CN214059913U - Food grade liquid SO2Preparation system - Google Patents
Food grade liquid SO2Preparation system Download PDFInfo
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- CN214059913U CN214059913U CN202021656230.0U CN202021656230U CN214059913U CN 214059913 U CN214059913 U CN 214059913U CN 202021656230 U CN202021656230 U CN 202021656230U CN 214059913 U CN214059913 U CN 214059913U
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- 239000007788 liquid Substances 0.000 title claims abstract description 129
- 238000004821 distillation Methods 0.000 claims abstract description 104
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 238000002360 preparation method Methods 0.000 claims abstract description 12
- 238000007599 discharging Methods 0.000 claims abstract description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 11
- 239000002253 acid Substances 0.000 claims description 7
- 238000012432 intermediate storage Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 4
- 238000005215 recombination Methods 0.000 abstract description 2
- 230000006798 recombination Effects 0.000 abstract description 2
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 21
- 229910052731 fluorine Inorganic materials 0.000 description 21
- 239000011737 fluorine Substances 0.000 description 21
- 238000003860 storage Methods 0.000 description 16
- 238000010992 reflux Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 239000011964 heteropoly acid Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000001035 drying Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910006124 SOCl2 Inorganic materials 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
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- FYSNRJHAOHDILO-UHFFFAOYSA-N thionyl chloride Substances ClS(Cl)=O FYSNRJHAOHDILO-UHFFFAOYSA-N 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides food-grade liquid SO2A preparation system, by which SO in the raw material gas can be treated2Extracting gas to obtain food-grade liquid SO2The method comprises the following steps: a primary distillation tower with a raw material gas inlet is used for extracting light components of the raw material gas; the primary distillation gas condenser is connected with a gas outlet at the top of the primary distillation tower and condenses the light components; the inlet of the primary distillation tower gas-liquid separator is connected with the outlet of the primary distillation gas condenser; the gas outlet of the gas-liquid separator of the primary distillation tower is communicated with the inside of the distillation tower through a first primary distillation gas compressor, and the gas-liquid separator of the primary distillation towerThe discharged gas is rectified in a rectifying tower, and the recombination after rectification in the rectifying tower is divided into product liquid SO2And discharging light components.
Description
Technical Field
The invention relates to food-grade liquid SO2The technical field of preparation, in particular to food-grade liquid SO2And (4) preparing the system.
Background
In industrial production, containing SO2If the industrial tail gas is randomly discharged, the environmental pollution is caused, the production cost of enterprises is increased if the industrial tail gas is treated by simple chemical neutralization, and the waste after treatment is simultaneously usedThe substances can cause certain pollution to water and soil, and if SO is contained in the substances2The extraction will bring extra profit to enterprises undoubtedly, and simultaneously the problem of environmental pollution caused by random discharge is solved well, SO the design provides a food-grade liquid SO2And (4) preparing the system.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, adapt to the practical requirements and provide food-grade liquid SO2A preparation system, by which SO in the raw material gas can be treated2Extracting gas to obtain food-grade liquid SO2。
In order to realize the purpose of the invention, the technical scheme adopted by the invention is as follows:
design a food-grade liquid SO2A manufacturing system, comprising:
a primary distillation tower with a raw material gas inlet is used for extracting light components of the raw material gas;
the primary distillation gas condenser is connected with a gas outlet at the top of the primary distillation tower and condenses the light components;
the inlet of the primary distillation tower gas-liquid separator is connected with the outlet of the primary distillation gas condenser;
the gas discharged from the gas-liquid separator of the primary tower enters the rectification tower for rectification, and the heavy components rectified by the rectification tower are divided into product liquid
SO2And discharging light components.
The liquid outlet of the gas-liquid separator of the primary distillation tower is communicated with the interior of the primary distillation tower.
The middle part of the rectifying tower is provided with a mixed acid outlet which is connected with a mixed acid intermediate storage tank, and the outlet of the mixed acid intermediate storage tank is connected with the inlet of the gas-liquid separator of the primary distillation tower.
The device also comprises a rectifying gas condenser and a rectifying tower gas-liquid first separator, wherein an exhaust port at the top of the rectifying tower is connected with an inlet of the rectifying gas condenser, an outlet of the rectifying gas condenser is connected with an inlet of the rectifying tower gas-liquid first separator, a liquid discharge port of the rectifying tower gas-liquid first separator is connected with the rectifying tower, and a gas outlet of the rectifying tower gas-liquid first separator is an HCL gas discharge port and is connected with an external hydrochloric acid preparation device.
The distillation tower further comprises a distillation liquid reboiler, a liquid outlet at the bottom of the distillation tower is further connected with an inlet of the distillation liquid reboiler, and an outlet of the distillation liquid reboiler is connected with the inside of the distillation tower.
Still include the initial distillation liquid reboiler, the liquid export of initial distillation tower bottom and the access connection of initial distillation liquid reboiler, the export and the initial distillation tower access connection of initial distillation liquid reboiler.
The first heat exchange subsystem is used for providing heat exchange energy for the primary distillation tower reboiler and the rectifying tower condenser; the first heat exchange subsystem comprises a first fluorine storage device, a liquefier, a first compressor, a first heat regenerator and a first separator, a liquid outlet of the first fluorine storage device is connected with a first inlet of the first separator through a first heat exchange tube in a first dryer and the first heat regenerator in sequence, a liquid outlet of the first separator is connected with a heat exchange tube inlet in a rectifying tower condenser through a first circulating pump, an outlet of the heat exchange tube in the rectifying tower condenser is connected with a second inlet of the first separator, and a top gas outlet of the first separator is connected with a first compressor inlet through a second heat exchange tube in the first heat regenerator; the outlet of the first compressor is connected with the inlet of the liquefier after sequentially passing through the heat exchange tubes in the reboiler of the primary distillation liquid, the outlet of the liquefier is connected with the first fluorine storage device, and the heat exchange tubes of the liquefier adopt cold water as a heat exchange medium.
The second heat exchange subsystem is used for providing heat exchange energy for the rectification liquid reboiler and the primary gas condenser; the second heat exchange subsystem comprises a second fluorine storage device, a second compressor, a subcooler, a second heat regenerator and a second separator; and a liquid outlet of the second fluorine storage device is connected with a first inlet of the second separator after sequentially passing through the second dryer, the subcooler and a first heat exchange tube in the second heat regenerator, a liquid outlet of the second separator is connected with a heat exchange tube inlet of the first distillation gas condenser through a second circulating pump, a heat exchange tube outlet of the first distillation gas condenser is connected with a second inlet of the second separator, a gas outlet of the second separator is connected with a heat exchange tube in the rectification liquid reboiler after sequentially passing through a second heat exchange tube of the second heat regenerator and a second compressor, and a heat exchange tube outlet in the rectification liquid reboiler is connected with a second fluorine storage device inlet.
The invention has the beneficial effects that:
the design adopts a double-tower design, and the primary tower can remove H2O、SOCL2Separating SO from heavy components in a rectifying tower2And HCL, SO2The boiling point of the HCL is-10 ℃, the boiling point of the HCL is-85 ℃, the HCL and the SO2 with high purity and food grade can be obtained at the bottom of the rectifying tower, and the HCL gas is obtained at the top of the rectifying tower.
Drawings
Fig. 1 is a schematic diagram of the design.
Detailed Description
The invention is further illustrated with reference to the following figures and examples:
example 1: food-grade liquid SO2Preparation system, see fig. 1.
The device comprises a primary distillation tower T1 with a raw material gas inlet for extracting light components of the raw material gas, a primary distillation gas condenser E1E1 which is connected with a gas outlet at the top of the primary distillation tower T1 and condenses the light components, and a liquid discharge port of a gas-liquid separator Y1 of the primary distillation tower is communicated with the inside of the primary distillation tower; the distillation tower further comprises a primary distillation liquid reboiler E2, a liquid outlet at the bottom of the primary distillation tower T1 is connected with an inlet of the primary distillation liquid reboiler E2, and an outlet of the primary distillation liquid reboiler E2 is connected with an inlet of the primary distillation tower.
The gas-liquid separator comprises a primary distillation tower Y1, wherein the inlet of the primary distillation tower Y1 is connected with the discharge port of a primary distillation gas condenser E1E1, the gas-liquid separator also comprises a rectification tower T2, the exhaust port of the primary distillation tower Y1 is communicated with the interior of the rectification tower T2 through a first primary distillation gas compressor C1 in sequence, a post-compressor cooler E6 is communicated with the interior of the rectification tower T2 in sequence, the post-compressor cooler E6 adopts water as a heat exchange medium, the gas discharged by the primary distillation tower Y1 is rectified in the rectification tower T2 after being compressed and cooled in sequence, and the recombination after rectification by the rectification tower T2 is divided into product liquid SO2And discharging light components.
Specifically, a heteropolyacid discharge port is arranged in the middle of the rectification tower T2 and connected with a heteropolyacid intermediate storage tank V5, a discharge port of the heteropolyacid intermediate storage tank V5 is connected with an inlet of the primary distillation tower gas-liquid separator Y1, impurity gas in the middle of the rectification tower T2 is discharged through the heteropolyacid discharge port and enters the primary distillation tower gas-liquid separator Y1 again for gas-liquid separation, liquid of the impurity gas enters the primary distillation tower again, and the gas of the impurity gas is cooled and enters the rectification tower again for rectification.
The device also comprises a rectifying gas condenser E7 and a rectifying tower gas-liquid first separator V3, wherein an exhaust port at the top of the rectifying tower T2 is connected with an inlet of the rectifying gas condenser E7, an outlet of the rectifying gas condenser E7 is connected with an inlet of a rectifying tower gas-liquid first separator V3, a liquid discharge port of the rectifying tower gas-liquid first separator V3 is connected with a rectifying tower T2, and a gas outlet of the rectifying tower gas-liquid first separator V3 is an HCL gas discharge port and is connected with an external hydrochloric acid preparation device (the prior art).
The distillation tower further comprises a rectification liquid reboiler E5, the liquid outlet at the bottom of the rectification tower T2 is further connected with the inlet of the rectification liquid reboiler E5, and the outlet of the rectification liquid reboiler E5 is connected with the interior of the rectification tower T2.
The first heat exchange subsystem is used for providing heat exchange energy for the preliminary distillation tower reboiler E2 and the rectifying tower condenser E7; specifically, the first heat exchange subsystem comprises a first fluorine storage device D1, a liquefier E3, a first compressor YS1, a first heat regenerator H1 and a first separator V4, a liquid outlet of the first fluorine storage device D1 is connected with a first inlet of the first separator V4 through a first heat exchange tube in a first dryer G2 and a first heat regenerator H1 in sequence, a liquid outlet of the first separator V4 is connected with an inlet of a heat exchange tube in a rectifying tower condenser E7 through a first circulating pump B1, an outlet of the heat exchange tube in the rectifying tower condenser E7 is connected with a second inlet of the first separator V4, and a top gas outlet of the first separator V4 is connected with an inlet of the first compressor YS1 after passing through a second heat exchange tube in the first heat regenerator H1; an outlet of the first compressor YS1 is connected with an inlet of a liquefier E3 after sequentially passing through heat exchange tubes in a prefractionation liquid reboiler E2, an outlet of the liquefier E3 is connected with a first fluorine storage device D1, and the heat exchange tubes of the liquefier adopt cold water as a heat exchange medium.
The second heat exchange subsystem is used for providing heat exchange energy for the rectification liquid reboiler E5 and the primary gas condenser E1; the second heat exchange subsystem comprises a second fluorine storage device D2, a second compressor YS2, a subcooler E4, a second heat regenerator H2 and a second separator Y2; a liquid outlet of the second fluorine storage device sequentially passes through first heat exchange tubes in a second dryer G2, a subcooler E4 and a second heat regenerator H2 and then is connected with a first inlet of a second separator Y2, a liquid outlet of the second separator Y2 is connected with an inlet of a heat exchange tube of a first gas condenser E1 through a second circulating pump B2, an outlet of the heat exchange tube of the first gas condenser E1 is connected with a second inlet of the second separator Y2, a gas outlet of the second separator Y2 sequentially passes through a second heat exchange tube reboiler of the second heat regenerator H2 and a second compressor YS2 and then is connected with a heat exchange tube in a rectification liquid reboiler E5, and an outlet of the heat exchange tube in the rectification liquid E5 is connected with an inlet of the second fluorine storage device.
In the design, the raw material gas is normal temperature from outside, not less than 0.148MPa (A), 300Nm3H, 62.4% SO2The raw material gas of (1) is a packed tower and is operated under the pressure of 0.148 MPa. Its function is to separate and remove SOCl from raw material gas2Discharging the kettle liquid from the bottom of the tower by using the same heavy components, and obtaining SO-containing components at the top of the tower2The primary distillation liquid is relatively thick.
In the operation of the system, the raw material gas firstly enters the primary tower, and in the primary tower, the raw material gas and the gas gasified from the tower bottom are in countercurrent contact with the reflux liquid from the top of the tower top primary gas condenser E1 from top to bottom on the filler for mass and heat transfer. The descending liquid part is gasified and the SO in the gas2Concentrating, and rising to the top of the column, liquefying part of the rising gas, and collecting SO in the liquid2The concentration is reduced and is reduced to the tower kettle.
In the primary distillation tower, the primary distillation gas rising to the top of the tower is cooled to-17 ℃ by a primary distillation gas condenser E1 and enters a primary distillation tower gas-liquid separator V1, the primary distillation gas in the primary distillation tower gas-liquid separator V1 is partially condensed, and condensate liquid contains SO297 percent (w), flows back (internal reflux) in the primary distillation tower again, and the uncondensed primary distillation gas is 192m3H, containing SO250 percent (v) is pressurized to 0.9MPa (A) by a primary gas compressor, cooled to normal temperature by water by a primary gas cooler and then sent to a rectification system.
In the primary distillation tower, the kettle liquid of the primary distillation tower is subjected to repeated reboiling treatment by a primary distillation tower reboiler E2, the kettle liquid of the primary distillation tower is at 28 ℃ and 9kg/h, and contains SO2～10％、SOCl288.46％、HCl0.6％、H20.80 percent of O is heavy component waste liquid and is discharged outside by utilizing the pressure of the primary distillation tower.
In the design, a rectifying tower is also a packed tower and operates under the pressure of 0.9MPa (A), primary distillation gas from a primary distillation system is cooled by a primary distillation gas cooler and then enters the middle part of the rectifying tower for rectification, the rectifying gas at the top of the tower is condensed by a rectifying gas condenser, most of the rectifying gas is liquefied and enters a rectifying tower gas-liquid first separator V3 at the lower part for gas-liquid separation, condensate liquid of the rectifying tower gas-liquid first separator enters the rectifying tower downwards for reflux (internal reflux), and uncondensed rectifying tail gas is 13m3The hydrochloric acid/h contains 97% of HCl, 3% of Air, and is discharged outside by utilizing the pressure of a rectifying tower to be used as a raw material for preparing the hydrochloric acid, wherein the temperature is-37 ℃.
The liquid in the rectifying tower is food-grade SO252 ℃ to 415kg/h, containing trace HCl-0.2 ppm (w) and Air, is conveyed to the outside by the pressure of a rectifying tower and is used as finished product liquid SO2。
The impurity gas in the middle of the rectifying tower T2 is discharged through a mixed acid discharge port and enters the primary tower gas-liquid separator Y1 again for gas-liquid separation, then the liquid enters the primary tower again, and the gas enters the rectifying tower again for rectification after being cooled.
In the first heat exchange subsystem, high-pressure and high-temperature (1.76MPa (A) and the saturation temperature of 37 ℃) fluorine compressed by a first compressor is used as a heat source of a reboiler of a primary distillation tower to heat kettle liquid, the fluorine is cooled and then enters a liquefier E3 to be liquefied and then enters a fluorine storage device to be stored, liquid in the 157 fluorine storage device enters a first heat regenerator through a first drying tank, and then enters a condenser of a rectification tower to exchange heat with rectification gas at the top of the rectification tower after throttling expansion, so that the rectification gas is condensed, and the cooling water consumption (no cooling water) of the condenser of the rectification tower is saved. After being gasified, the liquid fluorine in the condenser of the rectifying tower passes through a first separator V4, is superheated by a heat regenerator, and then enters a first compressor for pressurization, thereby forming a heat pump circulating system.
In the second heat exchange subsystem, high-pressure and high-temperature (1.57MPa (A) and saturation temperature of 52 ℃) fluorine compressed by a second compressor YS2 is used as a heat source of a reboiler of the rectifying tower to heat kettle liquid, the kettle liquid is completely liquefied and then stored in a second fluorine storage device, liquid in the second fluorine storage device enters a second drying tank into a subcooler E4, the temperature of the liquid is reduced to 37 ℃ by a second heat exchanger, the liquid enters a condenser of the primary distillation tower to exchange heat with primary distillation gas after throttling expansion, and the primary distillation gas is condensed, so that the consumption of cooling water of the condenser of the primary distillation tower is saved (no cooling water is used). And the liquid fluorine in the condenser of the primary distillation tower is gasified and then enters a second compressor for pressurization, so that a heat pump circulating system is formed.
The SO can be completed by the above process2And (4) preparing.
In summary, the food-grade liquid SO of this embodiment2The technological equipment adopts rectification technology to separate SO2, HCL and some heavy components (H2O, SOCL2), the rectification is a distillation method for separating mixture with high purity by utilizing reflux, and is the most widely applied mixture separation operation in industry2O、SOCL2Separating SO from heavy components in a rectifying tower2And HCL, SO2Boiling point of (b): -10 ℃, boiling point of HCL: and the temperature is 85 ℃ below zero, the two can be perfectly separated, high-purity food-grade SO2 is obtained at the bottom of the tower, HCL gas is obtained at the top of the tower, the scheme is feasible and easy to implement, and the process is put into operation and runs well.
The embodiments of the present invention are disclosed as the preferred embodiments, but not limited thereto, and those skilled in the art can easily understand the spirit of the present invention and make various extensions and changes without departing from the spirit of the present invention.
Claims (6)
1. Food-grade liquid SO2A manufacturing system, comprising:
a primary distillation tower with a raw material gas inlet is used for extracting light components of the raw material gas;
the primary distillation gas condenser is connected with a gas outlet at the top of the primary distillation tower and condenses the light components;
the inlet of the primary distillation tower gas-liquid separator is connected with the outlet of the primary distillation gas condenser;
the gas outlet of the gas-liquid separator of the primary distillation tower is communicated with the interior of the distillation tower through a first primary distillation gas compressor, the gas discharged by the gas-liquid separator of the primary distillation tower enters the distillation tower for distillation, and the heavy components rectified by the distillation tower are divided into product liquid SO2And discharging light components.
2. Food grade liquid SO according to claim 12The preparation system is characterized in that: the liquid outlet of the gas-liquid separator of the primary distillation tower is communicated with the interior of the primary distillation tower.
3. Food grade liquid SO according to claim 12The preparation system is characterized in that: the middle part of the rectifying tower is provided with a mixed acid outlet which is connected with a mixed acid intermediate storage tank, and the outlet of the mixed acid intermediate storage tank is connected with the inlet of the gas-liquid separator of the primary distillation tower.
4. Food grade liquid SO according to claim 12The preparation system is characterized in that: the device also comprises a rectifying gas condenser and a rectifying tower gas-liquid first separator, wherein an exhaust port at the top of the rectifying tower is connected with an inlet of the rectifying gas condenser, an outlet of the rectifying gas condenser is connected with an inlet of the rectifying tower gas-liquid first separator, a liquid discharge port of the rectifying tower gas-liquid first separator is connected with the rectifying tower, and a gas outlet of the rectifying tower gas-liquid first separator is an HCL gas discharge port and is connected with an external hydrochloric acid preparation device.
5. Food grade liquid SO according to claim 42The preparation system is characterized in that: the distillation tower further comprises a distillation liquid reboiler, a liquid outlet at the bottom of the distillation tower is also connected with an inlet of the distillation liquid reboiler, and an outlet of the distillation liquid reboiler is connected with an outlet of the distillation liquid reboilerThe tower is internally connected.
6. Food grade liquid SO according to claim 52The preparation system is characterized in that: still include the initial distillation liquid reboiler, the liquid export of initial distillation tower bottom and the access connection of initial distillation liquid reboiler, the export and the initial distillation tower access connection of initial distillation liquid reboiler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021656230.0U CN214059913U (en) | 2020-08-11 | 2020-08-11 | Food grade liquid SO2Preparation system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021656230.0U CN214059913U (en) | 2020-08-11 | 2020-08-11 | Food grade liquid SO2Preparation system |
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| Publication Number | Publication Date |
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| CN214059913U true CN214059913U (en) | 2021-08-27 |
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| CN202021656230.0U Expired - Fee Related CN214059913U (en) | 2020-08-11 | 2020-08-11 | Food grade liquid SO2Preparation system |
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| Country | Link |
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- 2020-08-11 CN CN202021656230.0U patent/CN214059913U/en not_active Expired - Fee Related
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Granted publication date: 20210827 |