CN217139235U - Hydrochloric acid distillation system in pinacolone production process - Google Patents
Hydrochloric acid distillation system in pinacolone production process Download PDFInfo
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- CN217139235U CN217139235U CN202220459137.3U CN202220459137U CN217139235U CN 217139235 U CN217139235 U CN 217139235U CN 202220459137 U CN202220459137 U CN 202220459137U CN 217139235 U CN217139235 U CN 217139235U
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Abstract
The utility model discloses a hydrochloric acid distillation system in pinacolone production process, this hydrochloric acid distillation system includes the stock solution jar, stock solution jar and pre-heater intercommunication, pre-heater and analytic top of the tower portion intercommunication, analytic bottom of the tower and reboiler intercommunication, the middle part of analytic tower be provided with the overflow mouth and with the hydrochloric acid and the stock solution heat transfer of pre-heater intercommunication messenger high temperature, pre-heater and dilute acid cooler intercommunication, dilute acid cooler and dilute acid jar intercommunication, the top of analytic tower is provided with the gas phase export, this gas phase export and recovery water cooler intercommunication, the pipeline of giving vent to anger and the hydrogen chloride absorption system intercommunication of recovery water cooler, the bottom of recovery water cooler is provided with the liquid phase export, this liquid phase export and organic matter cooler intercommunication, organic matter cooler and receiving tank intercommunication. This hydrochloric acid distillation system can be continuous distill hydrochloric acid stoste, makes pinacolone separate from the stoste, and entire system reasonable has utilized heat energy, has saved the energy.
Description
Technical Field
The utility model relates to a hydrochloric acid distillation system in pinacolone production process belongs to pinacolone production technical field.
Background
The existing pinacolone hydrochloric acid distillation technology uses an enamel reaction kettle to carry out intermittent operation, in the reaction operation process, hydrochloric acid separated from the front section is directly put into the reaction kettle, a reaction kettle jacket is heated by steam, and the hydrochloric acid in the kettle is distilled. After the distillation is finished by heating, a steam valve of the reaction kettle is closed, the hydrochloric acid is cooled to below 50 ℃ by opening cooling water, and then the hydrochloric acid is discharged, so that the whole process has no heat recovery, the field operation amount is large, and workers need to frequently adjust the valve to operate. Hydrochloric acid can have high boiling point organic matter in hydrochloric acid after high temperature distillation, this organic matter is the tar form, and density is less than hydrochloric acid, and owing to adopted this kind of intermittent type formula operation, lead to the tar form organic matter easily to glue on the pipeline wall after the temperature is low, the acid of clearance reation kettle evaporates, this organic tar form liquid can stratify to the hydrochloric acid upper strata in hydrochloric acid cooling process after the blowing, flow reation kettle at the blowing in-process at last, because the reduction of temperature is very easily hung the wall and forms the jam of pipeline valve on valve and pipeline.
SUMMERY OF THE UTILITY MODEL
The utility model discloses the technical problem that will solve is: the hydrochloric acid distillation system can be used for continuously distilling the hydrochloric acid stock solution to separate the pinacolone from the stock solution, and the whole system reasonably utilizes heat energy and saves energy.
In order to solve the technical problem, the technical scheme of the utility model is that: a hydrochloric acid distillation system in the production process of pinacolone comprises a raw liquid tank, wherein a discharge port of the raw liquid tank is connected with a raw liquid supply pipeline, a raw liquid pump is arranged on the raw liquid supply pipeline, the downstream end of the raw liquid supply pipeline is communicated with an inlet of a first heat exchange medium channel of a preheater, an outlet of the first heat exchange medium channel of the preheater is communicated with a raw liquid feeding port at the top of a desorption tower through a pipeline, a raw liquid circulating liquid outlet at the bottom of the desorption tower is communicated with a raw liquid circulating inlet of a reboiler through a liquid outlet circulating pipeline, a raw liquid circulating outlet of the reboiler is communicated with a raw liquid circulating liquid inlet of the desorption tower through a liquid inlet circulating pipeline, a heating system for heating the inside is arranged on the reboiler, an overflow port is arranged in the middle of the desorption tower and is communicated with an inlet of a second heat exchange medium channel of the preheater through an overflow pipeline, the export of the second heat transfer medium passageway of pre-heater and the diluted acid entry intercommunication of diluted acid cooler, the diluted acid export of diluted acid cooler and the collection mouth intercommunication of diluted acid jar, diluted acid cooler and first cooling system intercommunication, the top of desorption tower is provided with the gaseous phase export, and this gaseous phase export passes through distillation gaseous phase pipeline and retrieves water cooler intercommunication, retrieves the pipeline of giving vent to anger and the hydrogen chloride absorption system intercommunication of water cooler, retrieves water cooler and second cooling system intercommunication, the bottom of retrieving the water cooler is provided with the liquid phase export, and this liquid phase export communicates with the organic matter medium passageway entry of organic matter cooler, the organic matter medium passageway export and the receiving tank intercommunication of organic matter cooler, the organic matter cooler is connected with third cooling system.
As a preferred scheme, be fixed with sour liquid distributor in the analytic tower, sour liquid distributor is in the top of analytic tower, sour liquid distributor and stoste filling opening intercommunication, be provided with a plurality of on the sour liquid distributor and spray the hole.
As a preferred scheme, the sour liquid distributor includes the annular tube, be provided with feed liquor communicating pipe on the annular tube, this feed liquor communicating pipe and stoste filling opening intercommunication, the annular tube welding is in the analytic tower, be provided with intercrossing's cross pipe on the annular tube, the bottom of cross pipe and annular tube is provided with a plurality of spray the hole.
Preferably, the desorption tower is provided with a time delay packing structure below the acid liquid distributor, and the time delay packing structure is used for increasing the heat exchange time between liquid and gas.
As a preferable scheme, the time-delay packing structure comprises a packing cylinder fixed in the desorption tower, at least two layers of grid plates are arranged in the packing cylinder, and a plurality of spherical packings are arranged in the area between the grid plates.
As a preferable scheme, a supporting cylinder is arranged between two layers of grid plates in the packing cylinder, and a supporting step is fixed below the grid plate at the lowest layer in the packing cylinder.
As a preferable scheme, the distillation gas phase pipeline is communicated with the top of the recovery water cooler, and the gas outlet pipeline of the recovery water cooler is arranged at the lower part and is positioned above the liquid phase outlet of the recovery water cooler.
Preferably, the raw liquid supply line is provided with a flow meter, and thermometers are installed at the bottom and the top of the desorption tower.
After the technical scheme is adopted, the utility model discloses an effect is: compared with the prior intermittent distillation, the hydrochloric acid distillation system has the following advantages: 1. the distillation system can automatically and continuously realize the distillation of hydrochloric acid, the temperature of the tar of the organic matters in the desorption tower is higher, the tar and the hydrochloric acid can be discharged together, and the phenomenon that the tar wall is hung to block a pipeline valve after the pipeline valve which runs discontinuously is cooled can be avoided; 2. the distillation system utilizes the preheater to preheat the hydrochloric acid stock solution in the distillation process, and absorbs the heat in the hydrochloric acid solution overflowing from the desorption tower; meanwhile, the reboiler is utilized to circularly heat the hydrochloric acid solution in the desorption tower, the gasified hydrogen chloride gas and the pinacolone are heated to flow upwards in the desorption tower, and the gas and the stock solution flowing into the upper end of the desorption tower exchange heat, so that the gas-phase medium is cooled and the stock solution is heated, the heat is fully utilized in the whole process, and the energy is saved.
And because the acid liquid distributor is fixed in the analysis tower and is positioned at the top of the analysis tower, the acid liquid distributor is communicated with the stock solution filling opening, a plurality of spraying holes are formed in the acid liquid distributor, and the stock solution can be uniformly sprayed by using the acid liquid distributor, so that the acid liquid distributor is more uniformly contacted with a gas-phase medium, and the heat exchange efficiency is higher.
Because again the sour liquid distributor includes the annular tube, be provided with feed liquor communicating pipe on the annular tube, this feed liquor communicating pipe and stoste filling opening intercommunication, the annular tube welding is in analytic tower, be provided with intercrossing's crossover pipe on the annular tube, the bottom of crossover pipe and annular tube is provided with a plurality of spray the hole, this sour liquid distributor can be more even spray the acidizing fluid.
And because the analysis tower is arranged below the acid liquid distributor and is provided with the time delay filler structure for increasing the heat exchange time between the liquid and the gas, the time delay filler structure can prolong the heat exchange time between the liquid and the gas, thereby improving the recovery and utilization rate of heat energy.
And because the time-delay packing structure comprises a packing cylinder fixed in the desorption tower, at least two layers of grid plates are arranged in the packing cylinder, and a plurality of spherical packings are arranged in the area between the grid plates, the time-delay packing structure can simply and effectively disperse and fully contact gas and liquid, the gas can be separated into a plurality of repeated gases after passing through the grid plates, the gas can reduce the speed after entering the gaps of the spherical packings, and the flowing direction is changed, so that the contact time is prolonged, and the heat exchange rate is higher.
And the distillation gas phase pipeline is communicated with the top of the recovery water cooler, and the gas outlet pipeline of the recovery water cooler is arranged at the lower part and is positioned above the liquid phase outlet of the recovery water cooler, so that gas-phase media enter from the top of the recovery water cooler, flow downwards and flow out from the bottom after being cooled by the water cooler, the pinacolone is condensed and flows out from the bottom, and hydrogen chloride gas flows out from the gas outlet pipeline at the lower part, thereby realizing the full separation of the media.
And because the stock solution supply pipeline is provided with the flowmeter, thermometers are arranged at the tower bottom and the tower top of the desorption tower, so that the flow and the temperature of a reboiler can be more intuitively controlled through the flowmeter and the thermometers, and the fact that the pinacolone in the acid distillation can be completely distilled is ensured.
In addition the utility model also discloses a hydrochloric acid distillation technology in the pinacolone production process, this hydrochloric acid distillation technology has used the above-mentioned hydrochloric acid distillation system that records in, including following step:
s1, conveying the stock solution in the stock solution tank to the top of the analysis tower by using a stock solution pump;
s2, enabling the stock solution to flow out of the lower end of the desorption tower and enter a reboiler;
s3, the hydrochloric acid heated by the reboiler flows back to the desorption tower, the pinacolone and part of the hydrochloric acid in the stock solution are heated and gasified and flow upwards to be led out from a gas phase outlet at the upper end of the desorption tower, and the gas phase medium and the inflowing stock solution are subjected to contact heat exchange in the desorption tower; redundant hydrochloric acid solution in the desorption tower overflows into an overflow pipeline;
s4, cooling the gas-phase medium in a recovery water cooler, cooling and liquefying the pinacolone in the gas-phase medium in the recovery water cooler, flowing out, cooling by an organic matter cooler and collecting; hydrogen chloride in the gas phase medium passes through an air outlet pipeline of the recovery water cooler and is absorbed by a hydrogen chloride absorption system;
s5, exchanging heat between the hydrochloric acid solution in the overflow pipeline and the stock solution conveyed by the stock solution pump in the step S1 in a preheater;
and S6, refluxing the hydrochloric acid solution subjected to heat exchange into a dilute acid tank for collection.
Preferably, an acid liquid distributor and a time-delay filler structure are arranged in the desorption tower, and in step S2, the stock solution passes through the time-delay filler structure after being sprayed by the acid liquid distributor in the desorption tower; the gas phase medium flows upwards and passes through the gaps between the grid plate and the spherical filler to exchange heat with the stock solution, and the stock solution can be sprayed more uniformly by the method to perform heat exchange with the gas phase medium
After the technical scheme is adopted, the utility model discloses an effect is: the distillation process uses the distillation system, can continuously realize the distillation of the hydrochloric acid stock solution, is convenient for continuously and thoroughly recovering the pinacolone, simultaneously avoids the blockage caused by the adhesion of organic tar on the pipeline wall and a valve due to the cooling of the organic tar, simultaneously fully recovers the heat energy in the medium, and saves the energy.
Drawings
The present invention will be further explained with reference to the drawings and examples.
FIG. 1 is a system diagram of the structure of an embodiment of the present invention;
fig. 2 is a schematic structural diagram of an acid liquid distributor according to an embodiment of the present invention;
FIG. 3 is a cross-sectional view of the time delay filler structure according to an embodiment of the present invention;
in the drawings: 1. a stock solution tank; 2. a stock solution pump; 3. a preheater; 4. a stock solution supply line; 5. a resolution tower; 6. a reboiler; 7. a liquid inlet circulation pipeline; 8. a liquid outlet circulation pipeline; 9. an overflow conduit; 10. a dilute acid cooler; 11. a dilute acid tank; 12. a distillation gas phase conduit; 13. recovering the water cooler; 14. an organic medium channel; 15. an air outlet pipe; 16. an organic matter cooler; 17. an acid liquid distributor; 171. an annular tube 171; 172. a crossover tube 172; 173. a liquid inlet communicating pipe; 174. spraying holes; 18. a time-delayed filler structure; 181. a packing cylinder; 182. a support cylinder; 183. a grid plate; 184. a spherical filler; 185. and supporting the step.
Detailed Description
The present invention will be described in further detail with reference to the following examples.
As shown in fig. 1 to 3, a hydrochloric acid distillation system in the pinacolone production process comprises a raw liquid tank 1, wherein a discharge port of the raw liquid tank 1 is connected with a raw liquid supply pipeline 4, a raw liquid pump 2 is arranged on the raw liquid supply pipeline 4, a downstream end of the raw liquid supply pipeline 4 is communicated with an inlet of a first heat exchange medium channel of a preheater 3, an outlet of the first heat exchange medium channel of the preheater 3 is communicated with a raw liquid inlet at the top of a desorption tower 5 through a pipeline, a raw liquid circulation liquid outlet at the bottom of the desorption tower 5 is communicated with a raw liquid circulation inlet of a reboiler 6 through a liquid outlet circulation pipeline 8, a raw liquid circulation outlet of the reboiler 6 is communicated with a raw liquid circulation liquid inlet of the desorption tower 5 through a liquid inlet circulation pipeline 7, the reboiler 6 is provided with a heating system for heating the inside, and the heating system adopts steam for heating, the stock solution supply pipeline 4 is provided with a flow meter, thermometers are installed at the tower bottom and the tower top of the desorption tower 5, the thermometers can adopt remote digital display thermometers, and thus a remote control console can control the flow and the temperature of the reboiler 6 more visually through the flow meter and the thermometers, so that the fact that pinacolone can be completely distilled out in acid distillation is guaranteed.
The middle part of the desorption tower 5 is provided with an overflow port, the overflow port is communicated with an inlet of a second heat exchange medium channel of the preheater 3 through an overflow pipeline 9, wherein a region between an overflow port and a stock solution circulating liquid outlet at the bottom of the desorption tower 5 is used for ensuring a hydrochloric acid solution with enough liquid level, the reboiler 6 is heated by steam, the hydrochloric acid solution is boiled, and the hydrochloric acid with high temperature enters the desorption tower 5 from a liquid inlet circulating pipeline 7 above and naturally circulates through thermosiphon.
The outlet of the second heat exchange medium channel of the preheater 3 is communicated with the dilute acid inlet of the dilute acid cooler 10, the dilute acid outlet of the dilute acid cooler 10 is communicated with the collecting port of the dilute acid tank 11, the dilute acid cooler 10 is communicated with the first cooling system, the first cooling system adopts circulating water for cooling, the top of the desorption tower 5 is provided with a gas phase outlet, the gas phase outlet is communicated with a recovered water cooler 13 through a distilled gas phase pipeline 12, a gas outlet pipeline 15 of the recovered water cooler 13 is communicated with a hydrogen chloride absorption system, the recovered water cooler 13 is communicated with the second cooling system, similarly, the second cooling system also adopts circulating water for cooling, the bottom of the recovered water cooler 13 is provided with a liquid phase outlet, the liquid phase outlet is communicated with the inlet of the organic matter medium channel 14 of the organic matter cooler 16, the outlet of the organic matter medium channel 14 of the organic matter cooler 16 is communicated with the receiving tank, the organic matter cooler 16 is connected with a third cooling system, and the third cooling system is also cooled by circulating water.
The acid liquid distributor 17 is fixed in the desorption tower 5, the acid liquid distributor 17 is arranged at the top of the desorption tower 5, the acid liquid distributor 17 is communicated with the stock solution filling opening, and the acid liquid distributor 17 is provided with a plurality of spraying holes 174. The acid liquor distributor 17 comprises an annular pipe 171, a liquid inlet communicating pipe 173 is arranged on the annular pipe 171, the liquid inlet communicating pipe 173 is communicated with a stock solution filling opening, the annular pipe 171 is welded in the desorption tower 5, a cross pipe 172 which is mutually crossed is arranged on the annular pipe 171, and a plurality of spraying holes 174 are formed in the bottoms of the cross pipe 172 and the annular pipe 171. The stock solution enters the acid solution distributor 17 and then sprays a plurality of water columns on the layer through the spraying holes 174, so that the stock solution can be conveniently contacted with a gas-phase medium for heat exchange.
The desorption tower 5 is provided with a time delay filler structure 18 for increasing the heat exchange time between the liquid and the gas below the acid liquid distributor 17. In this embodiment, the time-delay filler structure 18 includes a filler cylinder 181 fixed in the desorption tower 5, at least two layers of grid plates 183 are disposed in the filler cylinder 181, and a plurality of spherical fillers 184 are disposed in an area between the grid plates 183. A supporting cylinder 182 is arranged between two layers of grid plates 183 in the packing cylinder 181, and a supporting step 185 is fixed below the grid plate 183 at the lowest layer in the packing cylinder 181. And the inside of the desorption tower 5 is welded with a support ring, so that the whole packing cylinder 181 can be freely put into the support ring to be supported, the grid plate 183 can be optimized according to the actual heat exchange requirement, and the grid plate 183 can be flexibly arranged by arranging one or more support cylinders 182.
The distillation gas phase pipeline 12 is communicated with the top of the recovered water cooler 13, and the gas outlet pipeline 15 of the recovered water cooler 13 is arranged at the lower part and is positioned above the liquid phase outlet of the recovered water cooler 13.
The utility model discloses a hydrochloric acid distillation system compares present interval distillation and has following advantage: 1. the distillation system can automatically and continuously realize the distillation of hydrochloric acid, the temperature of the tar of the organic matters in the desorption tower 5 is higher, and the tar and the hydrochloric acid can be discharged together, so that the phenomenon that the tar wall is hung to block a pipeline valve after the pipeline valve which runs discontinuously is cooled can be avoided; 2. the distillation system utilizes the preheater 3 to preheat the hydrochloric acid stock solution in the distillation process, and absorbs the heat in the hydrochloric acid solution overflowing from the desorption tower 5; meanwhile, the reboiler 6 is utilized to circularly heat the hydrochloric acid solution in the desorption tower 5, the gasified hydrogen chloride gas and the pinacolone are heated to flow upwards in the desorption tower 5, and the gas and the stock solution flowing into the upper end of the desorption tower 5 exchange heat, so that the gas-phase medium is cooled and the stock solution is heated, the heat is fully utilized in the whole process, and the energy is saved.
In addition the embodiment of the utility model provides a still disclose hydrochloric acid distillation process in the pinacolone production process, this hydrochloric acid distillation process has used the hydrochloric acid distillation system of above-mentioned record, including following step:
s1, conveying the stock solution in the stock solution tank 1 to the top of the analysis tower 5 by using the stock solution pump 2, wherein the flow of the stock solution in the conveying process is controllable;
s2, enabling the stock solution to flow out of the lower end of the desorption tower 5 and enter a reboiler 6;
s3, the hydrochloric acid heated by the reboiler 6 flows back to the desorption tower 5, the pinacolone and partial hydrochloric acid in the stock solution are heated and gasified and flow upwards to be led out from a gas phase outlet at the upper end of the desorption tower 5, and the gas phase medium is in contact heat exchange with the inflowing stock solution in the desorption tower 5; the redundant hydrochloric acid solution in the desorption tower 5 overflows into an overflow pipeline 9;
s4, cooling the gas-phase medium in the recovered water cooler 13, cooling and liquefying the pinacolone in the gas-phase medium in the recovered water cooler 13, flowing out, cooling by the organic matter cooler 16 and collecting; hydrogen chloride in the gas phase medium passes through an air outlet pipeline 15 of the recycling water cooler 13 and is absorbed by a hydrogen chloride absorption system;
s5, exchanging heat between the hydrochloric acid solution in the overflow pipeline 9 and the stock solution conveyed by the stock solution pump 2 in the step S1 in a preheater 3;
and S6, refluxing the hydrochloric acid solution subjected to heat exchange into the dilute acid tank 11 for collection.
Preferably, an acid liquid distributor 17 and a time-delay filler structure 18 are arranged inside the desorption tower 5, and in step S2, the stock solution passes through the time-delay filler structure 18 after being sprayed by the acid liquid distributor 17 inside the desorption tower 5; the gas phase medium flows upwards and passes through the gaps between the grid plates 183 and the spherical fillers 184 to exchange heat with the stock solution, and the stock solution can be sprayed more uniformly with the gas phase medium by the method
The distillation process uses the distillation system, can continuously realize the distillation of the hydrochloric acid stock solution, is convenient for continuously and thoroughly recovering the pinacolone, simultaneously avoids the blockage caused by the adhesion of organic tar on the pipeline wall and a valve due to the cooling of the organic tar, simultaneously fully recovers the heat energy in the medium, and saves the energy.
In this embodiment, the pre-heater is because the heating cooling material all is strong corrosive hydrochloric acid, and its inside heat transfer passageway all adopts corrosion resistant graphite material, and other reboiler and cooler can select graphite material or carbon steel material according to the demand of reality.
The pipeline that circulates between this device reboiler and the desorption tower has adopted high temperature resistant and corrosion-resistant steel lining tetrafluoro pipe, and all the other each takeovers have adopted corrosion-resistant PPR pipe or PP pipe, guarantee the safe long-term operation of device.
The above-mentioned embodiments are only descriptions of the preferred embodiments of the present invention, and are not intended to limit the scope of the present invention, and all modifications and changes made by the technical solution of the present invention should fall within the protection scope defined by the claims of the present invention on the basis of not departing from the spirit of the present invention.
Claims (8)
1. The utility model provides a hydrochloric acid distillation system in pinacolone production process, includes the stoste jar, the discharge gate of stoste jar is connected with stoste supply line, is provided with stoste pump, its characterized in that on this stoste supply line: the downstream end of the stock solution supply pipeline is communicated with the inlet of a first heat exchange medium channel of the preheater, the outlet of the first heat exchange medium channel of the preheater is communicated with a stock solution filling opening at the top of the analysis tower through a pipeline, a stock solution circulating liquid outlet at the bottom of the analysis tower is communicated with a stock solution circulating inlet of a reboiler through a liquid outlet circulating pipeline, the stock solution circulating outlet of the reboiler is communicated with the stock solution circulating liquid inlet of the analysis tower through a liquid inlet circulating pipeline, a heating system for heating the inside is arranged on the reboiler, an overflow opening is arranged at the middle part of the analysis tower and is communicated with the inlet of a second heat exchange medium channel of the preheater through an overflow pipeline, the outlet of the second heat exchange medium channel of the preheater is communicated with a dilute acid inlet of a dilute acid cooler, and the dilute acid outlet of the dilute acid cooler is communicated with a collecting opening of a dilute acid tank, the dilute acid cooler is communicated with the first cooling system, a gas phase outlet is formed in the top of the desorption tower, the gas phase outlet is communicated with a recovery water cooler through a distillation gas phase pipeline, an air outlet pipeline of the recovery water cooler is communicated with a hydrogen chloride absorption system, the recovery water cooler is communicated with the second cooling system, a liquid phase outlet is formed in the bottom of the recovery water cooler, the liquid phase outlet is communicated with an organic matter medium channel inlet of the organic matter cooler, the organic matter medium channel outlet of the organic matter cooler is communicated with the receiving tank, and the organic matter cooler is connected with a third cooling system.
2. The hydrochloric acid distillation system in the pinacolone production process of claim 1, wherein: the acid liquid distributor is fixed in the analysis tower and is positioned at the top of the analysis tower, the acid liquid distributor is communicated with the stock solution filling opening, and a plurality of spraying holes are formed in the acid liquid distributor.
3. The hydrochloric acid distillation system in the pinacolone production process of claim 2, wherein: the sour liquid distributor includes the annular tube, be provided with feed liquor communicating pipe on the annular tube, this feed liquor communicating pipe and stoste filling opening intercommunication, the annular tube welding is in the analytic tower, be provided with intercrossing's crossover pipe on the annular tube, the bottom of crossover pipe and annular tube is provided with a plurality of spray the hole.
4. The hydrochloric acid distillation system in the pinacolone production process according to claim 3, wherein: and a time delay filler structure for increasing the heat exchange time between liquid and gas is arranged below the acid liquid distributor of the desorption tower.
5. The hydrochloric acid distillation system in the pinacolone production process of claim 4, wherein: the time-delay packing structure comprises a packing cylinder fixed in the desorption tower, at least two layers of grid plates are arranged in the packing cylinder, and a plurality of spherical packings are arranged in the area between the grid plates.
6. The hydrochloric acid distillation system in the pinacolone production process of claim 5, wherein: a supporting cylinder is arranged between two layers of grid plates in the packing cylinder, and a supporting step is fixed below the grid plate at the lowest layer in the packing cylinder.
7. The hydrochloric acid distillation system in the pinacolone production process of claim 6, wherein: the distillation gas phase pipeline is communicated with the top of the recovery water cooler, and the gas outlet pipeline of the recovery water cooler is arranged at the lower part and is positioned above the liquid phase outlet of the recovery water cooler.
8. The hydrochloric acid distillation system in the pinacolone production process of claim 7, wherein: and a flowmeter is arranged on the stock solution supply pipeline, and thermometers are arranged at the tower bottom and the tower top of the desorption tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220459137.3U CN217139235U (en) | 2022-03-04 | 2022-03-04 | Hydrochloric acid distillation system in pinacolone production process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220459137.3U CN217139235U (en) | 2022-03-04 | 2022-03-04 | Hydrochloric acid distillation system in pinacolone production process |
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| CN217139235U true CN217139235U (en) | 2022-08-09 |
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