CN210065171U - Chlorosulfonic acid production system - Google Patents
Chlorosulfonic acid production system Download PDFInfo
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- CN210065171U CN210065171U CN201920447760.5U CN201920447760U CN210065171U CN 210065171 U CN210065171 U CN 210065171U CN 201920447760 U CN201920447760 U CN 201920447760U CN 210065171 U CN210065171 U CN 210065171U
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Abstract
The utility model discloses a chlorosulfonic acid production system, including raw materials HCl production unit, raw materials SO3Production unit, tail gas treatment unit, raw material HCl production unit and raw material SO3The production unit and the tail gas treatment unit are connected with each other, and the synthesis unit comprises a synthesis tower, a first ground groove for collecting finished products prepared by the synthesis tower, a refining tower and a second ground groove for collecting refined products; the top of the refining tower is provided with an HCl discharge pipeline, the upper part of the refining tower is provided with a finished chlorosulfonic acid feed pipeline, the lower part of the refining tower is provided with a refined product discharge pipeline, and the bottom of the refining tower is provided with an HCl feed pipeline; the top of the synthesis tower is provided with a gaseous chlorosulfonic acid discharge pipeline, the upper part is provided with a liquid chlorosulfonic acid feed pipeline, and the lower part is provided with a liquid chlorosulfonic acid discharge pipelineThe method comprises a raw material feeding pipeline and a liquid chlorosulfonic acid discharging pipeline, wherein the liquid chlorosulfonic acid is produced in a synthesis tower and is refined without arranging a branch pipeline in the conveying process of the raw material HCl.
Description
Technical Field
The utility model relates to a chemical industry field, concretely relates to chlorosulfonic acid safety production system.
Background
The chlorosulfonic acid is mainly used for preparing saccharin, producing sulfa drug, synthesizing dye and dye intermediate and sulfonating alkylbenzene which is used for synthesizing raw material of detergent; also used for producing pesticides and smoke screen agents. SO is used in the traditional chlorosulfonic acid production process3And synthesizing with HCl in gas phase to obtain chlorosulfonic acid. Wherein the starting HCl is passed over Cl2、H2Prepared by burning in an HCl synthesis furnace, SO3By roasting sulphur or pyrite, first SO is prepared2，SO2Obtaining SO by catalytic oxidation3Thus SO3The concentration is not more than 9 percent, and is generally only about 7 percent. SO (SO)3The concentration is low, which not only affects the quality of chlorosulfonic acid synthesis, but also causes the equipment increase, the investment is huge and the maintenance is complicated in daily production when the tail gas is treated. In order to increase SO3In the concentration of (A) and (B) in the production of SO from fuming sulfuric acid3The production capacity is greatly increased, and the corresponding equipment maintenance and updating cost is greatly reduced. More importantly, the product quality can be greatly improved, and the product has great market competitiveness along with the improvement of the quality and the yield.
In addition, the low-concentration hydrogen chloride gas generated by the Mannheim furnace in the industry is cooled and dried to become gas containing 45% of hydrogen chloride and 0.06% of moisture. The gas is sent into a synthesis tower by a draught fan, and reacts with the gas containing 7.5 percent of sulfur trioxide from the conversion section of a sulfuric acid device at a certain temperature and pressure to generate chlorosulfonic acid gas, and the chlorosulfonic acid gas is condensed and separated. Containing part of SO3And the tail gas of HCl is discharged after being treated by a tail gas absorption system.
SO3The production of chlorosulfonic acid by gas phase synthesis with HCl is commonly used, for example, patent application No. 201720299875.5 discloses a gas phase synthesis apparatus for chlorosulfonic acid from pure sulfur trioxide, HCl and SO being in a synthesis tower3And (2) performing mixing reaction by using a multi-stage baffle plate to prepare gaseous chlorosulfonic acid, condensing the gaseous chlorosulfonic acid by using a two-stage condenser, then feeding the condensed gaseous chlorosulfonic acid into a ground tank, conveying the condensed gaseous chlorosulfonic acid to a heat exchanger by using a pump, cooling, and then feeding the cooled gaseous chlorosulfonic acid into an auxiliary absorption tower for refining to obtain a finished product. The chlorosulfonic acid produced by the device in the synthesis tower is in gaseous state, becauseThe raw material HCl enters the auxiliary absorption tower through a branch path, the HCl consumption is not easy to control, the HCl in the tail gas is increased, and the pressure of tail gas treatment is increased.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model provides a chlorosulfonic acid production system obtains the chlorosulfonic acid of liquid form at the inside production of synthetic tower, and raw materials HCl need not set up the branch pipeline again and carries and be used for the refining, reduces the HCl in the tail gas, improves refining efficiency.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a chlorosulfonic acid production system comprises a raw material HCl production unit and a raw material SO3Production unit, tail gas treatment unit, raw material HCl production unit and raw material SO3The production unit and the tail gas treatment unit are connected with each other, and the synthesis unit comprises a synthesis tower, a first ground groove for collecting finished products prepared by the synthesis tower, a refining tower and a second ground groove for collecting refined products;
the top of the refining tower is provided with an HCl discharge pipeline, the upper part of the refining tower is provided with a finished chlorosulfonic acid feed pipeline, the lower part of the refining tower is provided with a refined product discharge pipeline, and the bottom of the refining tower is provided with an HCl feed pipeline;
the top of the synthesis tower is provided with a gaseous chlorosulfonic acid discharge pipeline, the upper part of the synthesis tower is provided with a liquid chlorosulfonic acid feed pipeline, and the lower part of the synthesis tower is provided with a raw material feed pipeline and a liquid chlorosulfonic acid discharge pipeline;
the HCl discharge pipeline at the top of the refining tower is communicated with a raw material feeding pipeline of the synthesis tower, the other end of a gaseous chlorosulfonic acid discharge pipeline of the synthesis tower is communicated with a cooler, the cooler is communicated with a first ground groove through a pipeline, the first ground groove is communicated with the synthesis tower through a liquid chlorosulfonic acid feeding pipeline and a liquid chlorosulfonic acid discharge pipeline of the synthesis tower respectively, and a first circulating pump is arranged on the liquid chlorosulfonic acid feeding pipeline of the synthesis tower;
the first ground groove is communicated with the refining tower through a finished product chlorosulfonic acid feeding pipeline, a finished product circulating pump is arranged on the finished product chlorosulfonic acid feeding pipeline, and the refining tower is communicated with the second ground groove through a refined product discharging pipeline.
SO3And HCl enters the synthesis tower through a raw material feeding pipeline of the synthesis tower according to the volume ratio of 1.05: 1, and chlorosulfonic acid is formed through synthetic reaction in a packed bed of the synthesis tower. Gaseous chlorosulfonic acid enters a cooler from a gaseous chlorosulfonic acid discharge pipeline at the top of the synthesis tower and is condensed into liquid chlorosulfonic acid, and then the liquid chlorosulfonic acid enters a first ground tank through a liquid chlorosulfonic acid discharge pipeline. The liquid chlorosulfonic acid in the synthesis tower enters a first ground tank from a liquid chlorosulfonic acid discharge pipeline arranged at the lower part of the synthesis tower. And liquid chlorosulfonic acid in the first ground groove enters the upper part of the synthesis tower through a liquid chlorosulfonic acid feeding pipeline, is adsorbed in the synthesis tower from top to bottom, and enters the first ground groove through a liquid chlorosulfonic acid discharging pipeline again after adsorption is finished to obtain a chlorosulfonic acid finished product. The first ground groove is conveyed into the refining tower through a finished product chlorosulfonic acid feeding pipeline and a finished product circulating pump arranged on the finished product chlorosulfonic acid feeding pipeline. In the refining tower, the by-product of chlorosulfonic acid reacts with HCl from the HCl production unit to produce chlorosulfonic acid and SO3The purpose of refining is achieved. The chlorosulfonic acid refined by the refining tower enters a second ground tank through a refined product discharge pipeline. Finally transported to the chlorosulfonic acid tank area through a second ground tank.
Compared with the prior art, the utility model, following beneficial effect has:
HCl is added without independently arranging a branch pipeline, HCl directly generated from an HCl production unit is adopted to be adsorbed and reacted with finished chlorosulfonic acid in a refining tower, so that chlorosulfonic acid produced by a byproduct in the chlorosulfonic acid is refined, HCl with the maximum concentration in the system is used for refining, control conditions in the refining process are reduced, refining conditions are simplified, the purity of the refined chlorosulfonic acid is higher than 97%, and the national first-grade product requirement is met; and a HCl branch is not required to be arranged for refining, so that the concentration of HCl in tail gas is reduced.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure, the raw material SO3Production unit 1, raw material HCl production unit 2, tail gas treatment unit 3, synthetic tower 4, refining tower 5, first geosyncline 6, second geosyncline 7, first defroster8. The system comprises a second demister 9, a flow meter 10, a cooler 11, a separator 12, a demister 13, an HCl washing tower 31, an acid washing tower 32, a water washing tower 33, a sulfuric acid plant tail gas treatment tower 34, a raw material feeding pipeline 41, a gaseous chlorosulfonic acid discharge pipeline 42, a liquid chlorosulfonic acid feeding pipeline 43, a liquid chlorosulfonic acid discharge pipeline 44, a first spray device 45, a second spray device 46, an HCl discharge pipeline 51, a refined product discharge pipeline 52, an HCl feeding pipeline 53, a finished product chlorosulfonic acid feeding pipeline 54, a first circulating pump 61, a finished product circulating pump 62 and a refined chlorosulfonic acid delivery port 71.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings, and specific embodiments will be given.
As shown in figure 1, a chlorosulfonic acid production system comprises a raw material HCl production unit 2 and a raw material SO3Production unit 1, tail gas treatment unit 3, raw material HCl production unit 2 and raw material SO3The production unit 1 and the tail gas treatment unit 3 are connected with each other, and the synthesis unit comprises a synthesis tower 4, a first ground tank 6 for collecting finished products prepared by the synthesis tower 4, a refining tower 5 and a second ground tank 7 for collecting refined products;
the top of the refining tower 5 is provided with an HCl discharge pipeline 51, the upper part is provided with a finished chlorosulfonic acid HCl feed pipeline 53, the lower part is provided with a refined product discharge pipeline 52, and the bottom is provided with an HCl feed pipeline 53;
the top of the synthesis tower 4 is provided with a gaseous chlorosulfonic acid discharge pipeline 42, the upper part is provided with a liquid chlorosulfonic acid HCl feeding pipeline 43, and the lower part is provided with a raw material HCl feeding pipeline 41 and a liquid chlorosulfonic acid discharge pipeline 44;
wherein, the HCl discharging pipeline 51 at the top of the refining tower 5 is communicated with the raw material HCl feeding pipeline 53 of the synthesis tower 4, the other end of the gaseous chlorosulfonic acid discharging pipeline 42 of the synthesis tower 4 is communicated with the cooler 11, the cooler 11 is communicated with the first ground tank 6 through a pipeline, the first ground tank 6 is respectively communicated with the synthesis tower 4 through the liquid chlorosulfonic acid feeding pipeline and the liquid chlorosulfonic acid discharging pipeline 44 of the synthesis tower 4, and the liquid chlorosulfonic acid feeding pipeline 43 of the synthesis tower 4 is provided with a first circulating pump 61;
the first ground tank 6 is communicated with the refining tower 5 through a finished chlorosulfonic acid HCl feeding pipeline 53, a finished product circulating pump 62 is arranged on the finished chlorosulfonic acid HCl feeding pipeline 53, and the refining tower 5 is communicated with the second ground tank 7 through a refined product discharging pipeline 52.
The HCl feeding pipeline 53 of the refining tower 5 is provided with a first demister 8 for impurity removal.
The raw material SO3The production unit is communicated with the synthesis tower 4 through a raw material HCl feeding pipeline 41, and a branch of the raw material HCl feeding pipeline 41 is provided with a device for SO3And a second demister 9 for removing impurities.
The synthesis tower 4 is provided therein with a first spray device 45 and a second spray device 46.
The liquid chlorosulfonic acid HCl feeding pipeline 43 of the synthesis tower 4 is respectively communicated with a first spraying device 45 and a second spraying device 46.
The SO3The production unit is connected to the raw material HCl feeding pipe 41 of the synthesis tower 4.
The raw material HCl feed line 41 of the synthesis column 4 is provided with a flow meter 10 for controlling the feed amount of the raw materials HCl and SO 3.
Raw material SO3: from raw material SO3SO produced by a production unit3Enters the pipeline and is subjected to impurity removal by a second demister 9 to obtain purer gas SO3The SO enters the synthesis tower 4 through a branch pipe of a raw material HCl feeding pipeline 41 after being discharged from the second demister 9, and before entering the synthesis tower 43The temperature of (3) is 100 + -0.5 deg.C and the pressure is 32 kpa.
Raw material HCl: the HCl gas from the HCl generation unit enters the HCl scrubber tower 31 where it meets concentrated sulfuric acid from the scrubber tower 32 to remove moisture. And the dried HCl gas enters the first demister 8 for demisting, the purity of the HCl gas is higher than 99%, and the HCl gas is discharged from the first demister 8 and enters the refining tower 5 through an HCl feeding pipeline 53 of the refining tower 5. The liquid chlorosulfonic acid is subjected to heat exchange with HCl gas in the refining tower 5, so that the temperature of the HCl gas is increased; on the other hand, HCl reacts with chlorosulfonic acid by-products to produce chlorosulfonic acid and SO3To achieve the purpose of refining. HCl gas carries a small amount of SO3Enters a raw material HCl feeding pipeline 41 from a refining tower 5 and an HCl discharge pipeline 51, then enters a synthesis tower 4, and has the temperature of 80 +/-0.5 ℃ and the pressure of 22kpa before entering the synthesis tower 4.
Chlorosulfonic acid synthesis and refining: SO (SO)3And HCl enter the synthesis tower 4 through a flow meter 10 according to the volume ratio of 1.05: 1, and chlorosulfonic acid is formed through the synthesis reaction of a packed bed in the synthesis tower 4. Gaseous chlorosulfonic acid is discharged from a gaseous chlorosulfonic acid discharge pipe 42 at the top, enters a cooler 11 of the synthesis tower 4, is cooled to become liquid, and enters a first ground tank 6. In addition, liquid chlorosulfonic acid in the synthesis tower 4 enters the first sump 6 from a liquid chlorosulfonic acid discharge pipe 44 at the bottom of the synthesis tower 4. The liquid chlorosulfonic acid HCl feed line 43 of the synthesis tower 4 is fed by a first circulation pump 61 arranged on the first sump 6 to liquid chlorosulfonic acid HCl and then to the synthesis tower 4 to the spray equipment. The first spray device 45 absorbs gaseous chlorosulfonic acid produced by the reaction, and the second spray device 46 absorbs small droplets of chlorosulfonic acid. After spray adsorption, the mixture enters the first ground tank 6 again through a liquid chlorosulfonic acid discharge pipe 44. The finished product circulation pump 62 arranged on the first ground tank 6 conveys the finished product chlorosulfonic acid out of the first ground tank 6, enters the refining tower 5 through the finished product chlorosulfonic acid HCl feeding pipeline 53 of the refining tower 5, meets the dried and demisted raw material HCl, and enables byproducts in the finished product chlorosulfonic acid to react with the HCl to generate chlorosulfonic acid and SO3Achieving the purpose of refinement. The refined finished product in the refining tower 5 enters the second ground tank 7 through the refined product discharge pipeline 52 and is conveyed into the finished product tank through a pump and a refined chlorosulfonic acid conveying opening 71 arranged on the second ground tank 7.
The first spraying device and the second spraying device are arranged inside the tower from top to bottom and are respectively a first spraying device and a second spraying device, so that the spraying of liquid chlorosulfonic acid can be realized, and a plurality of atomizing nozzles, pressure control parts and the like can be arranged to form the spraying devices.
Tail gas treatment: the incompletely reacted SO is also introduced into the gaseous chlorosulfonic acid discharge pipe 42 together with the gaseous chlorosulfonic acid in the synthesis tower 43HCl and SO2. After passing through a cooler 11 of the synthesis tower 4, a separator 12 and a demister 13, and enters the tailThe acid washing tower 32 of the gas treatment unit 3 enters the water washing tower 33 from the acid washing tower 32, and the tail gas treatment tower 34 of the sulfuric acid device is discharged from the water washing tower 33 to carry out ammonia absorption for removing SO2. The tail gas treatment tower 34 of the sulfuric acid device in the system is shared with the tail gas treatment device for sulfuric acid production.
Finally, although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the present invention can be modified or replaced by other means without departing from the spirit and scope of the present invention, which should be construed as limited only by the appended claims.
Claims (6)
1. A chlorosulfonic acid production system, which comprises a raw material HCl production unit (2) and a raw material SO3A production unit (1), a tail gas treatment unit (3), a raw material HCl production unit (2) and a raw material SO3The synthesis unit that production unit (1), tail gas processing unit (3) all link to each other, its characterized in that: the synthesis unit comprises a synthesis tower (4), a first ground tank (6) for collecting finished products prepared by the synthesis tower (4), a refining tower (5) and a second ground tank (7) for collecting refined products;
the top of the refining tower (5) is provided with an HCl discharge pipeline (51), the upper part of the refining tower is provided with a finished chlorosulfonic acid feed pipeline (54), the lower part of the refining tower is provided with a refined product discharge pipeline (52), and the bottom of the refining tower is provided with an HCl feed pipeline (53);
the top of the synthesis tower (4) is provided with a gaseous chlorosulfonic acid discharge pipeline (42), the upper part is provided with a liquid chlorosulfonic acid feed pipeline (43), and the lower part is provided with a raw material feed pipeline (41) and a liquid chlorosulfonic acid discharge pipeline (44);
wherein an HCl discharge pipeline (51) at the top of the refining tower (5) is communicated with a raw material feeding pipeline (41) of the synthesis tower (4), the other end of a gaseous chlorosulfonic acid discharge pipeline (42) of the synthesis tower (4) is communicated with a cooler (11), the cooler (11) is communicated with a first ground tank (6) through a pipeline, the first ground tank (6) is communicated with the synthesis tower (4) through a liquid chlorosulfonic acid feeding pipeline (43) and a liquid chlorosulfonic acid discharge pipeline (44) of the synthesis tower (4) respectively, and a first circulating pump (61) is arranged on the liquid chlorosulfonic acid feeding pipeline (43) of the synthesis tower (4);
the first ground groove (6) is communicated with the refining tower (5) through a finished product chlorosulfonic acid feeding pipeline (54), a finished product circulating pump (62) is arranged on the finished product chlorosulfonic acid feeding pipeline (54), and the refining tower (5) is communicated with the second ground groove (7) through a refined product discharging pipeline (52).
2. The chlorosulfonic acid production system of claim 1, further comprising: and a first demister (8) for impurity removal is arranged on an HCl feeding pipeline (53) of the refining tower (5).
3. The chlorosulfonic acid production system of claim 1, further comprising: the raw material SO3The production unit is communicated with the synthesis tower (4) through a raw material feeding pipeline (41), and a branch of the raw material feeding pipeline (41) is provided with a device for SO3A second demister (9) for removing impurities.
4. The chlorosulfonic acid production system of claim 1, further comprising: a first spraying device (45) and a second spraying device (46) are arranged in the synthesis tower (4).
5. The chlorosulfonic acid production system of claim 4, wherein: and a liquid chlorosulfonic acid feeding pipeline (43) of the synthesis tower (4) is respectively communicated with a first spraying device (45) and a second spraying device (46).
6. A chlorosulfonic acid production system according to any one of claims 1 to 5, wherein: the raw material feeding pipeline (41) of the synthesis tower (4) is provided with HCl and SO for controlling raw materials3A flow meter (10) for the amount of feed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920447760.5U CN210065171U (en) | 2019-04-03 | 2019-04-03 | Chlorosulfonic acid production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920447760.5U CN210065171U (en) | 2019-04-03 | 2019-04-03 | Chlorosulfonic acid production system |
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| CN210065171U true CN210065171U (en) | 2020-02-14 |
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| CN201920447760.5U Active CN210065171U (en) | 2019-04-03 | 2019-04-03 | Chlorosulfonic acid production system |
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