CN211098326U - HC L gas drying system in chlorosulfonic acid production process - Google Patents

HC L gas drying system in chlorosulfonic acid production process Download PDF

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Publication number
CN211098326U
CN211098326U CN201921340633.1U CN201921340633U CN211098326U CN 211098326 U CN211098326 U CN 211098326U CN 201921340633 U CN201921340633 U CN 201921340633U CN 211098326 U CN211098326 U CN 211098326U
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drying
gas
pipe
tank
sulfuric acid
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刘华
徐化林
杨世立
田文成
张力
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Huaqiang Chemical Group Co Ltd
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Huaqiang Chemical Group Co Ltd
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Abstract

The utility model discloses a HC L gas drying system in chlorosulfonic acid production process, including gas drying unit and concentrated sulfuric acid drying unit, gas drying unit is gaseous through leading-in concentrated sulfuric acid drying HC L, concentrated sulfuric acid drying unit is used for retrieval and utilization to gas drying unit after the concentrated sulfuric acid drying process after with dry gas, the utility model discloses utilize the strong water absorption of concentrated sulfuric acid, set up the drying system who corresponds and be convenient for the concentrated sulfuric acid to the gaseous drying of HC L to the concentration of concentrated sulfuric acid in the gas drying pond can be guaranteed in the cooperation use through the batching pipe, avoid concentrated sulfuric acid concentration to reduce the corrosion pipeline.

Description

HC L gas drying system in chlorosulfonic acid production process
Technical Field
The utility model belongs to the technical field of gas drying, concretely relates to HC L gas drying system in chlorosulfonic acid production process.
Background
Chlorosulfonic acid is used primarily for the sulfonation of organic compounds. Chlorosulfonic acid is used as sulfonating agent or chlorosulfonating agent, mainly used for saccharin preparation, sulfa drug production, dye and dye intermediate synthesis and sulfonation of synthetic detergent raw material alkylbenzene; in addition, it is also used for the production of pesticides and smoke screens. However, chlorosulfonic acid produced by the traditional process has poor product quality and low purity due to impure raw materials and organic matters, and the application of chlorosulfonic acid in organic chemical industry is severely restricted.
The main production process of chlorosulfonic acid comprises the following 3 types:
① A traditional production method
Synthesis of chlorosulfonic acid in gas phase with SO3 and HCl: raw materials Cl2 and H2 are combusted in an HCl synthesis furnace to synthesize HCl gas, the HCl gas is cooled and dehydrated, then is mixed with SO3 gas and enters a chlorosulfonic acid synthesis tower, and the synthesized gas-phase chlorosulfonic acid is cooled into liquid and then flows into a finished product tank after further reaction with HCl through an auxiliary absorption tower. The waste gas is subjected to acid absorption SO3 and SO2 and water washing to absorb HCl, and then is further absorbed by alkali and then is discharged into the atmosphere.
② production process using oleum as raw material
105% sulfuric acid contains 20% free SO3, SO3 is extracted from fuming sulfuric acid, and only the partial pressure of SO3 needs to be reduced or the temperature of the fuming sulfuric acid needs to be properly increased, SO that the fuming sulfuric acid can be used as a raw material to produce chlorosulfonic acid. The 105% fuming sulfuric acid is extracted by a SO3 fan under reduced pressure, and the 98% sulfuric acid after the SO3 is extracted can be sent back to a sulfuric acid plant for absorbing SO3, SO that the 105% fuming sulfuric acid is reused. Therefore, after the fuming sulfuric acid is used, the cost is not increased greatly, and the equipment is not increased greatly. The production of chlorosulfonic acid by using fuming sulfuric acid can greatly increase the production capacity under the same equipment condition, and correspondingly, the 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. Therefore, for a factory with a fuming sulfuric acid production device, the fuming sulfuric acid is adopted as a raw material to produce chlorosulfonic acid, and the method is worthy of popularization and application.
③ production process using pure hydrogen chloride gas as raw material
HC L gas from the desorption tower contains saturated water vapor, and is generally condensed by circulating water to remove most of water in the gas, and then is cooled by frozen brine to remove the rest of water.
In the production process of the chlorosulfonic acid, the third method is mature and reliable in technology and is an existing general chlorosulfonic acid production process, but HC L gas produced by the method needs to be dried before reaction, because the chlorosulfonic acid reacts violently when meeting water, the product purity is reduced, and the generated dilute acid is easy to corrode equipment pipelines, so that leakage which is not easy to dispose is caused.
On the basis, the cryogenic process is mostly adopted for drying HC L gas in the prior art, but a refrigerating unit for preparing frozen brine has higher motor power, so that the energy consumption for producing chlorosulfonic acid is higher.
In the prior art, in order to solve the problem of high energy consumption in the HC L gas drying operation, an operation method for drying HC L gas by using concentrated sulfuric acid is provided, water molecules in HC L gas are captured by using strong water absorption of the concentrated sulfuric acid to dry HC L gas, but as the concentration of the concentrated sulfuric acid is reduced after water absorption, a sulfuric acid solution with reduced concentration is very easy to corrode pipelines and equipment (the concentrated sulfuric acid can passivate metal so as not to corrode metal equipment), so that an HC L gas drying system capable of effectively ensuring the concentration of the concentrated sulfuric acid in the effluent water is provided.
SUMMERY OF THE UTILITY MODEL
To the not enough that exists among the prior art, the utility model provides a HC L gas drying system in chlorosulfonic acid production process has solved among the prior art and has adopted concentrated sulfuric acid to reduce the problem of corroding pipeline and equipment easily to HC L gaseous drying time its concentration.
In order to achieve the purpose, the HC L gas drying system in the chlorosulfonic acid production process adopts the following technical scheme that the HC L gas drying system comprises a gas drying unit and a concentrated sulfuric acid drying unit, wherein the gas drying unit is used for drying HC L gas by leading-in concentrated sulfuric acid, and the concentrated sulfuric acid drying unit is used for recycling the concentrated sulfuric acid after the drying gas to the gas drying unit after being dried;
the device comprises a gas drying unit, a transition pool, a feeding pipe, a feeding pump, a circulating pipe, a mixing pipe, a concentrated sulfuric acid introducing pipe, a concentrated sulfuric acid drying unit and a concentrated sulfuric acid drying unit, wherein the gas drying unit comprises a gas drying pool and the transition pool, the bottom of the gas drying pool is connected with the gas inlet fan and is provided with an HC L gas inlet pipe, the top of the gas drying pool is connected with the bottom of the transition pool through an HC L transition pipe, the top of the transition pool is connected with an HC L gas outlet pipe;
wherein the discharge end of the HC L air inlet pipe and the discharge end of the HC L transition pipe are both provided with aeration devices.
The utility model discloses an application principle is that the concentrated sulfuric acid (called as No. 1 concentrated sulfuric acid) that gets into the transition pond from the batching pipe gets into the gas drying pond through the inlet pipe, when the concentrated sulfuric acid that gets into the gas drying pond all reaches the take the altitude with the concentrated sulfuric acid in the transition pond, the control circulating pipe switches on and makes the gas drying pond form the return circuit unit with the transition pond, at this moment, wet HC L gas is dried through the concentrated sulfuric acid of HC L intake pipe leading-in gas drying pond in, HC L gas after drying gets into the transition pond through HC L transition pipe and carries out the external row after carrying out the secondary drying;
concentrated sulfuric acid (called as No. 2 concentrated sulfuric acid) dried by HC L gas in the gas drying tank enters the transition tank through a circulating pipeline and is mixed with No. 1 concentrated sulfuric acid (concentrated sulfuric acid led out by a batching pipe) led in the transition tank, the concentration of the concentrated sulfuric acid is improved, and the concentrated sulfuric acid which is lower than the No. 1 concentrated sulfuric acid and higher than the No. 2 concentrated sulfuric acid is obtained and enters the gas drying tank to be dried by HC L gas, so that the concentrated sulfuric acid concentration in the gas drying tank is not too low;
with the continuous capture of the concentrated sulfuric acid to the water molecules in the HC L gas, the liquid in the transition tank gradually increases and finally enters the concentrated sulfuric acid drying unit through the overflow pipe for drying treatment, and the treated concentrated sulfuric acid enters the material mixing pipe and enters the gas drying unit for recycling.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model discloses utilize the strong water absorption of concentrated sulfuric acid, set up the drying system who corresponds and be convenient for concentrated sulfuric acid to the gaseous drying work of HC L to use the concentration that can guarantee concentrated sulfuric acid in the gas drying pond through the cooperation of batching pipe, avoid concentrated sulfuric acid concentration to reduce the corrosion pipeline.
2. The utility model discloses all be equipped with aeration equipment at HC L intake pipe discharge end and HC L transition pipe discharge end, aeration equipment that HC L intake pipe discharge end set up can effectively go HC L to listen to the dispersion to concentrated sulfuric acid solution in, and cooperate the feeding you with the use of circulating pipe, make the flow direction of HC L gas and concentrated sulfuric acid be the form against the current, strengthen the gas-liquid contact and improve gaseous drying effect, aeration equipment that HC L transition pipe discharge end set up can also effectively mix the liquid in the transition pond except can effectively dispersing gas in the liquid (aeration equipment originally has the effect of mixing liquid), make things convenient for concentrated sulfuric acid after the batching pipe is leading-in to melt into in the original liquid in the transition pond fast.
3. The utility model is used for dry HC L's concentrated sulfuric acid can recycle, still avoids the production of spent acid when practicing thrift manufacturing cost, causes the environment burden.
Drawings
FIG. 1 is a schematic flow chart of the present invention;
fig. 2 is a schematic structural view of the aeration device of the utility model.
In the figure, a main pipeline 1, an auxiliary pipeline 11 and an air guide hole 111.
Detailed Description
As shown in fig. 1 and 2, the utility model relates to a HC L gas drying system in chlorosulfonic acid production process, which comprises a gas drying unit and a concentrated sulfuric acid drying unit, wherein the gas drying unit is used for drying HC L gas by leading-in concentrated sulfuric acid, and the concentrated sulfuric acid drying unit is used for recycling the concentrated sulfuric acid after drying the gas to the gas drying unit after drying treatment;
the system comprises a gas drying unit, a transition tank, a gas drying tank, a heat supply drying unit, a waste gas drying and drying unit and a waste gas drying and drying unit, wherein the gas drying tank is connected with the bottom of the gas drying tank through an air inlet fan and provided with an HC L air inlet pipe, the top of the gas drying tank is connected with the bottom of the transition tank through an HC L transition pipe, the top of the transition tank is connected with an HC L air outlet pipe, the position, close to the top of the gas drying tank, of the gas drying tank is connected with the transition tank through a feed pipe with a feed pump, the position, close to the bottom of the gas drying tank, of the gas drying tank is connected with the transition tank through a circulating pipe with a circulating pump, the transition tank is connected with a concentrated sulfuric acid feed pipe, the end of the transition tank is connected with a concentrated sulfuric acid feed pipe, the solid drying tank is connected with a spiral feeder for feeding and drying solid dried concentrated sulfuric acid, the solid drying tank is connected with the waste gas drying and drying unit, the waste gas drying unit is connected with a waste gas drying and drying unit, the waste gas drying unit is connected with a waste gas drying and drying unit.
The utility model discloses an application principle is that the concentrated sulfuric acid (called as No. 1 concentrated sulfuric acid) that gets into the transition pond from the batching pipe gets into the gas drying pond through the inlet pipe, when the concentrated sulfuric acid that gets into the gas drying pond all reaches the take the altitude with the concentrated sulfuric acid in the transition pond, the control circulating pipe switches on and makes the gas drying pond form the return circuit unit with the transition pond, at this moment, wet HC L gas is dried through the concentrated sulfuric acid of HC L intake pipe leading-in gas drying pond in, HC L gas after drying gets into the transition pond through HC L transition pipe and carries out the external row after carrying out the secondary drying;
concentrated sulfuric acid (called as No. 2 concentrated sulfuric acid) dried by HC L gas in the gas drying tank enters the transition tank through a circulating pipeline and is mixed with No. 1 concentrated sulfuric acid (concentrated sulfuric acid led out by a batching pipe) led in the transition tank, the concentration of the concentrated sulfuric acid is improved, and the concentrated sulfuric acid which is lower than the No. 1 concentrated sulfuric acid and higher than the No. 2 concentrated sulfuric acid is obtained and enters the gas drying tank to be dried by HC L gas, so that the concentrated sulfuric acid concentration in the gas drying tank is not too low;
with the continuous capture of the concentrated sulfuric acid to the water molecules in the HC L gas, the liquid in the transition tank gradually increases and finally enters the liquid drying tank through the overflow pipe, and as the anhydrous magnesium sulfate has water absorption property (one magnesium sulfate molecule can absorb seven water molecules to form MgSO4 & 7H2O), and does not react with the concentrated sulfuric acid, the magnesium sulfate after absorption is not dissolved in the concentrated sulfuric acid, so that the solid-liquid separation is convenient, the concentrated sulfuric acid entering the liquid drying tank is introduced into the transition tank through the spiral feeder to improve the concentration of the concentrated sulfuric acid (form No. 1 concentrated sulfuric acid) after water absorption treatment of the anhydrous magnesium sulfate, and then is introduced into the transition tank through the material distribution pipe;
the magnesium sulfate after water absorption is led out from the liquid drying tank to enter the solid drying tank, water molecules in the hydrated magnesium sulfate are removed through hot air drying treatment (decomposition reaction of the magnesium sulfate does not exist, the decomposition reaction of the magnesium sulfate needs to be burnt under the condition of more than 900 ℃), the anhydrous magnesium sulfate is obtained and recycled to the spiral feeder, and finally the anhydrous magnesium sulfate enters the liquid drying tank to be dried and concentrated sulfuric acid so as to improve the concentration of the concentrated sulfuric acid for recycling, the air led out from the solid drying tank can contain acid mist particles besides the increase of the water content, so that the gas led out from the solid drying tank needs to be discharged after being washed by the waste gas washing tank, and the waste gas washing tank can utilize acid-base neutralization and acid mist particles contained in reaction and washing gas.
It is worth noting that: in the initial stage of system operation, the flow rate of the metering pump in unit hour can be controlled to be relatively large, and when the concentrated sulfuric acid in the gas drying tank and the concentrated sulfuric acid in the transition tank reach a certain height, the conveying flow rate in unit time is adjusted.
The utility model discloses all be equipped with aeration equipment at HC L intake pipe discharge end and HC L transition pipe discharge end, aeration equipment that HC L intake pipe discharge end set up can effectively go HC L to listen to the dispersion to concentrated sulfuric acid solution in, and cooperate the feeding you with the use of circulating pipe, make the flow direction of HC L gas and concentrated sulfuric acid be the form against the current, strengthen the gas-liquid contact and improve gaseous drying effect, aeration equipment that HC L transition pipe discharge end set up can also effectively mix the liquid in the transition pond except can effectively dispersing gas in the liquid (aeration equipment originally has the effect of mixing liquid), make things convenient for concentrated sulfuric acid after the batching pipe is leading-in to melt into in the original liquid in the transition pond fast.
The utility model is used for dry HC L's concentrated sulfuric acid can recycle, still avoids the production of spent acid when practicing thrift manufacturing cost, causes the environment burden.
For the mixed effect of the concentrated sulfuric acid of liquid in the improvement transition pond and newly-added, the utility model discloses the circulating pipe discharge end that sets up all is close to transition bottom of the pool portion setting with batching pipe feed end relatively, the inlet pipe feed end is close to transition top of the pool portion installation, the overflow pipe feed end is close to transition top of the pool portion setting and is higher than the inlet pipe feed end installation. Set up circulation pipe discharging pipe and batching pipe feed end relatively and all be close to transition bottom of the pool portion and set up, cooperate the use of aeration equipment in the transition pond, can effectively with the leading-in liquid of two inlet ports fast with original liquid flash mixed in the transition pond, the inlet pipe of following at last is derived.
For the convenience also can have the effect of stirring for making things convenient for the effective dispersion of gas in liquid in the aeration process, as shown in fig. 2, the utility model discloses the aeration equipment that sets up includes trunk line 1 of being connected with HC L intake pipe discharge end or HC L transition pipe discharge end, trunk line 1 periphery is encircled and is equipped with a plurality of auxiliary conduit 11 rather than communicating the setting, all is equipped with a plurality of air guide holes 111 on every auxiliary conduit 11.
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 (5)

1. The HC L gas drying system in the chlorosulfonic acid production process is characterized by comprising a gas drying unit and a concentrated sulfuric acid drying unit, wherein the gas drying unit is used for drying HC L gas by introduced concentrated sulfuric acid, and the concentrated sulfuric acid drying unit is used for drying and recycling the concentrated sulfuric acid after the gas is dried to the gas drying unit;
the device comprises a gas drying unit, a transition tank, a feeding pipe, a circulating pipe, a mixing pipe and a concentrated sulfuric acid drying unit, wherein the gas drying unit comprises a gas drying tank and the transition tank, the bottom of the gas drying tank is connected with the HC L gas inlet pipe with a gas inlet fan, the top of the gas drying tank is connected with the bottom of the transition tank through an HC L transition pipe, and the top of the transition tank is connected with an HC L gas outlet pipe;
wherein the discharge end of the HC L air inlet pipe and the discharge end of the HC L transition pipe are both provided with aeration devices.
2. The HC L gas drying system of claim 1, wherein the concentrated sulfuric acid drying unit comprises a solid drying tank disposed at a discharge end of an overflow pipe, the solid drying tank is connected to a screw feeder for feeding solid dry matter of dried concentrated sulfuric acid, the solid drying tank is connected to a liquid storage tank, and the liquid storage tank is communicated with a batching pipe.
3. The HC L gas drying system in the chlorosulfonic acid production process according to claim 2, further comprising a solid drying unit, wherein the solid drying unit comprises a solid drying tank connected with a liquid drying tank through a solid discharge pipe, the solid drying tank is communicated with a discharge passage, the solid drying tank is communicated with a heat supply unit, the heat supply unit comprises an air compressor and a heater which are sequentially connected, the heater is connected with the solid drying tank, the solid drying tank is connected with a waste gas washing tank through a pipeline, and the waste gas washing tank is provided with an emptying pipe.
4. The HC L gas drying system for chlorosulfonic acid production according to claim 3, wherein the discharge end of the circulation pipe and the feed end of the ingredient pipe are disposed opposite to each other and are both disposed near the bottom of the transition tank, the feed end of the feed pipe is disposed near the top of the transition tank, and the feed end of the overflow pipe is disposed near the top of the transition tank and is disposed higher than the feed end of the feed pipe.
5. The HC L gas drying system for chlorosulfonic acid production according to claim 4, wherein the aerator comprises a main pipe connected to the discharge end of HC L gas inlet pipe or HC L transition pipe, and a plurality of auxiliary pipes are disposed around the main pipe and communicated with the main pipe, and each auxiliary pipe is provided with a plurality of gas holes.
CN201921340633.1U 2019-08-16 2019-08-16 HC L gas drying system in chlorosulfonic acid production process Active CN211098326U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201921340633.1U CN211098326U (en) 2019-08-16 2019-08-16 HC L gas drying system in chlorosulfonic acid production process

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Application Number Priority Date Filing Date Title
CN201921340633.1U CN211098326U (en) 2019-08-16 2019-08-16 HC L gas drying system in chlorosulfonic acid production process

Publications (1)

Publication Number Publication Date
CN211098326U true CN211098326U (en) 2020-07-28

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