium standard solution is titrated, and this is iodimetric titration (or indirect iodometric processes, iodometry).
Titration process is using starch as indicator.Because HCl is highly soluble in water, so in Cl2Absorbed by KI solution
Meanwhile, HCl is also absorbed simultaneously.Titrated with hypo solution after terminating, can titrate HCl's with standard solution of sodium hydroxide
Amount, the titrimetry phenolphthalein indicator.
Concrete operation step is as follows：After system stable operation, a 20% KI solution is prepared at regular intervals
100ml, switching oxidation reactor outlet triple valve, mixed gas after reaction are passed into (100ml) liquor kalii iodide of constant volume
In, absorb 3 minutes, by absorbing liquid immigration conical flask after absorption, titrated with the sodium thiosulfate standard solution of 0.1mol/l, with
Starch makees indicator；Followed by, with phenolphthalein indicator, titrated with 0.1mol/l standard solution of sodium hydroxide unreacted
HC1。
HCl conversion ratios：
Conv%=b/ (b+d) * 100%
B represents that titration consumes Na2S2O3Solution milliliter number, ml
D represents that titration consumes NaOH solution milliliter number, ml
The present invention is described in further details with reference to embodiment.
Embodiment 1
Load a certain amount of catalyst in fixed-bed tube reactor, preparing chlorine by oxidizing hydrogen chloride catalyst precursor is pressed
Implement according to following percentage by weight：
Wherein component A is cupric oxide, and component B is chromium oxide, and component C is potassium chloride, and component D is silica.Gained chlorination
Hydroxide preparing chlorine gas catalyst is labeled as A.
Preparing chlorine by oxidizing hydrogen chloride catalyst of the invention is prepared by the following method.
A) by component A cupric oxide, uniformly mix with component B chromium oxide, insert and 15min is ground in mortar, dry；
B) metal oxide powder obtained by step a) is added to the aqueous solution containing component C potassium chloride (1mol/L)
In, metal oxide powder is 1 with aqueous solution mass ratio:5, it is heated to backflow, stirring reaction 2h, filtering, washing, drying, 350
DEG C calcination process 6h；
C) granulated after adding component D silica well mixed material obtained by step b), it is compressing, before the catalyst
Drive body under the conditions of 400 DEG C of temperature, calcination process 8h；
D) catalyst is fitted into fixed bed reactors, is passed through HF and N2Gaseous mixture, gaseous mass ratio be 1~5:1, by
500 DEG C are gradually warming up to be fluorinated catalyst；
E) after fluorination certain hour, it is changed to be passed through N2, temperature is gradually reduced, obtain preparing chlorine by oxidizing hydrogen chloride catalyst.
Embodiment 2
Preparing chlorine by oxidizing hydrogen chloride catalyst precursor of the present invention is implemented according to following percentage by weight：
Wherein component A is cupric oxide, and component B is chromium oxide, and component C is potassium chloride, and component D is silica.Gained chlorination
Hydroxide preparing chlorine gas catalyst is labeled as B.
Preparing chlorine by oxidizing hydrogen chloride catalyst of the invention is prepared by the following method.
A) by component A cupric oxide, uniformly mix with component B chromium oxide, insert and 15min is ground in mortar, dry；
B) metal oxide powder obtained by step a) is added to the aqueous solution containing component C potassium chloride (0.5mol/L)
In, metal oxide powder is 1 with aqueous solution mass ratio:5, it is heated to backflow, stirring reaction 2h, filtering, washing, drying, 350
DEG C calcination process 6h；
C) granulated after adding component D silica well mixed material obtained by step b), it is compressing, before the catalyst
Drive body under the conditions of 400 DEG C of temperature, calcination process 8h；
D) catalyst is fitted into fixed bed reactors, is passed through HF and N2Gaseous mixture, gaseous mass ratio be 1~5:1, by
500 DEG C are gradually warming up to be fluorinated catalyst；
E) after fluorination certain hour, it is changed to be passed through N2, temperature is gradually reduced, obtain preparing chlorine by oxidizing hydrogen chloride catalyst.
Comparative example 1
Preparing chlorine by oxidizing hydrogen chloride catalyst precursor of the present invention is implemented according to following percentage by weight：
Wherein component A is cupric oxide, and component B is chromium oxide, and component C is potassium chloride, and component D is silica.Gained chlorination
Hydroxide preparing chlorine gas catalyst is labeled as C.
Preparing chlorine by oxidizing hydrogen chloride catalyst preparation step of the present invention is with embodiment 1, except that being only passed through in step d
N2, it is not passed through HF.
Embodiment 3
Preparing chlorine by oxidizing hydrogen chloride catalyst precursor of the present invention is implemented according to following percentage by weight：
Wherein component A is cupric oxide, and component B is chromium oxide, and component C is potassium chloride, and component D is silica.Gained chlorination
Hydroxide preparing chlorine gas catalyst is labeled as D.
Preparing chlorine by oxidizing hydrogen chloride catalyst preparation step of the present invention with embodiment 1, except that the content of each component.
Embodiment 4
Preparing chlorine by oxidizing hydrogen chloride catalyst precursor of the present invention is implemented according to following percentage by weight：
Wherein component A is cupric oxide, and component B is chromium oxide, and component C is equimolar potassium chloride and sodium chloride, and component D is
Silica.Gained preparing chlorine by oxidizing hydrogen chloride catalyst is labeled as E.
Preparing chlorine by oxidizing hydrogen chloride catalyst preparation step of the present invention is with embodiment 1, except that component C is potassium chloride
And sodium chloride, gained preparing chlorine by oxidizing hydrogen chloride catalyst is labeled as E.
Embodiment 5
Preparing chlorine by oxidizing hydrogen chloride catalyst precursor of the present invention is implemented according to following percentage by weight：
Component A 55%
Component B 25%
Component C 20%
Wherein component A is cupric oxide；Component B is chromium oxide；Component C is equimolar potassium chloride and cesium chloride.Gained chlorine
Change hydroxide preparing chlorine gas catalyst and be labeled as F.
Preparing chlorine by oxidizing hydrogen chloride catalyst preparation step of the present invention is with embodiment 1, except that component C is tri-chlorination
Iron, gained preparing chlorine by oxidizing hydrogen chloride catalyst is labeled as F.
The application of preparing chlorine by oxidizing hydrogen chloride catalyst prepared by the inventive method
Preparing chlorine by oxidizing hydrogen chloride catalyst A, B, C, D, E, F prepared by embodiment 1~5 and comparative example 1 is loaded into
Fixed-bed tube reactor, loaded catalyst is 60mL, N2330 DEG C are heated under protection, reaction mass is entered by pressure-reducing valve
Material, feeds as the mol ratio of hydrogen chloride and oxygen is 1:1-2, the temperature in reactor is 380 DEG C, and pressure is 0.1MPa, stabilization
Reaction 24h post analysis reaction results, statistics is as shown in table 1.
The preparing chlorine by oxidizing hydrogen chloride catalyst reaction result of table 1
| Preparing chlorine by oxidizing hydrogen chloride catalyst | Conversion ratio % | Selective % |
| A | 98.2 | 100.0 |
| B | 97.1 | 99.9 |
| C | 78.3 | 99.9 |
| D | 97.6 | 100.0 |
| E | 97.5 | 99.9 |
| F | 98.4 | 100.0 |
Contrasted with comparative example 1 by embodiment 1, it can be seen that in catalyst preparation process, the catalyst A using HF pore-creating turns
Rate is higher than the catalyst C that HF pore-creating is not used.Be can be seen that by determining BET, the specific surface area of catalyst A compares catalyst C
Dramatically increase.Method for preparing catalyst of the invention can effectively improve catalyst performance.
Claims (2)
1. a kind of preparation method of preparing chlorine by oxidizing hydrogen chloride catalyst, described complex catalyst precursor weight percentage composition is：
Component A：50%~60%, component B：35%~50%, component C：1%~2%, component D：3%~5%, wherein component A are oxygen
Change chromium, component B is cupric oxide, and component C is K+、Na+、Cs+In one or more, component D be silica；It is characterized in that urging
Agent is prepared by following methods：
A) by component A, uniformly mix with component B, the mass ratio of component A and component B is 2~3:1, insert in mortar and grind
15min, drying；
B) solid powder obtained by step a) is added in the aqueous solution containing component C, solid powder and aqueous solution mass ratio
It is 1:5, it is heated to backflow, stirring reaction 2h, filtering, washing, drying, 350 DEG C of calcination process 6h；
C) granulated after adding component D well mixed material obtained by step b), compressing, the catalyst precursor is in temperature
Under the conditions of 400 DEG C, calcination process 8h；
D) catalyst precursor is fitted into fixed bed reactors, is passed through HF and N2Gaseous mixture, gaseous mass ratio be 1~5:1,
500 DEG C are gradually heating to be fluorinated catalyst；
E) after fluorination certain hour, it is changed to be passed through N2, temperature is gradually reduced, obtain preparing chlorine by oxidizing hydrogen chloride catalyst.
2. the preparation method of the preparing chlorine by oxidizing hydrogen chloride catalyst as described in right 1, it is characterised in that described component D oxygen
SiClx uses HF as filling pore creating material in its poration process.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109607478A (en) * | 2018-12-25 | 2019-04-12 | 西安近代化学研究所 | A kind of technique of step oxidation chlorination hydrogen and hydrogen fluoride gaseous mixture preparing chlorine gas |
| CN109675582A (en) * | 2018-12-25 | 2019-04-26 | 西安近代化学研究所 | A kind of preparing chlorine by oxidizing hydrogen chloride catalyst and preparation method thereof |
| CN109806864A (en) * | 2019-03-15 | 2019-05-28 | 西安近代化学研究所 | A kind of high stability catalyst of preparing chlorine by oxidizing hydrogen chloride |
| WO2021198479A1 (en) | 2020-04-03 | 2021-10-07 | Total Se | Production of light olefins via oxychlorination |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5154911A (en) * | 1989-11-02 | 1992-10-13 | University Of Southern California | Efficient method for the chemical production of chlorine and the separation of hydrogen chloride from complex mixtures |
| CN1126637A (en) * | 1994-11-14 | 1996-07-17 | 三井东压化学株式会社 | Catalysts for preparing chlorine from mydrogen chloride |
| CN1145275A (en) * | 1995-09-13 | 1997-03-19 | 西安近代化学研究所 | Catalyst for fluoreation of halogenated hydrocarbon |
| CN101070140A (en) * | 2007-06-18 | 2007-11-14 | 南京工业大学 | Process for producing chlorine by chloration hydro-oxidation and dewatering coupling |
| CN101722019A (en) * | 2008-10-17 | 2010-06-09 | 拜尔材料科学股份公司 | Catalyst and process for preparing chlorine by gas phase oxidation |
| JP2010189206A (en) * | 2009-02-16 | 2010-09-02 | Mitsui Chemicals Inc | Method for producing chlorine |
| CN103889568A (en) * | 2011-10-24 | 2014-06-25 | 拜耳知识产权有限责任公司 | Catalyst and method for producing chlorine by means of a gas-phase oxidation |
| CN105126930A (en) * | 2015-08-28 | 2015-12-09 | 烟台大学 | Preparing method of catalyst carrier and application of preparing method in hydrogen chloride catalytic oxidation |
| CN105289631A (en) * | 2015-11-25 | 2016-02-03 | 上海氯碱化工股份有限公司 | Catalyst for chlorine gas preparation through catalytic oxidation of hydrogen chloride, preparation method and applications thereof |
-
2017
- 2017-02-09 CN CN201710071510.1A patent/CN106861707B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5154911A (en) * | 1989-11-02 | 1992-10-13 | University Of Southern California | Efficient method for the chemical production of chlorine and the separation of hydrogen chloride from complex mixtures |
| CN1126637A (en) * | 1994-11-14 | 1996-07-17 | 三井东压化学株式会社 | Catalysts for preparing chlorine from mydrogen chloride |
| CN1145275A (en) * | 1995-09-13 | 1997-03-19 | 西安近代化学研究所 | Catalyst for fluoreation of halogenated hydrocarbon |
| CN101070140A (en) * | 2007-06-18 | 2007-11-14 | 南京工业大学 | Process for producing chlorine by chloration hydro-oxidation and dewatering coupling |
| CN101722019A (en) * | 2008-10-17 | 2010-06-09 | 拜尔材料科学股份公司 | Catalyst and process for preparing chlorine by gas phase oxidation |
| JP2010189206A (en) * | 2009-02-16 | 2010-09-02 | Mitsui Chemicals Inc | Method for producing chlorine |
| CN103889568A (en) * | 2011-10-24 | 2014-06-25 | 拜耳知识产权有限责任公司 | Catalyst and method for producing chlorine by means of a gas-phase oxidation |
| CN105126930A (en) * | 2015-08-28 | 2015-12-09 | 烟台大学 | Preparing method of catalyst carrier and application of preparing method in hydrogen chloride catalytic oxidation |
| CN105289631A (en) * | 2015-11-25 | 2016-02-03 | 上海氯碱化工股份有限公司 | Catalyst for chlorine gas preparation through catalytic oxidation of hydrogen chloride, preparation method and applications thereof |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109607478A (en) * | 2018-12-25 | 2019-04-12 | 西安近代化学研究所 | A kind of technique of step oxidation chlorination hydrogen and hydrogen fluoride gaseous mixture preparing chlorine gas |
| CN109675582A (en) * | 2018-12-25 | 2019-04-26 | 西安近代化学研究所 | A kind of preparing chlorine by oxidizing hydrogen chloride catalyst and preparation method thereof |
| CN109607478B (en) * | 2018-12-25 | 2022-02-22 | 西安近代化学研究所 | Process for preparing chlorine by oxidizing hydrogen chloride and hydrogen fluoride mixed gas in one step |
| CN109806864A (en) * | 2019-03-15 | 2019-05-28 | 西安近代化学研究所 | A kind of high stability catalyst of preparing chlorine by oxidizing hydrogen chloride |
| CN109806864B (en) * | 2019-03-15 | 2022-03-15 | 西安近代化学研究所 | High-stability catalyst for preparing chlorine by oxidizing hydrogen chloride |
| WO2021198479A1 (en) | 2020-04-03 | 2021-10-07 | Total Se | Production of light olefins via oxychlorination |
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| CN106861707B (en) | 2019-08-27 |
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