CN114436215B - Dehydrogenation process of hydrogen chloride synthesis gas - Google Patents
Dehydrogenation process of hydrogen chloride synthesis gas Download PDFInfo
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- CN114436215B CN114436215B CN202111637350.5A CN202111637350A CN114436215B CN 114436215 B CN114436215 B CN 114436215B CN 202111637350 A CN202111637350 A CN 202111637350A CN 114436215 B CN114436215 B CN 114436215B
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- hydrogen chloride
- hydrogen
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- gas
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 153
- 239000007789 gas Substances 0.000 title claims abstract description 119
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 93
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 93
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 65
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 65
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 28
- 230000008569 process Effects 0.000 title claims abstract description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000001257 hydrogen Substances 0.000 claims abstract description 46
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 46
- 238000001179 sorption measurement Methods 0.000 claims abstract description 43
- 208000005156 Dehydration Diseases 0.000 claims abstract description 41
- 230000018044 dehydration Effects 0.000 claims abstract description 41
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 41
- 238000000926 separation method Methods 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000002485 combustion reaction Methods 0.000 claims abstract description 26
- 238000011084 recovery Methods 0.000 claims abstract description 25
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 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
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 239000003054 catalyst Substances 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 4
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical group [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 15
- 239000012528 membrane Substances 0.000 claims description 13
- 239000002808 molecular sieve Substances 0.000 claims description 12
- 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 12
- 239000000463 material Substances 0.000 claims description 7
- 230000007246 mechanism Effects 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 239000004642 Polyimide Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 239000012466 permeate Substances 0.000 claims description 3
- 229920001721 polyimide Polymers 0.000 claims description 3
- 229920006254 polymer film Polymers 0.000 claims description 3
- 229920002492 poly(sulfone) Polymers 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 150000002431 hydrogen Chemical class 0.000 abstract description 4
- 238000004090 dissolution Methods 0.000 abstract description 3
- 230000006872 improvement Effects 0.000 description 9
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 6
- 239000000460 chlorine Substances 0.000 description 6
- 229910052801 chlorine Inorganic materials 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 238000003795 desorption Methods 0.000 description 4
- 229910001882 dioxygen Inorganic materials 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
Classifications
-
- 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
- C01B7/012—Preparation of hydrogen chloride from the elements
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Drying Of Gases (AREA)
Abstract
The invention discloses a dehydrogenation process of hydrogen chloride synthetic gas, which relates to the technical field of synthesis gas dehydrogenation and comprises the steps of constructing a dehydrogenation device, dissolving hydrogen chloride in water in a synthesis gas separation tank, introducing hydrogen recovered in a hydrogen recovery tank and oxygen in an oxygen tank into a combustion device, introducing hydrochloric acid solution into an analytical tower, adding a catalyst, collecting reaction heat generated by hydrogen combustion reaction into a heating jacket, heating the analytical tower by using the heating jacket, cooling hydrogen chloride gas separated out from the analytical tower by using a cooler, performing primary dehydration by using an adsorption column, and performing multistage dehydration on the hydrogen chloride gas subjected to the primary dehydration; the synthesis gas separation tank is utilized to separate hydrogen chloride gas and hydrogen, and the exothermic heat of the reaction of the separated hydrogen and oxygen is utilized as a heat source in the analysis process of the hydrogen chloride solution, so that the reasonable utilization of resources can be effectively realized, and the product water generated by the reaction of the hydrogen and the oxygen can be used as the dissolution water when the hydrogen chloride gas is dissolved in the synthesis gas separation tank.
Description
Technical Field
The invention relates to the technical field of synthesis gas dehydrogenation, in particular to a dehydrogenation process of hydrogen chloride synthesis gas.
Background
The hydrogen chloride gas is an important basic raw material and product in the chemical industry, and is used in food processing, spinning, medicine and the like
The industrial application is wide, and plays a very key role in the chlor-alkali chemical industry. Wherein, the hydrogen chloride can be generated by the combustion reaction of chlorine and hydrogen, and the reaction formula is as follows: cl2+h2=2hcl+q, as can be seen from the equation, chlorine and hydrogen are in a molar ratio of 1:1, in the actual production process, the excessive chlorine is more harmful, in order to fully burn the chlorine completely, the volume flow of the hydrogen is 5% -10% more than that of the chlorine, and under the control of the ratio of chlorine to hydrogen, the flame of the burning reaction is bluish white.
However, when the hydrogen is excessive, the excessive hydrogen cannot participate in the combustion reaction, the flame is unstable and white, and white vaporous air flow is generated at the burner nozzle of the synthesis furnace, so that the purity of the hydrogen chloride is reduced, therefore, the purity of the hydrogen chloride can be improved by removing the hydrogen in the hydrogen chloride synthesis gas, the energy consumption of the existing dehydrogenation process is larger, and the process cyclicity is poor. Therefore, the invention provides a dehydrogenation process of hydrogen chloride synthesis gas to solve the defects in the prior art.
Disclosure of Invention
Aiming at the problems, the invention aims to provide a dehydrogenation process of hydrogen chloride synthesis gas, which is characterized in that a dehydrogenation device is constructed, hydrogen chloride gas and hydrogen gas are separated by a synthesis gas separation tank, the exothermic heat of the reaction of the separated hydrogen gas and oxygen gas is used as a heat source in the analysis process of a hydrogen chloride solution, so that the reasonable utilization of resources can be effectively realized, and product water generated by the reaction of the hydrogen gas and the oxygen gas can be used as dissolved water when dissolved hydrogen chloride gas is dissolved in the synthesis gas separation tank, reaction products are fully utilized, and the whole synthesis gas dehydrogenation process is simple to operate.
In order to achieve the above purpose, the present invention provides the following technical solutions:
a process for the dehydrogenation of hydrogen chloride synthesis gas comprising the steps of:
step one: constructing a dehydrogenation device, wherein the dehydrogenation device comprises a synthesis gas separation tank, a hydrogen recovery tank, a hydrochloric acid recovery tank, a resolution tower, a heating jacket, a combustion device, an oxygen tank, a cooler and a demister;
step two: introducing hydrogen chloride synthesis gas into a synthesis gas separation tank, dissolving hydrogen chloride by using water in the synthesis gas separation tank to form hydrochloric acid solution, recovering and storing hydrogen in the hydrogen chloride synthesis gas through a hydrogen recovery tank, and discharging the hydrochloric acid solution in the synthesis gas separation tank to the hydrochloric acid recovery tank;
step three: introducing the hydrogen recovered from the hydrogen recovery tank and the oxygen in the oxygen tank into a combustion device, and performing a hydrogen combustion reaction in the combustion device;
step four: introducing hydrochloric acid solution in a hydrochloric acid recovery tank into a desorption tower, adding a catalyst into the desorption tower, collecting reaction heat generated by hydrogen combustion reaction into a heating jacket, heating the desorption tower by using the heating jacket, and separating out hydrogen chloride gas in the desorption tower;
step five: cooling the hydrogen chloride gas separated out from the analysis tower by using a cooler, and carrying out primary dehydration on the cooled hydrogen chloride gas by using a demister;
step six: and carrying out multistage dehydration on the hydrogen chloride gas subjected to the primary dehydration by utilizing an adsorption column to obtain the hydrogen chloride gas with the moisture content lower than 6 ppm.
The further improvement is that: in the first step, a membrane separator is arranged between the synthesis gas separating tank and the hydrogen recycling tank, and the membrane separator adopts a polyimide or polysulfone high polymer film as a membrane material.
The further improvement is that: in the second step, when the hydrogen chloride synthetic gas enters the synthesis gas separation tank, the high-permeation-rate hydrogen gas permeates the membrane separator and enters the hydrogen recovery tank, and the low-permeation-rate hydrogen chloride gas is intercepted in the synthesis gas separation tank and is dissolved in water in the synthesis gas separation tank.
The further improvement is that: in the third step, water generated by the hydrogen combustion reaction in the combustion device is recycled to the synthesis gas separation tank through a pipeline and used as dissolved water for dissolving hydrogen chloride.
The further improvement is that: in the fourth step, the catalyst is calcium chloride solution, and a stirring mechanism is further arranged in the analysis tower and is used for mixing the calcium chloride solution and the hydrochloric acid solution.
The further improvement is that: in the fourth step, the water containing a small amount of hydrogen chloride generated after the calcium chloride solution and the hydrochloric acid solution in the resolving tower are resolved also needs to be pumped back to the resolving tower again for repeated resolving for 2-3 times.
The further improvement is that: in the fourth step, after the calcium chloride solution and the hydrochloric acid solution in the analyzing tower are analyzed, the catalyst calcium chloride solution is prepared again through a flash evaporation diversion tank and then is reused.
The further improvement is that: in the sixth step, a molecular sieve with high adsorption capacity is used as an adsorption material in the adsorption column, a multistage adsorption column is constructed to carry out multistage dehydration on the hydrogen chloride gas after the first-stage dehydration, and when the adsorption column dehydrates the hydrogen chloride gas after the first-stage dehydration, the hydrogen chloride gas after the first-stage dehydration is introduced from the lower part of one side of the adsorption column and is discharged from the upper part of the other side of the adsorption column.
The further improvement is that: in the sixth step, before the adsorption column is used for carrying out multistage dehydration on the hydrogen chloride gas subjected to the first-stage dehydration, the water content of the hydrogen chloride gas subjected to the first-stage dehydration is measured, and the stage number of the multistage dehydration is set according to the water content.
The further improvement is that: the molecular sieve with high adsorption capacity is any one of NKF-5 (50) molecular sieve, NKF-4A molecular sieve and NKF-5 (300) molecular sieve.
The beneficial effects of the invention are as follows: according to the invention, a dehydrogenation device is constructed, the hydrogen chloride gas and the hydrogen gas are separated by the synthesis gas separation tank, the exothermic heat of the reaction of the separated hydrogen gas and the oxygen gas is used as a heat source in the analysis process of the hydrogen chloride solution, so that the reasonable utilization of resources can be effectively realized, and the product water generated by the reaction of the hydrogen gas and the oxygen gas can be used as the dissolution water when the hydrogen chloride gas is dissolved in the synthesis gas separation tank, so that the reaction product is fully utilized, and the whole synthesis gas dehydrogenation process is simple to operate;
the hydrogen chloride gas with the moisture content lower than 6ppm can be obtained by arranging the resolving tower and utilizing the catalyst to resolve the hydrogen chloride solution and carrying out multistage dehydration on the product hydrogen chloride gas, the catalyst can be recycled, the technical consumption in the dehydrogenation process is low, and the cyclicity is high.
Drawings
FIG. 1 is a schematic illustration of the process flow of the present invention;
FIG. 2 is a schematic diagram of the structure of the dehydrogenation unit according to the present invention.
Wherein: 1. a synthesis gas separation tank; 2. a hydrogen recovery tank; 3. a hydrochloric acid recovery tank; 4. an analytical tower; 5. a heating jacket; 6. a combustion device; 7. an oxygen tank; 8. a cooler; 9. a demister; 10. a membrane separator; 11. a pipe; 12. a stirring mechanism; 13. an adsorption column.
Detailed Description
The present invention will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.
According to fig. 1-2, this embodiment provides a process for dehydrogenation of hydrogen chloride synthesis gas, comprising the steps of:
step one: constructing a dehydrogenation device, wherein the dehydrogenation device comprises a synthesis gas separation tank 1, a hydrogen recovery tank 2, a hydrochloric acid recovery tank 3, an analysis tower 4, a heating jacket 5, a combustion device 6, an oxygen tank 7, a cooler 8 and a demister 9, wherein a membrane separator 10 is further arranged between the synthesis gas separation tank 1 and the hydrogen recovery tank 2, the membrane separator 10 adopts a polyimide high polymer film as a membrane material, in the embodiment, the heating jacket 5 is arranged at the bottom of the analysis tower 4, the gas outlet end of the analysis tower 4 is connected with the cooler 8, and the gas outlet end of the cooler 8 is connected with the demister 9;
step two: introducing hydrogen chloride synthesis gas into the synthesis gas separation tank 1, allowing hydrogen with high permeation rate to permeate through the membrane separator 10 and enter the hydrogen recovery tank 2 when the hydrogen chloride synthesis gas enters the synthesis gas separation tank 1, intercepting the hydrogen chloride gas with low permeation rate in the synthesis gas separation tank 1, dissolving the hydrogen chloride in water in the synthesis gas separation tank 1, dissolving the hydrogen chloride by using the water in the synthesis gas separation tank 1 to form hydrochloric acid solution, recovering and storing the hydrogen in the hydrogen chloride synthesis gas through the hydrogen recovery tank 2, and discharging the hydrochloric acid solution in the synthesis gas separation tank 1 to the hydrochloric acid recovery tank 3;
step three: introducing the hydrogen recovered in the hydrogen recovery tank 2 and the oxygen in the oxygen tank 7 into the combustion device 6, performing a hydrogen combustion reaction in the combustion device 6, and recovering water generated by the hydrogen combustion reaction in the combustion device 6 into the synthesis gas separation tank 1 through a pipeline 11 to be used as dissolved water for dissolving hydrogen chloride;
step four: introducing the hydrochloric acid solution in the hydrochloric acid recovery tank 3 into the analysis tower 4, adding a catalyst which is calcium chloride solution into the analysis tower 4, wherein the analysis tower 4 is also provided with a stirring mechanism 12, the stirring mechanism 12 is used for mixing the calcium chloride solution and the hydrochloric acid solution, collecting reaction heat generated by the hydrogen combustion reaction into a heating jacket 5, heating the analysis tower 4 by the heating jacket 5, separating out hydrogen chloride gas in the analysis tower 4, pumping water which contains a small amount of hydrogen chloride and is generated after the analysis of the calcium chloride solution and the hydrochloric acid solution in the analysis tower 4 back into the analysis tower 4 again for repeated analysis for 3 times, and preparing the catalyst calcium chloride solution again through a flash evaporation diversion tank after the analysis of the calcium chloride solution and the hydrochloric acid solution;
step five: cooling the hydrogen chloride gas precipitated in the analysis tower 4 by using a cooler 8, and carrying out primary dehydration on the cooled hydrogen chloride gas by using a demister 9;
step six: firstly, measuring the moisture content of the hydrogen chloride gas subjected to primary dehydration, setting the stage number of the multistage dehydration according to the moisture content, and then carrying out multistage dehydration on the hydrogen chloride gas subjected to primary dehydration by using an adsorption column 13 to obtain the hydrogen chloride gas with the moisture content lower than 6ppm, wherein in the embodiment, the air inlet end of the adsorption column 13 of the first stage is connected with the air outlet end of a demister 9, the air inlet end of the adsorption column 13 of the subsequent stage is connected with the air outlet end of the adsorption column 13 of the previous stage, NKF-5 (50) molecular sieve is adopted as an adsorption material in the adsorption column 13, so that the multistage adsorption column 13 is constructed to carry out multistage dehydration on the hydrogen chloride gas subjected to primary dehydration, and when the adsorption column 13 is used for dehydrating the hydrogen chloride gas subjected to primary dehydration, the hydrogen chloride gas subjected to primary dehydration is introduced from the lower part of one side of the adsorption column 13 and is discharged from the upper part of the other side of the adsorption column 13; in this embodiment, the moisture content of the first-stage dehydrated hydrogen chloride gas is 120ppm, and the moisture content is higher, so the embodiment selects three adsorption columns 13 filled with NKF-5 (50) molecular sieves for dehydration by three stages of dehydration, and the embodiment selects NKF-5 (50) molecular sieves as adsorption materials, because the adsorption capacity of the NKF-5 (50) molecular sieves is better than that of the NKF-4A molecular sieves and the NKF-5 (300) molecular sieves, the first adsorption column, the second adsorption column and the third adsorption column are marked respectively, then the first-stage dehydrated hydrogen chloride gas enters the first adsorption column from the air inlet below one side of the first adsorption column to complete the second-stage dehydration, then enters the air inlet below one side of the second adsorption column from the air outlet above the other side of the first adsorption column to complete the third-stage dehydration, and then enters the third adsorption column to complete the fourth-stage dehydration, and the moisture content of the hydrogen chloride gas discharged from the air outlet of the third adsorption column is measured to be 5.4ppm.
According to the invention, a dehydrogenation device is constructed, the synthesis gas separation tank 1 is utilized to separate hydrogen chloride gas and hydrogen, the exothermic heat of the reaction of the separated hydrogen gas and oxygen is utilized as a heat source in the analysis process of the hydrogen chloride solution, so that the reasonable utilization of resources can be effectively realized, and the product water generated by the reaction of the hydrogen gas and the oxygen can be used as the dissolution water when the dissolved hydrogen chloride gas is dissolved in the synthesis gas separation tank 1, so that the reaction product is fully utilized, and the whole synthesis gas dehydrogenation process is simple to operate;
the hydrogen chloride gas with the moisture content lower than 6ppm can be obtained by arranging the analyzing tower 4, analyzing the hydrogen chloride solution by using the catalyst and carrying out multistage dehydration on the product hydrogen chloride gas, the catalyst can be recycled, the technical consumption in the dehydrogenation process is low, and the cyclicity is high.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (7)
1. A process for the dehydrogenation of hydrogen chloride synthesis gas, characterized by: the method comprises the following steps:
step one: constructing a dehydrogenation device, wherein the dehydrogenation device comprises a synthesis gas separation tank, a hydrogen recovery tank, a hydrochloric acid recovery tank, a resolution tower, a heating jacket, a combustion device, an oxygen tank, a cooler and a demister;
step two: introducing hydrogen chloride synthesis gas into a synthesis gas separation tank, dissolving hydrogen chloride by using water in the synthesis gas separation tank to form hydrochloric acid solution, recovering and storing hydrogen in the hydrogen chloride synthesis gas through a hydrogen recovery tank, and discharging the hydrochloric acid solution in the synthesis gas separation tank to the hydrochloric acid recovery tank;
step three: introducing the hydrogen recovered from the hydrogen recovery tank and the oxygen in the oxygen tank into a combustion device, performing hydrogen combustion reaction in the combustion device, and recovering water generated by the hydrogen combustion reaction in the combustion device into a synthesis gas separation tank through a pipeline to be used as dissolved water for dissolving hydrogen chloride;
step four: introducing a hydrochloric acid solution in a hydrochloric acid recovery tank into a resolving tower, adding a catalyst into the resolving tower, collecting reaction heat generated by hydrogen combustion reaction into a heating jacket, heating the resolving tower by using the heating jacket, separating out hydrogen chloride gas in the resolving tower, wherein the catalyst is a calcium chloride solution, and a stirring mechanism is also arranged in the resolving tower and is used for mixing the calcium chloride solution and the hydrochloric acid solution;
step five: cooling the hydrogen chloride gas separated out from the analysis tower by using a cooler, and carrying out primary dehydration on the cooled hydrogen chloride gas by using a demister;
step six: and carrying out multistage dehydration on the hydrogen chloride gas subjected to the primary dehydration by utilizing an adsorption column to obtain the hydrogen chloride gas with the moisture content lower than 6 ppm.
2. A process for the dehydrogenation of hydrogen chloride synthesis gas according to claim 1, wherein: in the first step, a membrane separator is arranged between the synthesis gas separating tank and the hydrogen recycling tank, and the membrane separator adopts a polyimide or polysulfone high polymer film as a membrane material.
3. A process for the dehydrogenation of hydrogen chloride synthesis gas according to claim 1, wherein: in the second step, when the hydrogen chloride synthetic gas enters the synthesis gas separation tank, the high-permeation-rate hydrogen gas permeates the membrane separator and enters the hydrogen recovery tank, and the low-permeation-rate hydrogen chloride gas is intercepted in the synthesis gas separation tank and is dissolved in water in the synthesis gas separation tank.
4. A process for the dehydrogenation of hydrogen chloride synthesis gas according to claim 1, wherein: in the fourth step, the water containing a small amount of hydrogen chloride generated after the calcium chloride solution and the hydrochloric acid solution in the resolving tower are resolved also needs to be pumped back to the resolving tower again for repeated resolving for 2-3 times.
5. A process for the dehydrogenation of hydrogen chloride synthesis gas according to claim 1, wherein: in the fourth step, after the calcium chloride solution and the hydrochloric acid solution in the analyzing tower are analyzed, the catalyst calcium chloride solution is prepared again through a flash evaporation diversion tank and then is reused.
6. A process for the dehydrogenation of hydrogen chloride synthesis gas according to claim 1, wherein: in the sixth step, a molecular sieve with high adsorption capacity is used as an adsorption material in the adsorption column, a multistage adsorption column is constructed to carry out multistage dehydration on the hydrogen chloride gas after the first-stage dehydration, and when the adsorption column dehydrates the hydrogen chloride gas after the first-stage dehydration, the hydrogen chloride gas after the first-stage dehydration is introduced from the lower part of one side of the adsorption column and is discharged from the upper part of the other side of the adsorption column.
7. A process for the dehydrogenation of hydrogen chloride synthesis gas according to claim 6, wherein: in the sixth step, before the adsorption column is used for carrying out multistage dehydration on the hydrogen chloride gas subjected to the first-stage dehydration, the water content of the hydrogen chloride gas subjected to the first-stage dehydration is measured, and the stage number of the multistage dehydration is set according to the water content.
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| CN202111637350.5A CN114436215B (en) | 2021-12-29 | 2021-12-29 | Dehydrogenation process of hydrogen chloride synthesis gas |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5497597A (en) * | 1978-01-20 | 1979-08-01 | Denki Kagaku Kogyo Kk | Purification of hydrochloric acid gas |
| WO2001025143A1 (en) * | 1999-10-06 | 2001-04-12 | Norsk Hydro Asa | METHOD AND APPARATUS FOR SYNTHESIS OF HCl |
| CN102161474A (en) * | 2010-09-08 | 2011-08-24 | 泸州北方化学工业有限公司 | Method for refining hydrogen chloride gas |
| CN202625835U (en) * | 2012-04-11 | 2012-12-26 | 中国恩菲工程技术有限公司 | System for recovering hydrogen chloride from reduction exhaust gas |
| CN203098053U (en) * | 2013-03-12 | 2013-07-31 | 中国神华能源股份有限公司 | Chemical hydrogen-rich gas collecting and utilizing system |
| CN208893910U (en) * | 2018-09-14 | 2019-05-24 | 四川开元科技有限责任公司 | A kind of dry regenerative system of hydrogen chloride gas |
| CN113264507A (en) * | 2021-06-03 | 2021-08-17 | 陕西北元化工集团股份有限公司 | Method for removing hydrogen in hydrogen chloride gas |
-
2021
- 2021-12-29 CN CN202111637350.5A patent/CN114436215B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5497597A (en) * | 1978-01-20 | 1979-08-01 | Denki Kagaku Kogyo Kk | Purification of hydrochloric acid gas |
| WO2001025143A1 (en) * | 1999-10-06 | 2001-04-12 | Norsk Hydro Asa | METHOD AND APPARATUS FOR SYNTHESIS OF HCl |
| CN102161474A (en) * | 2010-09-08 | 2011-08-24 | 泸州北方化学工业有限公司 | Method for refining hydrogen chloride gas |
| CN202625835U (en) * | 2012-04-11 | 2012-12-26 | 中国恩菲工程技术有限公司 | System for recovering hydrogen chloride from reduction exhaust gas |
| CN203098053U (en) * | 2013-03-12 | 2013-07-31 | 中国神华能源股份有限公司 | Chemical hydrogen-rich gas collecting and utilizing system |
| CN208893910U (en) * | 2018-09-14 | 2019-05-24 | 四川开元科技有限责任公司 | A kind of dry regenerative system of hydrogen chloride gas |
| CN113264507A (en) * | 2021-06-03 | 2021-08-17 | 陕西北元化工集团股份有限公司 | Method for removing hydrogen in hydrogen chloride gas |
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| CN114436215A (en) | 2022-05-06 |
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