IE64525B1 - Method for the recovery of chlorine from hydrogen chloride by means of a transport catalyst process and equipment for carrying out this method - Google Patents
Method for the recovery of chlorine from hydrogen chloride by means of a transport catalyst process and equipment for carrying out this methodInfo
- Publication number
- IE64525B1 IE64525B1 IE62190A IE62190A IE64525B1 IE 64525 B1 IE64525 B1 IE 64525B1 IE 62190 A IE62190 A IE 62190A IE 62190 A IE62190 A IE 62190A IE 64525 B1 IE64525 B1 IE 64525B1
- Authority
- IE
- Ireland
- Prior art keywords
- chlorine
- hydrogen chloride
- gas
- chloride
- catalyst
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000003054 catalyst Substances 0.000 title claims abstract description 31
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 239000000460 chlorine Substances 0.000 title claims abstract description 29
- 229910052801 chlorine Inorganic materials 0.000 title claims abstract description 29
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 29
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 238000011084 recovery Methods 0.000 title claims description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000001301 oxygen Substances 0.000 claims abstract description 16
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 16
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 15
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 claims abstract description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 8
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 239000011780 sodium chloride Substances 0.000 claims abstract description 7
- 238000010521 absorption reaction Methods 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 26
- 239000000463 material Substances 0.000 claims description 10
- 229910001868 water Inorganic materials 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 239000006096 absorbing agent Substances 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 238000010586 diagram Methods 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 3
- 239000007800 oxidant agent Substances 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 239000012159 carrier gas Substances 0.000 claims 2
- 239000002245 particle Substances 0.000 claims 2
- 239000011148 porous material Substances 0.000 claims 2
- 239000000047 product Substances 0.000 claims 2
- 239000000243 solution Substances 0.000 claims 2
- 238000001354 calcination Methods 0.000 claims 1
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 239000004035 construction material Substances 0.000 claims 1
- 239000012467 final product Substances 0.000 claims 1
- 239000012530 fluid Substances 0.000 claims 1
- 238000005243 fluidization Methods 0.000 claims 1
- 238000009434 installation Methods 0.000 claims 1
- 239000007769 metal material Substances 0.000 claims 1
- 238000002360 preparation method Methods 0.000 claims 1
- 238000005057 refrigeration Methods 0.000 claims 1
- 239000012047 saturated solution Substances 0.000 claims 1
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical class [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 abstract description 11
- 230000003197 catalytic effect Effects 0.000 abstract description 6
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 abstract description 6
- 230000001590 oxidative effect Effects 0.000 abstract description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract description 3
- 239000005751 Copper oxide Substances 0.000 abstract description 3
- 229910000431 copper oxide Inorganic materials 0.000 abstract description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 abstract 1
- 239000011734 sodium Substances 0.000 abstract 1
- 229910052708 sodium Inorganic materials 0.000 abstract 1
- 238000007254 oxidation reaction Methods 0.000 description 11
- 230000003647 oxidation Effects 0.000 description 9
- 238000005660 chlorination reaction Methods 0.000 description 5
- 239000002184 metal Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 235000002639 sodium chloride Nutrition 0.000 description 4
- 150000002739 metals Chemical class 0.000 description 3
- 229910021592 Copper(II) chloride Inorganic materials 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 229910016505 CuCl2 + 1 Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/06—Halogens; Compounds thereof
- B01J27/08—Halides
- B01J27/10—Chlorides
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
The method comprises two stages: (1) passing a gaseous current of hydrogen chloride across a fluidized bed of copper oxides and sodium chloride deposited onto a suitable support, the reaction of the hydrogen chloride with the oxides to form a complex chloride taking place in a reactor (11); and (2) passing the chlorinated transport catalyst over a fluidized bed of transport catalyst which contains copper chloride and sodium, injecting a mixture of oxygen and nitrogen, carrying out the oxidizing reaction in a reactor (21) and liberating chlorine from the catalytic mass while the copper chloride is converted into copper oxide, extracting a continuous flow of transport catalyst which returns to the first stage. An absorption/ separation system (47) using carbon tetrachloride recovers the chlorine give off in the reactor (21).
Description
METHOD FOR THE RECOVERY OF CHLORINE FROM HYDROGEN CHLORIDE BY MEANS OF A TRANSPORT CATALYST PROCESS AND EQUIPMENT FOR CARRYING OUT THIS METHOD.
The present invention relates to a procedure for * 5 the recovery of chlorine from hydrogen chloride, using a transport catalyst. The equipment for carrying out this procedure is also referred to.
Hydrogen chloride is obtained as a by-product- in 10 many chemical processes, being recovered both in the anhydrous gaseous form and in aqueous solution. Recovery of the hydrogen chloride produced in chlorination processes is necessary for ecological and environmental reasons, but getting rid of this hydrogen chloride in an economic manner has been a very difficult task which has been studied for many years.
The procedure described in the present invention makes use of a new technology the best definition of which is that of a transport catalyst system. In the previous attempts to recover chlorine from hydrogen chloride catalytic systems formed by a metal or a group of metals on an alumina or silica support have been tried, with sufficient success but with considerable problems. Among the problems which these methods present is the extreme difficulty of separating the gases which are given off from the catalytic reactor due to the simultaneous presence in the gas current of hydrogen chloride, chlorine, water, oxygen, nitrogen and other products. In addition, it has been observed that the catalyst used has, in general, a relatively short life due to the fact that, in a chlorine atmosphere and at the * temperatures required for the reaction to proceed at an economically suitable speed, the volatility of the metals used is high.
According to the present invention there is provided a method for the recovery of chlorine from hydrogen chloride by means of a transport catalyst process, which essentially comprises two stages: - a first stage which consists in passing a gaseous current of hydrogen chloride which is anhydrous or contains water and any hydrocarbons which may be present, across a fluidized bed of copper oxides and sodium chloride, deposited on a suitable support, which are in the molar ratio 1:1, the reaction of the hydrogen chloride with the oxides taking place to form a complex chloride, according to the equation: (1) CuO + 2HC1 ---> CuCl2 + H20 at a temperature of between 100 and 300’C, maintaining the fluidized bed at a constant temperature. - a second stage which consists in passing the chlorinated transport catalyst material coming from the first stage across a fluidized bed of transport catalyst which contains from 2 to 20% copper and sodium chloride so that the fluidized bed transport catalyst is continually mixed with the chlorinated transport catalyst, injecting a mixture of oxygen and nitrogen with an oxygen content of between 99% and 10% by volume, carrying out the oxidizing reaction at a temperature to liberate chlorine from the catalytic mass while the copper chloride is converted into copper oxide, according to the equation: (2) CuCl2 + l/202 ---> CuO + Cl2 extracting from this second stage a continuous flow of transport catalyst which returns to the first stage.
The oxidizing reaction may be carried out at a temperature between 300 and 380°C.
The heat generated in the second oxidation stage may be made use of in the first chlorination stage.
The method may comprise at least two contact stages in series in the first chlorination stage between hydrogen chloride gas and the transport catalyst, and in addition two contact stages in the second oxidation stage between the gas containing oxygen and the transport catalyst which has already absorbed the hydrogen chloride, thus ensuring the total conversion of the hydrogen chloride in the first chlorination stage and more efficient utilization of the oxygen in the second oxydation stage.
Equipment to be used in a procedure according to the invention may comprise at least two independent reactors, a first chlorinating reactor where the first chlorination stage takes place and a second oxidation reactor in which the second oxidation stage takes place, wherein said first and second reactors each have a fluidized bed with a heat exchanger placed in a reactor zone where the catalyst is fluidised by the gas.
Such equipment may comprise an absorption/separation system with carbon tetrachloride or other suitable solvent, for the recovery of the chlorine from the gases emerging from the oxidation reactor.
The equipment may comprise a gas turbine and an expansion chamber for using the heat generated in the chlorinating reactor as source of the energy necessary for the gas rich in oxygen to act as a fluidizer within the oxidation reactor.
The equipment may comprise internal cyclones placed such that the dust collected in the cyclone passes directly to the tubing for the exit of the solids at the bottom of the reactors, thus minimizing the accumulation of fine dust in circulation within the reactor system.
The procedure which is shown in the present invention differs from the procedures which have already been published in that it uses a transport catalyst system. In the present technique the metals used to bring about the catalytic reaction are impregnated into a support mass, such as alumina, silica or a molecular sieve, which is suitable for use in the form of a fluidized bed. The first reaction is arranged so that it takes place in a sequence of stages which can be summarized by saying that they give rise to the following final result: (1) CuO + 2 HC1-^CuCl2 + H20 Stage 1: The gaseous current of hydrogen chloride, which is anhydrous or contains water and the hydrocarbons which may be present as impurities, crosses a fluidized bed of copper oxides and sodium chloride, deposited on a suitable support, which are in the molar ratio 1:1. The reaction takes place at a temperature of between 100 and 300°C. The hydrogen chloride reacts with the oxides to form a complex chloride, in accordance with the theoretical equation. The fluidized bed is maintained at constant temperature by means of a system of heat exchangers, arranged in the bed, which extract the heat of the exothermic reaction. In the preferred description of the procedure, the extracted heat is used to generate steam and in this manner improve the overall thermal balance of the procedure.
The chlorinated transport catalyst material is extracted continuously from the first chlorinating reactor and conducted to a second reactor, as is described below in stage 2. (2) CuCl2 + 1/2 0/->CuO + Cl2 Stage 2: The second reactor consists of a fluidized bed of transport catalyst which contains from 2 to about 20% of copper and sodium chlorides, which continuously mix with the current of similar material proceeding from the chlorinator, λ mixture of oxygen and nitrogen, the oxygen content of which is between about 99% and about 10% by volume, is injected into the fluidized bed in this oxidizing reactor. The best temperature for the oxidation reaction is between 300 and 380 C. Under these conditions, oxidation takes place rapidly and free chlorine is liberated from the catalytic mass, while the copper chloride is transformed into copper oxide.
A continuous flow of transport catalyst, which contains copper oxides, is extracted from the second reactor (the oxidizer) and returns to the first reactor (the chlorinator). A suitable heat exchange system nay be situated in the fluidized bed of each reactor and used to raise the temperature to the appropriate level for the reaction velocity to be sufficiently high. The heat exchange system provides the heat for the endothermic reaction so as to maintain the transport catalyst system isothermic.
The above paragraphs describe the basic process under consideration. A flow diagram as shewn in Fig.l which illustrates the said process is included in this description of the invention.
There are many factors to be considered in this particular reaction system. The flow of gases which emerges from the chlorinator is essentially formed of water vapour together with the inert gases which can be present in the hydrogen chloride which initially took part. Basically in this stage chlorine is not liberated, and in consequence the gases which leave the reactor are easily condensed and removed without ecological risk.
With regard to the oxidizing reactor, the gases which leave the system at the maximum temperature are formed of free chlorine, unreacted oxygen and the nitrogen originally present. Depending on the manner in which the reaction is carried out, small quantities of water vapour can also be present in the gas. Nevertheless, recovery of the chlorine from this mixture is not complicated by the presence of hydrogen chloride, thus avoiding difficult problems of corrosion in the recovery train.
The complete flow throughout the process is represented in the flow diagram. As can be seen, the gases which leave the oxidation reactor pass through a heat exchanger and a heat recovery system in order to allow recovery of the high degree of heat which would be carried along by the hot gases.
This heat can be used to preheat the air and the oxygen which enter the oxidation reactor, or, in an alternative form, can be used to generate steam at high temperature and pressure, which can be used either in the process itself, or to generate electricity. Once the gas has been cooled by heat exchange to a suitable level, for example between 70-170C, it is cooled still more with an air cooler in order to reduce the temperature to 40*C50* C. The current of thus cooled gas, which contains the chlorine, is then directed into an absorption and separation system using carbon tetrachloride or another suitable solvent which absorbs the chlorine from the gas » and concentrates it in the liquid phase used as absorption medium. The chlorine which is separated in this manner from the gas is liberated in a separation tower and afterwards is compressed, cooled, condensed and collected as liquid chlorine.
The nitrogen and the oxygen in the gas leaving the absorber are treated to separate the traces of chlorine which could be present, before proceeding to the chimney.
This system, as it has been described, has various advantages compared with other catalytic systems having a single stage which have been
Claims (3)
1. The conversion of hydrogen chloride to chlorine can take place in such a manner that it approximates to 100% in place of 80-83%, which is the conversion level attained by the previous systems described both in the literature and in the claims of patents.
2. The recovery of chlorine is simplified when the gas which contains it is free of hydrogen chloride, as in this case. 3. The gas which leaves the chlorinator is essentially free of hydrogen chloride and of chlorine, and basically consists of water vapour and inert gases which can be present in the starting hydrogen chloride. This simplifies the system which is needed for treating this current of gas. 4. Due to the naturalness of the two stage process and the use of the transport catalyst to produce separation of the currents of chlorine and hydrogen chloride, the complete procedure is significantly less expensive than the alternative systems which had been considered. Table 1 1 shows an overall material balance for the procedure as it would be carried out. Table 2 gives an estimated cost of the said procedure for an installation capable of producing 30,000 tons/year of liquid chlorine from gaseous hydrogen chloride, showing the economic advantages of this approach compared with the similar procedures which have been described by others in the literature and patents. 5. The procedure, considered as a whole, uses an advanced system for the absorption of chlorine from the exit gases, thus materially reducing the magnitude of refrigeration and cold necessary for the final condensation of the chlorine. 6. Due to the fact that the products which leave the reactors are, in one case (chlorinator) principally water, and in the other case (oxidizer) simply chlorine in the presence of oxygen .and nitrogen, the construction materials required for both reactors and the recovery system can be relatively less costly than they would need to be if the exit currents simultaneously contained chlorine and hydrogen chloride, as occurs in the alternative systems. 7. The use of a catalyst support allows the continuous recharging of the metallic material on the support, simply removing and replacing the transport catalyst while the procedure is working continuously. Experimental data have been gathered which show that this material » retains a high degree of activity for periods of more than 10,000 to 20,000 hours of continuous work. The typical supported catalyst system used for this process will contain copper chloride and sodium chloride in mol to mol proportions, placed on a support of alumina, silica or molecular sieves. These materials must be selected such that they have a total surface area not less than values of between 200 and 500 square metres per gramme, having a pore diameter of between 40 and 100 angstrom. It has been shown that the copper chloride and the sodium chloride thus prepared form, at the working temperature, a melted mixture in the pore structure of the catalyst, which increases its capability of reacting rapidly both with the hydrogen chloride and with the oxygen according to the specific reaction which takes place in the reaction zone of the fluidized bed. One method for the preparation of the catalyst used in this system is the following: copper chloride and sodium chloride, in the chosen suitable proportions and in saturated solutions, are mixed with the suitable support material. The proportions of the mixture are of an order of magnitude such that the final product will contain between 5 and about 20% of active copper material on the solid support. Once the material has been impregnated, it is dried at approximately 120 degrees and then calcined at 300 degrees C. Calcination takes place In a fluidized bed using preheated inert gas. As has been indicated above the solid support should be selected to have a particle size distribution suitable for fluidization in a normal fluidizing apparatus. Typical values for the particle size distribution are presented in Table
3. It should be emphasized that it is necessary to include a considerable fraction of small size material, with values of between 10 and 100 microns, to ensure that the catalyst has the desired fluid properties when it is stirred by a gas current with a superficial velocity of between 5 and 200 centimetres per second under the conditions existing in the interior of the reactor. KEY TO TOE FLOW DIAGRAM SHOWN IN FIG.l A. Feed hydrogen chloride. B. Gas containing oxygen. C. Carrier gas for the chlorinated transport catalyst (normally steam). D. Carrier gas for the oxidized transport catalyst (normally steam). E. Gas emerging from the chlorinator, principally water vapour. F. Gas emerging from the oxidizer, principally chlorine with nitrogen and oxygen. G. Condensate to be removed. H. Residual gas to be removed. J. Chlorine-free gas to the chimney. K. Rich solution from the absorber. L. Poor solution to the absorber. M. Liquid chlorine product. N. Steam rich in chlorine to be recycled to the absorber.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ES8901105A ES2010473A6 (en) | 1989-03-06 | 1989-03-06 | Recovery of chlorine from hydrogen chloride by means of a transport catalyst process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| IE900621L IE900621L (en) | 1990-09-06 |
| IE64525B1 true IE64525B1 (en) | 1995-08-09 |
Family
ID=8261185
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| IE62190A IE64525B1 (en) | 1989-03-06 | 1990-02-20 | Method for the recovery of chlorine from hydrogen chloride by means of a transport catalyst process and equipment for carrying out this method |
Country Status (11)
| Country | Link |
|---|---|
| BE (1) | BE1004114A3 (en) |
| CH (1) | CH680132A5 (en) |
| DE (1) | DE4004454A1 (en) |
| ES (1) | ES2010473A6 (en) |
| FR (1) | FR2643893B1 (en) |
| GB (1) | GB2229430B (en) |
| IE (1) | IE64525B1 (en) |
| IT (1) | IT1237811B (en) |
| LU (1) | LU87664A1 (en) |
| NL (1) | NL9000504A (en) |
| PT (1) | PT90982B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4959202A (en) * | 1989-05-31 | 1990-09-25 | Medalert Incorporated | Recovery of chlorine from hydrogen chloride by carrier catalyst process |
| DE69019981T2 (en) * | 1989-11-02 | 1995-11-02 | University Of Southern California, Los Angeles, Calif. | EFFICIENT METHOD FOR PRODUCING CHLORINE FROM HYDROCHLORINE. |
| SG67942A1 (en) * | 1995-05-18 | 1999-10-19 | Sumitomo Chem Ind | Process for producing chlorine |
| DE19533660A1 (en) * | 1995-09-12 | 1997-03-13 | Basf Ag | Process for the production of chlorine |
| DE19533659A1 (en) * | 1995-09-12 | 1997-03-13 | Basf Ag | Process for the production of chlorine from hydrogen chloride |
| CA2229993A1 (en) * | 1997-02-27 | 1998-08-27 | Air Products And Chemicals, Inc. | Fixed-bed temperature swing catalytic process for chemical reactions |
| DE10336522A1 (en) * | 2003-08-08 | 2005-02-24 | Basf Ag | Process for the production of chlorine |
| EP2165757A1 (en) * | 2008-09-16 | 2010-03-24 | Ahmed Mohammed Diaa Khafagy | Method and appliance for exothermal chemical processes with heat recovery |
| FR2958183B1 (en) * | 2010-04-06 | 2014-09-05 | Inst Francais Du Petrole | PROCESS FOR REMOVING GASEOUS PHASE HYDROGEN HALIDES |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2436870A (en) * | 1942-10-31 | 1948-03-02 | Standard Oil Dev Co | Preparation of chlorine |
| US2602021A (en) * | 1948-06-30 | 1952-07-01 | Kellogg M W Co | Catalytic production of chlorine |
| BE620364A (en) * | 1961-07-18 | |||
| NL282441A (en) * | 1962-08-10 | 1900-01-01 | ||
| US3323871A (en) * | 1963-06-26 | 1967-06-06 | Asahi Glass Co Ltd | Process for the production of chlorine |
| GB1192666A (en) * | 1967-06-21 | 1970-05-20 | Sir Soc Italiana Resine Spa | Process for the Catalytic Preparation of Chlorine from Hydrochloric Acid |
| BE789630A (en) * | 1971-10-04 | 1973-04-03 | Rhone Progil | REACTING MASSES INTENDED IN PARTICULAR FOR THE PREPARATION OF CHLORINE AND AMMONIA FROM AMMONIUM CHLORIDE, THEIR PREPARATION AND THEIR APPLICATIONS |
| JPS5034072A (en) * | 1973-06-20 | 1975-04-02 | ||
| US4119705A (en) * | 1977-04-06 | 1978-10-10 | The Lummus Company | Production of chlorine |
-
1989
- 1989-03-06 ES ES8901105A patent/ES2010473A6/en not_active Expired
- 1989-06-26 PT PT90982A patent/PT90982B/en not_active IP Right Cessation
- 1989-12-22 IT IT02282589A patent/IT1237811B/en active IP Right Grant
- 1989-12-26 FR FR8917195A patent/FR2643893B1/en not_active Expired - Fee Related
-
1990
- 1990-01-09 GB GB9000475A patent/GB2229430B/en not_active Expired - Fee Related
- 1990-01-23 CH CH198/90A patent/CH680132A5/fr not_active IP Right Cessation
- 1990-01-24 LU LU87664A patent/LU87664A1/en unknown
- 1990-02-01 BE BE9000115A patent/BE1004114A3/en not_active IP Right Cessation
- 1990-02-14 DE DE4004454A patent/DE4004454A1/en not_active Withdrawn
- 1990-02-20 IE IE62190A patent/IE64525B1/en not_active IP Right Cessation
- 1990-03-05 NL NL9000504A patent/NL9000504A/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| GB9000475D0 (en) | 1990-03-07 |
| CH680132A5 (en) | 1992-06-30 |
| BE1004114A3 (en) | 1992-09-29 |
| IT1237811B (en) | 1993-06-17 |
| DE4004454A1 (en) | 1990-09-13 |
| GB2229430B (en) | 1993-02-17 |
| NL9000504A (en) | 1990-10-01 |
| FR2643893A1 (en) | 1990-09-07 |
| FR2643893B1 (en) | 1993-02-05 |
| PT90982A (en) | 1990-11-07 |
| IE900621L (en) | 1990-09-06 |
| IT8922825A0 (en) | 1989-12-22 |
| ES2010473A6 (en) | 1989-11-01 |
| LU87664A1 (en) | 1990-05-15 |
| GB2229430A (en) | 1990-09-26 |
| PT90982B (en) | 1995-03-31 |
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