CN114436215A - Dehydrogenation process of hydrogen chloride synthesis gas - Google Patents
Dehydrogenation process of hydrogen chloride synthesis gas Download PDFInfo
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- CN114436215A CN114436215A CN202111637350.5A CN202111637350A CN114436215A CN 114436215 A CN114436215 A CN 114436215A CN 202111637350 A CN202111637350 A CN 202111637350A CN 114436215 A CN114436215 A CN 114436215A
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- hydrogen chloride
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- dehydrogenation
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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 120
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 92
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 67
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 36
- 230000008569 process Effects 0.000 title claims abstract description 32
- 239000001257 hydrogen Substances 0.000 claims abstract description 53
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 53
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 238000001179 sorption measurement Methods 0.000 claims abstract description 44
- 208000005156 Dehydration Diseases 0.000 claims abstract description 39
- 230000018044 dehydration Effects 0.000 claims abstract description 39
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 39
- 238000000926 separation method Methods 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000002485 combustion reaction Methods 0.000 claims abstract description 27
- 238000011084 recovery Methods 0.000 claims abstract description 27
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000001301 oxygen Substances 0.000 claims abstract description 18
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 239000003054 catalyst Substances 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 238000003795 desorption Methods 0.000 claims description 17
- 239000002808 molecular sieve Substances 0.000 claims description 16
- 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 16
- 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 14
- 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
- 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
- 238000007599 discharging Methods 0.000 claims description 2
- 229920002492 poly(sulfone) Polymers 0.000 claims description 2
- 229920006254 polymer film Polymers 0.000 claims 1
- 150000002431 hydrogen Chemical class 0.000 abstract description 4
- 230000006872 improvement Effects 0.000 description 9
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- 239000000460 chlorine Substances 0.000 description 5
- 229910052801 chlorine Inorganic materials 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 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
- 239000003814 drug Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920005597 polymer membrane Polymers 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
Images
Classifications
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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
- C01B7/012—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 synthesis 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 a 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 in the analytical tower by using a cooler, performing primary dehydration on a demister, and performing multistage dehydration on the hydrogen chloride gas subjected to primary dehydration by using an adsorption column; the synthesis gas separation tank is used for separating hydrogen chloride gas and hydrogen, the separated hydrogen and oxygen react to release heat to be used as a heat source in the analysis process of the hydrogen chloride solution, reasonable utilization of resources can be effectively achieved, and product water generated by the reaction of the hydrogen and the oxygen can be used as dissolved water when the dissolved 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
Hydrogen chloride gas is an important basic raw material and product in chemical industry, such as food processing, textile, medicine, etc
The method has wide industrial application, and plays a very key role in 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 present in a molar ratio of 1: 1, the chlorine is excessive and harmful more greatly in the actual production process, in order to ensure that the chlorine is fully combusted, the volume flow of the hydrogen is excessive by 5-10 percent compared with the chlorine, and the flame of the combustion reaction is bluish white under the control of the chlorine-hydrogen ratio.
However, when the hydrogen is excessive, the excessive hydrogen cannot participate in the combustion reaction, the flame is unstable and white, and white mist airflow is generated at the burner nozzle of the synthesis furnace, so that the purity of the hydrogen chloride is reduced, therefore, the hydrogen in the hydrogen chloride synthesis gas can be removed, the purity of the hydrogen chloride can be improved, the existing dehydrogenation process has high energy consumption, and the process has poor cyclability. Therefore, the invention provides a dehydrogenation process of hydrogen chloride synthesis gas, which aims to overcome the defects in the prior art.
Disclosure of Invention
In view of the above problems, an object of the present invention is to provide a dehydrogenation process for a hydrogen chloride synthesis gas, in which a dehydrogenation apparatus is constructed, a synthesis gas separation tank is used to separate hydrogen chloride gas and hydrogen gas, and the heat generated by the reaction between the separated hydrogen gas and oxygen gas is used as a heat source in the analysis process of a hydrogen chloride solution, so that reasonable utilization of resources can be effectively achieved, and water produced by the reaction between hydrogen gas and oxygen gas can be used as water for dissolving the hydrogen chloride gas in the synthesis gas separation tank, so that reaction products are fully utilized, and the operation of the whole synthesis gas dehydrogenation process is simple.
In order to achieve the purpose, the invention provides the following technical scheme:
a dehydrogenation process of hydrogen chloride synthesis gas comprises the following steps:
the method comprises the following steps: constructing a dehydrogenation device, wherein the dehydrogenation device comprises a synthesis gas separation tank, a hydrogen recovery tank, a hydrochloric acid recovery tank, a desorption tower, a heating jacket, a combustion device, an oxygen tank, a cooler and a demister;
step two: introducing the hydrogen chloride synthesis gas into a synthesis gas separation tank, dissolving hydrogen chloride by using water in the synthesis gas separation tank to form a 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 in the hydrogen recovery tank and the oxygen in the oxygen tank into a combustion device, and carrying out hydrogen combustion reaction in the combustion device;
step four: introducing a hydrochloric acid solution in a hydrochloric acid recovery tank into an analytical tower, adding a catalyst into the analytical tower, collecting reaction heat generated by hydrogen combustion reaction into a heating jacket, heating the analytical tower by using the heating jacket, and separating out hydrogen chloride gas in the analytical tower;
step five: cooling the hydrogen chloride gas precipitated in the desorption tower by using a cooler, and performing primary dehydration on the cooled hydrogen chloride gas by using a demister;
step six: and (3) performing multistage dehydration on the hydrogen chloride gas subjected to the first-stage dehydration by using an adsorption column to obtain the hydrogen chloride gas with the water content of less than 6 ppm.
The further improvement lies in that: in the first step, a membrane separator is arranged between the synthesis gas separation tank and the hydrogen recovery tank, and the membrane material adopted by the membrane separator is a polyimide or polysulfone high-molecular polymer membrane.
The further improvement lies in that: in the second step, when the hydrogen chloride synthesis gas enters the synthesis gas separation tank, the hydrogen with high permeation rate permeates the membrane separator and enters the hydrogen recovery tank, and the hydrogen chloride gas with low permeation rate is intercepted in the synthesis gas separation tank and dissolved in the water in the synthesis gas separation tank.
The further improvement lies in that: in the third step, water generated by the combustion reaction of the hydrogen in the combustion device is recycled to the synthesis gas separation tank through a pipeline and is used as dissolved water for dissolving the hydrogen chloride.
The further improvement lies in that: in the fourth step, the catalyst is calcium chloride solution, and a stirring mechanism is further arranged in the desorption tower and used for mixing the calcium chloride solution and the hydrochloric acid solution.
The further improvement lies in 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 desorption tower are desorbed also needs to be pumped back to the desorption tower again for repeated desorption for 2-3 times.
The further improvement lies in that: in the fourth step, after the calcium chloride solution and the hydrochloric acid solution in the desorption tower are desorbed, the catalyst calcium chloride solution is prepared again through the flash evaporation shunt tank and then is reused.
The further improvement is that: and in the sixth step, a molecular sieve with high adsorption capacity is adopted as an adsorption material in the adsorption column, a multi-stage adsorption column is constructed to carry out multi-stage 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 enters from the lower part of one side of the adsorption column and exits from the upper part of the other side of the adsorption column.
The further improvement lies in that: in the sixth step, before the hydrogen chloride gas after the first-stage dehydration is subjected to the multi-stage dehydration by using the adsorption column, the moisture content of the hydrogen chloride gas after the first-stage dehydration is firstly measured, and the stage number of the multi-stage dehydration is set according to the moisture content.
The further improvement lies in 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 invention has the beneficial effects that: according to the invention, by constructing the dehydrogenation device, the synthesis gas separation tank is used for separating hydrogen chloride gas and hydrogen, and the separated hydrogen and oxygen react to release heat to be used as a heat source in the analysis process of the hydrogen chloride solution, so that reasonable utilization of resources can be effectively realized, the product water generated by the reaction of the hydrogen and the oxygen can be used as the dissolved water when the dissolved hydrogen chloride gas is dissolved in the synthesis gas separation tank, the reaction product is fully utilized, and the whole synthesis gas dehydrogenation process is simple to operate;
by arranging the desorption tower, desorbing the hydrogen chloride solution by using the catalyst and performing multi-stage dehydration on the product hydrogen chloride gas, the hydrogen chloride gas with the moisture content lower than 6ppm can be obtained, the catalyst can be recycled, the process consumption in the dehydrogenation process is low, and the cyclability is high.
Drawings
FIG. 1 is a schematic view of the process of the present invention;
FIG. 2 is a schematic view of the dehydrogenation unit according to the present invention.
Wherein: 1. a syngas 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 pipeline; 12. a stirring mechanism; 13. and (4) adsorbing the column.
Detailed Description
In order to further understand the present invention, the following detailed description will be made with reference to the following examples, which are only used for explaining the present invention and are not to be construed as limiting the scope of the present invention.
According to fig. 1-2, this embodiment proposes a dehydrogenation process of hydrogen chloride synthesis gas, comprising the following steps:
the method comprises the following steps: 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 analytical tower 4, a heating jacket 5, a combustion device 6, an oxygen tank 7, a cooler 8 and a demister 9, a membrane separator 10 is further arranged between the synthesis gas separation tank 1 and the hydrogen recovery tank 2, the membrane material adopted by the membrane separator 10 is a polyimide high-molecular polymer thin membrane, in the embodiment, the heating jacket 5 is arranged at the bottom of the analytical tower 4, the gas outlet end of the analytical 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 a synthesis gas separation tank 1, when the hydrogen chloride synthesis gas enters the synthesis gas separation tank 1, hydrogen with high permeation rate permeates a membrane separator 10 and enters a hydrogen recovery tank 2, hydrogen chloride gas with low permeation rate is intercepted in the synthesis gas separation tank 1 and dissolved in water in the synthesis gas separation tank 1, the hydrogen chloride is dissolved by water in the synthesis gas separation tank 1 to form hydrochloric acid solution, the hydrogen in the hydrogen chloride synthesis gas is recovered and stored through the hydrogen recovery tank 2, and the hydrochloric acid solution in the synthesis gas separation tank 1 is discharged to a 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 a combustion device 6, carrying out 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 a hydrochloric acid solution in a hydrochloric acid recovery tank 3 into an analysis tower 4, adding a catalyst into the analysis tower 4, wherein the catalyst is a calcium chloride solution, a stirring mechanism 12 is further arranged in the analysis tower 4, the stirring mechanism 12 is used for mixing the calcium chloride solution and the hydrochloric acid solution, collecting reaction heat generated by a hydrogen combustion reaction into a heating jacket 5, heating the analysis tower 4 by using the heating jacket 5, separating out hydrogen chloride gas in the analysis tower 4, pumping water containing a small amount of hydrogen chloride generated after the calcium chloride solution and the hydrochloric acid solution in the analysis tower 4 are analyzed back to the analysis tower 4 again for repeated analysis for 3 times, and preparing the catalyst calcium chloride solution again through a flash evaporation shunt tank for reuse after the calcium chloride solution and the hydrochloric acid solution in the analysis tower 4 are analyzed;
step five: cooling the hydrogen chloride gas precipitated in the desorption tower 4 by using a cooler 8, and performing 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 after primary dehydration, setting the number of stages of the multi-stage dehydration according to the moisture content, and then performing the multi-stage dehydration on the hydrogen chloride gas after the 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 at the first stage is connected with the air outlet end of a demister 9, the air inlet end of the adsorption column 13 at the later stage is connected with the air outlet end of the adsorption column 13 at the later stage, an NKF-5 (50) molecular sieve is adopted in the adsorption column 13 as an adsorption material, the multi-stage adsorption column 13 is constructed to perform the multi-stage dehydration on the hydrogen chloride gas after the primary dehydration, and when the adsorption column 13 dehydrates the hydrogen chloride gas after the primary dehydration, the hydrogen chloride gas after the primary dehydration enters from the lower part of one side of the adsorption column 13 and exits from the upper part of the other side of the adsorption column 13; in this embodiment, the water content of the first-stage dehydrated hydrogen chloride gas is 120ppm, and the water content is higher, so in this embodiment, three stages of dehydration are selected to dehydrate the first-stage dehydrated hydrogen chloride gas, and three adsorption columns 13 filled with NKF-5 (50) molecular sieves are correspondingly constructed, in this embodiment, NKF-5 (50) molecular sieves are selected as the adsorption materials, because the adsorption capacity of the NKF-5 (50) molecular sieves is superior to that of the NKF-4A molecular sieve and the NKF-5 (300) molecular sieves, which are respectively marked as a first adsorption column, a second adsorption column and a third adsorption column, 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, and 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, and the third-stage dehydration is completed in the second adsorption column, then the third-stage dehydration is completed in the third adsorption column, and the water content of the hydrogen chloride gas discharged from the gas outlet of the third adsorption column is 5.4ppm by determination.
According to the invention, by constructing the dehydrogenation device, the synthesis gas separation tank 1 is used for separating hydrogen chloride gas and hydrogen, and the heat released by the reaction of the separated hydrogen and oxygen is used as a heat source in the analysis process of the hydrogen chloride solution, so that reasonable utilization of resources can be effectively realized, the product water generated by the reaction of the hydrogen and oxygen can be used as the dissolved water when the dissolved hydrogen chloride gas is dissolved in the synthesis gas separation tank 1, the reaction product is fully utilized, and the whole synthesis gas dehydrogenation process is simple to operate;
by arranging the desorption tower 4, desorbing the hydrogen chloride solution by using the catalyst and performing multi-stage dehydration on the product hydrogen chloride gas, the hydrogen chloride gas with the water content lower than 6ppm can be obtained, the catalyst can be recycled, the process consumption in the dehydrogenation process is low, and the cyclability is high.
The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (10)
1. A dehydrogenation process of hydrogen chloride synthesis gas is characterized in that: the method comprises the following steps:
the method comprises the following steps: constructing a dehydrogenation device, wherein the dehydrogenation device comprises a synthesis gas separation tank, a hydrogen recovery tank, a hydrochloric acid recovery tank, a desorption tower, a heating jacket, a combustion device, an oxygen tank, a cooler and a demister;
step two: introducing the hydrogen chloride synthesis gas into a synthesis gas separation tank, dissolving hydrogen chloride by using water in the synthesis gas separation tank to form a 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 in the hydrogen recovery tank and the oxygen in the oxygen tank into a combustion device, and carrying out hydrogen combustion reaction in the combustion device;
step four: introducing a hydrochloric acid solution in a hydrochloric acid recovery tank into an analytical tower, adding a catalyst into the analytical tower, collecting reaction heat generated by hydrogen combustion reaction into a heating jacket, heating the analytical tower by using the heating jacket, and separating out hydrogen chloride gas in the analytical tower;
step five: cooling the hydrogen chloride gas precipitated in the desorption tower by using a cooler, and performing primary dehydration on the cooled hydrogen chloride gas by using a demister;
step six: and (3) performing multistage dehydration on the hydrogen chloride gas subjected to the first-stage dehydration by using an adsorption column to obtain the hydrogen chloride gas with the water content of less than 6 ppm.
2. The dehydrogenation process of hydrogen chloride synthesis gas according to claim 1, characterized in that: in the first step, a membrane separator is arranged between the synthesis gas separation tank and the hydrogen recovery tank, and the membrane material adopted by the membrane separator is a polyimide or polysulfone high-molecular polymer film.
3. The dehydrogenation process of hydrogen chloride synthesis gas according to claim 1, characterized in that: in the second step, when the hydrogen chloride synthesis gas enters the synthesis gas separation tank, the hydrogen with high permeation rate permeates the membrane separator and enters the hydrogen recovery tank, and the hydrogen chloride gas with low permeation rate is intercepted in the synthesis gas separation tank and dissolved in the water in the synthesis gas separation tank.
4. The dehydrogenation process of hydrogen chloride synthesis gas according to claim 1, characterized in that: in the third step, water generated by the combustion reaction of the hydrogen in the combustion device is recycled to the synthesis gas separation tank through a pipeline and is used as dissolved water for dissolving the hydrogen chloride.
5. The dehydrogenation process of hydrogen chloride synthesis gas according to claim 1, characterized in that: in the fourth step, the catalyst is calcium chloride solution, and a stirring mechanism is further arranged in the desorption tower and used for mixing the calcium chloride solution and the hydrochloric acid solution.
6. The dehydrogenation process of hydrogen chloride synthesis gas according to claim 5, characterized in 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 desorption tower are desorbed also needs to be pumped back to the desorption tower again for repeated desorption for 2-3 times.
7. The dehydrogenation process of hydrogen chloride synthesis gas according to claim 5, characterized in that: in the fourth step, after the calcium chloride solution and the hydrochloric acid solution in the desorption tower are desorbed, the catalyst calcium chloride solution is prepared again through the flash evaporation shunt tank and then is reused.
8. The process according to claim 1, characterized in that: in the sixth step, a molecular sieve with high adsorption capacity is used as an adsorption material in the adsorption column, a multi-stage adsorption column is constructed to dehydrate the hydrogen chloride gas subjected to the first-stage dehydration, and when the adsorption column dehydrates the hydrogen chloride gas subjected to the first-stage dehydration, the hydrogen chloride gas subjected to the first-stage dehydration enters from the lower part of one side of the adsorption column and exits from the upper part of the other side of the adsorption column.
9. The process of claim 8, wherein the dehydrogenation comprises: in the sixth step, before the hydrogen chloride gas subjected to the first-stage dehydration is subjected to the multi-stage dehydration by using the adsorption column, the moisture content of the hydrogen chloride gas subjected to the first-stage dehydration is measured, and the stages of the multi-stage dehydration are set according to the moisture content.
10. The process of claim 8, wherein the dehydrogenation comprises: 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.
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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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