CN203754414U - System for producing hydrogen chloride gas by hydrochloric acid analysis - Google Patents
System for producing hydrogen chloride gas by hydrochloric acid analysis Download PDFInfo
- Publication number
- CN203754414U CN203754414U CN201420096997.0U CN201420096997U CN203754414U CN 203754414 U CN203754414 U CN 203754414U CN 201420096997 U CN201420096997 U CN 201420096997U CN 203754414 U CN203754414 U CN 203754414U
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- Prior art keywords
- gas
- outlet
- phase
- import
- hydrochloric acid
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 106
- 239000007789 gas Substances 0.000 title claims abstract description 76
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 23
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 239000007791 liquid phase Substances 0.000 claims abstract description 22
- 239000000463 material Substances 0.000 claims abstract description 20
- 239000012071 phase Substances 0.000 claims abstract description 15
- 230000008676 import Effects 0.000 claims description 33
- 239000007792 gaseous phase Substances 0.000 claims description 11
- 239000002253 acid Substances 0.000 claims description 9
- 150000003839 salts Chemical class 0.000 claims description 7
- 239000007788 liquid Substances 0.000 abstract description 6
- 230000000630 rising effect Effects 0.000 abstract description 3
- 238000001556 precipitation Methods 0.000 abstract 1
- 238000009835 boiling Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- LIKFHECYJZWXFJ-UHFFFAOYSA-N dimethyldichlorosilane Chemical compound C[Si](C)(Cl)Cl LIKFHECYJZWXFJ-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000000178 monomer Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- IJOOHPMOJXWVHK-UHFFFAOYSA-N chlorotrimethylsilane Chemical compound C[Si](C)(C)Cl IJOOHPMOJXWVHK-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 241000237983 Trochidae Species 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010504 bond cleavage reaction Methods 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- YGZSVWMBUCGDCV-UHFFFAOYSA-N chloro(methyl)silane Chemical compound C[SiH2]Cl YGZSVWMBUCGDCV-UHFFFAOYSA-N 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- JLUFWMXJHAVVNN-UHFFFAOYSA-N methyltrichlorosilane Chemical compound C[Si](Cl)(Cl)Cl JLUFWMXJHAVVNN-UHFFFAOYSA-N 0.000 description 1
- 150000001282 organosilanes Chemical class 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 229910000077 silane Inorganic materials 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000005051 trimethylchlorosilane Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a system for producing a hydrogen chloride gas by hydrochloric acid analysis. The system comprises an analysis tower, a double-effect heat exchanger, a gas-liquid separating tank, a re-boiler and a gas condenser group, wherein a liquid-phase inlet and a gas-phase outlet are formed in the top of the analysis tower; a liquid-phase outlet and a gas-phase inlet are formed in the bottom of the analysis tower; the liquid-phase outlet is connected with a tube pass inlet of the double-effect heat exchanger; the gas-phase inlet is connected with the re-boiler; the gas-phase outlet is connected with a material inlet of the gas condenser group; the liquid-phase inlet is connected with the bottom of the gas-liquid separating tank; a tube pass outlet and the shell pass inlet are formed in the top of the double-effect heat exchanger; a tube pass inlet and a shell pass outlet are formed in the bottom of the double-effect heat exchanger; the tube pass outlet is connected with the top of a buffer tank; the gas-liquid separating tank is higher than the liquid-phase inlet of the analysis tower; the top end of the gas-liquid separating tank is connected with the material inlet of the gas condenser group by a pipeline; the re-boiler is arranged below the gas-phase inlet of the analysis tower; the gas condenser group is arranged above gas-phase outlet the analysis tower. By virtue of the system disclosed by the utility model, concentrated hydrochloric acid passes through the tube pass of the double-effect heat exchanger, so that a gas resistance problem produced by hydrogen chloride gas precipitation can be avoided, and therefore, heat exchange between the concentrated hydrochloric acid and a rising high-temperature gas is more sufficient.
Description
Technical field
The utility model relates to a kind of gas resolution system, relates in particular to a kind of system of producing hydrogen chloride by resolving hydrochloric acid gas
Background technology
At present, adopt direct synthesis organosilane monomer both at home and abroad, except target product dimethyldichlorosilane(DMCS), also have some by products, comprise monomethyl trichlorosilane, trimethylchlorosilane, dimethyl dichlorosilane (DMCS), high boiling material and low-boiling-point substance etc.Organosilicon high-boiling product refers to 80～215 DEG C of boiling ranges, taking-Si-Si-,-Si-CH2-,-Si-O-Si-as main high boiling point silane mixture, account for the 5-8% left and right of mix monomer composition, organosilicon is a kind of smell with irritating, and there is the very yellow liquid of severe corrosive, be not easy to store and process, pose a big pressure to environmental protection.
Through research and development for many years, develop now the method for several recycling organosilicon high-boiling products, comprise catalystic pyrolysis and hydrolysis method, wherein cracking process is the most ripe at present method, its principal reaction principle is as follows:
Concrete operations are: in cracking reactor, add successively high boiling material cut, N, after N dimethyl benzene amine catalyst, turn on agitator is also adjusted to certain rotating speed, and when temperature of reactor is increased to 150～160 DEG C of set(ting)values, open hydrogen chloride gas steel cylinder, hydrogen chloride gas passes into cracking reactor bottom in bubbling mode after drying, under catalyst action with high boiling material generation scission reaction; The methyl chlorosilane monomer that cracking produces is by packing tower fractionation, and its mid-boiling point is collected after lower than the cut condensation of 70 DEG C, and boiling point by regulating splitting ratio to return in reactor, need to use a large amount of hydrogen chloride gas higher than the cut of 100 DEG C as seen.
Hydrogenchloride is mainly produced acquisition by resolving hydrochloric acid now, its cardinal principle falls concentrated hydrochloric acid exactly from Analytic Tower top, and high-temp chlorination hydrogen and water vapour pass into from Analytic Tower bottom, both realize heat exchange in tower, make the hydrogen chloride gas in concentrated hydrochloric acid resolve and deviate from.Before concentrated hydrochloric acid passes into Analytic Tower, concentrated hydrochloric acid and dilute hydrochloric acid need to be carried out to heat exchange in double-effect heat exchanger, generally concentrated hydrochloric acid is that bottom shell side import enters, and then flow out from the outlet of top shell side, and dilute hydrochloric acid is to pass through shell side.Because concentrated hydrochloric acid temperature raises, partial oxidation hydrogen is separated out from concentrated hydrochloric acid, can cause shell side to have vapour lock, makes acid amount unstable.In addition, concentrated hydrochloric acid is to be generally sprayed in Analytic Tower by high pressure, if sneak into partial oxidation hydrogen, can cause two strands of air-flows contrary, is unfavorable for heat exchange.
Utility model content
The utility model provides a kind of system of producing hydrogen chloride by resolving hydrochloric acid gas, after solving the heat exchange of existing system concentrated hydrochloric acid, separates out vapour lock and the inadequate problem of heat exchange that partial oxidation hydrogen causes.
A system for producing hydrogen chloride by resolving hydrochloric acid gas, comprising:
Analytic Tower, top is provided with liquid phase import, gaseous phase outlet, bottom is provided with liquid-phase outlet, gas phase import, liquid-phase outlet connects the tube side import of economic benefits and social benefits heat exchanger, gas phase import connects reboiler, gaseous phase outlet connects the material inlet of gas condenser group, and liquid phase import connects the bottom of knockout drum;
Economic benefits and social benefits heat exchanger, comprises tube side and shell side, and top is provided with tube side outlet and shell side import, and bottom is provided with tube side import and shell side outlet, and tube side outlet connects the top of surge tank;
Knockout drum, higher than the liquid phase import of Analytic Tower, top connects the material inlet of gas condenser group by pipeline;
Reboiler, is located at the below of Analytic Tower gas phase import;
Gas condenser group, the gas condenser that comprises some mutual series connection, is located at the top of resolving gaseous phase outlet.
After concentrated hydrochloric acid part analysis after heating, first send in knockout drum, the top of gas in knockout drum, can directly enter condenser by the pipeline at top, and concentrated hydrochloric acid enters Analytic Tower by the pipeline of bottom, meet with the high-temperature gas rising, owing to not existing air-flow to cross, can realize sufficient heat exchange.
Described reboiler bottom connects shell side import.
Described gas condenser group comprises front gas condenser and the rear gas condenser of mutual series connection, the material inlet of gas condenser before described gaseous phase outlet is connected with surge tank.
Comprise the gas buffer tank being connected with the material outlet of described rear gas condenser.
Comprise the scum dredger being connected with described gas buffer tank top.
Comprise the moisture eliminator being connected with described scum dredger.
Comprise that material inlet exports with described shell side the salt acid condenser being connected.
Comprise the hydrochloride buffer tank being connected with described salt acid condenser material outlet, hydrochloride buffer tank is located at the below of gas condenser group and gas surge tank, connects the bottom of gas buffer tank and gas condenser.
The utility model passes through the tube side of economic benefits and social benefits heat exchanger by concentrated hydrochloric acid, can avoid hydrogen chloride gas to separate out the vapour lock problem of generation, allow the concentrated hydrochloric acid flowing out first send in knockout drum, pass into again Analytic Tower, can avoid two strands of airflow collisions, make the high-temperature gas heat exchange of concentrated hydrochloric acid and rising more abundant, thereby more separate out hydrogen chloride gas.
Brief description of the drawings
Fig. 1 is the structural representation of the utility model system.
Embodiment
As shown in Figure 1, a kind of system of producing hydrogen chloride by resolving hydrochloric acid gas, comprise Analytic Tower 1, reboiler 2, economic benefits and social benefits heat exchanger 3, front gas condenser 4, rear gas condenser 5, gas buffer tank 6, scum dredger 7, hydrochloride buffer tank 8, salt acid condenser 9 and knockout drum 10.Analytic Tower 1 is legacy equipment, comprises liquid phase import, gaseous phase outlet, liquid-phase outlet and gas phase import, and wherein liquid phase import, gaseous phase outlet are positioned at top, and bottom is located in liquid-phase outlet and gas phase import.
The import that the liquid phase import of Analytic Tower 1 is concentrated hydrochloric acid, it is connected with the bottom of knockout drum, the outlet that gaseous phase outlet is hydrogen chloride gas, it is connected with the material inlet of front gas condenser 4.The gas phase import of Analytic Tower 1 is connected with reboiler 2, and the outlet that liquid-phase outlet is dilute hydrochloric acid is connected with the shell side import of economic benefits and social benefits heat exchanger 3.
Economic benefits and social benefits heat exchanger 3 comprises tube side and shell side, the outlet that the tube side outlet at top is concentrated hydrochloric acid, and the import that the tube side import of bottom is concentrated hydrochloric acid, connects concentrated hydrochloric acid storage tank.The shell side import at top is dilute hydrochloric acid import, be connected with the liquid-phase outlet of Analytic Tower 1, the shell side outlet of bottom, for dilute hydrochloric acid outlet, be connected, and the material outlet of salt acid condenser connects the hydrochloride buffer tank 8 for collecting dilute hydrochloric acid with the material inlet of salt acid condenser 9.
Front gas condenser 4 and rear gas condenser 5 are connected mutually, both heat-eliminating medium differences used, the former is recirculated cooling water, the latter is chilled brine, the most of water vapour that can go out in hydrogen chloride gas, surge tank can be by the standing water vapour cooling-sedimentation that allows.Because all produced concentrated hydrochloric acid, bottom connects hydrochloride buffer tank 8, reaches the object of collection.
The utility model System Working Principle is as follows:
Utilize high-temperature steam to heat the azeotrope in reboiler 2, the high-temperature gas that hydrogenchloride and water vapour mix enters the bottom of Analytic Tower 1 from bottom, and high-temperature gas rises, and contacts with the concentrated hydrochloric acid falling, and concentrated hydrochloric acid heats up and separates out hydrogen chloride gas.
The dilute hydrochloric acid that flow out bottom is azeotrope, concentration is in 21% left and right, it enters economic benefits and social benefits heat exchanger 2 and carries out heat exchange with concentrated hydrochloric acid, after exchange, concentrated hydrochloric acid rises to 80 DEG C of left and right, and there is partial oxidation hydrogen to separate out, because by the tube side of economic benefits and social benefits heat exchanger 2, therefore there is not the problem of vapour lock in dense smoke acid.
First enter knockout drum 10 from economic benefits and social benefits heat exchanger 2 concentrated hydrochloric acid out, after gas-liquid separation, concentrated hydrochloric acid again high pressure is squeezed into Analytic Tower 1 and is carried out heat exchange with high-temperature gas, the kinetic energy that can avoid air-flow to offset on the contrary gas flow mutually, cause heat exchange insufficient, enter front gas condenser 4 together with the hydrogen chloride gas that the gas of separation flows out with Analytic Tower 1.
Hydrogen chloride gas purity after multiple condensation improves, and the concentrated hydrochloric acid falling is collected in hydrochloride buffer tank 8, sends into next process together with condensed dilute hydrochloric acid, as again resolved hydrogen chloride gas.
Claims (8)
1. a system for producing hydrogen chloride by resolving hydrochloric acid gas, comprising:
Analytic Tower, top is provided with liquid phase import, gaseous phase outlet, bottom is provided with liquid-phase outlet, gas phase import, liquid-phase outlet connects the tube side import of economic benefits and social benefits heat exchanger, gas phase import connects reboiler, gaseous phase outlet connects the material inlet of gas condenser group, and liquid phase import connects the bottom of knockout drum;
Economic benefits and social benefits heat exchanger, comprises tube side and shell side, and top is provided with tube side outlet and shell side import, and bottom is provided with tube side import and shell side outlet, and tube side outlet connects the top of surge tank;
Knockout drum, higher than the liquid phase import of Analytic Tower, top connects the material inlet of gas condenser group by pipeline;
Reboiler, is located at the below of Analytic Tower gas phase import;
Gas condenser group, the gas condenser that comprises some mutual series connection, is located at the top of resolving gaseous phase outlet.
2. the system as claimed in claim 1, is characterized in that, described reboiler bottom connects shell side import.
3. the system as claimed in claim 1, is characterized in that, described gas condenser group comprises front gas condenser and the rear gas condenser of mutual series connection, the material inlet of gas condenser before described gaseous phase outlet is connected with surge tank.
4. system as claimed in claim 3, is characterized in that, comprises the gas buffer tank being connected with the material outlet of described rear gas condenser.
5. system as claimed in claim 4, is characterized in that, comprises the scum dredger being connected with described gas buffer tank top.
6. system as claimed in claim 5, is characterized in that, comprises the moisture eliminator being connected with described scum dredger.
7. the system as claimed in claim 1, is characterized in that, comprises that material inlet exports with described shell side the salt acid condenser being connected.
8. system as claimed in claim 7, is characterized in that, comprises the hydrochloride buffer tank being connected with described salt acid condenser material outlet, and hydrochloride buffer tank is located at the below of gas condenser group and gas surge tank, connects the bottom of gas buffer tank and gas condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420096997.0U CN203754414U (en) | 2014-03-04 | 2014-03-04 | System for producing hydrogen chloride gas by hydrochloric acid analysis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420096997.0U CN203754414U (en) | 2014-03-04 | 2014-03-04 | System for producing hydrogen chloride gas by hydrochloric acid analysis |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203754414U true CN203754414U (en) | 2014-08-06 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420096997.0U Expired - Lifetime CN203754414U (en) | 2014-03-04 | 2014-03-04 | System for producing hydrogen chloride gas by hydrochloric acid analysis |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203754414U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106242942A (en) * | 2016-09-07 | 2016-12-21 | 山东道可化学有限公司 | The method for continuously synthesizing of a kind of 1 chlorobutane and the equipment of production thereof |
| CN108191132A (en) * | 2018-01-05 | 2018-06-22 | 江苏天楹环保能源成套设备有限公司 | The recovery method of heavy metal in a kind of high villaumite acid waste water |
| CN112650176A (en) * | 2020-12-22 | 2021-04-13 | 天能化工有限公司 | DCS control method for hydrochloric acid analysis start-stop process |
-
2014
- 2014-03-04 CN CN201420096997.0U patent/CN203754414U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106242942A (en) * | 2016-09-07 | 2016-12-21 | 山东道可化学有限公司 | The method for continuously synthesizing of a kind of 1 chlorobutane and the equipment of production thereof |
| CN108191132A (en) * | 2018-01-05 | 2018-06-22 | 江苏天楹环保能源成套设备有限公司 | The recovery method of heavy metal in a kind of high villaumite acid waste water |
| CN112650176A (en) * | 2020-12-22 | 2021-04-13 | 天能化工有限公司 | DCS control method for hydrochloric acid analysis start-stop process |
| CN112650176B (en) * | 2020-12-22 | 2022-08-30 | 天能化工有限公司 | DCS control method for hydrochloric acid analysis start-stop process |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: HOSHINE SILICON CO., LTD. Free format text: FORMER NAME: ZHEJIANG HESHENG SILICON INDUSTRY CO., LTD. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: Jiaxing City, Zhejiang province 314000 Zhapu Zhen Ya Mountain Road No. 530 Patentee after: HOSHINE SILICON INDUSTRY CO.,LTD. Address before: Jiaxing City, Zhejiang province 314000 Zhapu Zhen Ya Mountain Road No. 530 Patentee before: ZHEJIANG HESHENG SILICON INDUSTRY Co.,Ltd. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20140806 |
|
| CX01 | Expiry of patent term |