CN212832849U - Recovery processing system of chlor-alkali industry dilute sulfuric acid - Google Patents
Recovery processing system of chlor-alkali industry dilute sulfuric acid Download PDFInfo
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- CN212832849U CN212832849U CN202020924458.7U CN202020924458U CN212832849U CN 212832849 U CN212832849 U CN 212832849U CN 202020924458 U CN202020924458 U CN 202020924458U CN 212832849 U CN212832849 U CN 212832849U
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Abstract
The utility model provides a recovery processing system of dilute sulfuric acid of chlor-alkali industry, include: the first dilute sulphuric acid standing tank is communicated with a chlorine drying device; a dechlorination tower communicated with the first dilute sulphuric acid standing tank; the condenser is communicated with the gas-phase outlet of the dechlorination tower; the conveying pipeline is communicated with the outlet of the condenser; the liquid seal tank is communicated with the conveying pipeline and is positioned below the condenser; and the first vacuum pump is communicated with the liquid seal tank. Compared with the prior art, the utility model discloses the jar that stews through dilute sulphuric acid earlier reduces the content of wherein organic matter and inorganic salt, reduces its adhering to the condenser, has improved the cooling effect, then makes the mixed condensate flow to the liquid seal jar through liquid gravity potential difference, also the greatly reduced influence to follow-up technology jam when further eliminating to the pipeline jam.
Description
Technical Field
The utility model belongs to the technical field of the chlor-alkali industry, especially, relate to a recovery processing system of dilute sulfuric acid of chlor-alkali industry.
Background
At present, the chlorine drying of a chlor-alkali device mainly utilizes 98% non-fuming sulfuric acid for drying, 75% -78% of dilute sulfuric acid after chlorine drying is used as chemical hazardous compounds for treatment, the part of dilute sulfuric acid contains certain free chlorine and a small amount of impurities, part of free chlorine is desorbed in the storage and transportation process, the surrounding environment is influenced, and how to recycle the part of dilute sulfuric acid is always a big problem troubling chlor-alkali enterprises.
Because the content of sulfuric acid in dilute sulfuric acid is still very high, in order to recycle waste, the water, organic matters, trace chlorine and the like in the dilute sulfuric acid can be evaporated and concentrated to 96 percent sulfuric acid for recycling, see figure 1, and figure 1 is a structural schematic diagram of the existing dilute sulfuric acid concentration and utilization system, wherein C-3000 is a dechlorination tower, TI-3000 is the on-site display temperature in the C-3000 tower of the dechlorination tower, PIC3000 is the remote transmission belt regulation of gas pressure in a pipeline, E3002 is a condenser, TE3003 is the circulating water temperature, J-3001 is a vacuum pump for pumping liquid, J-3000 is a vacuum pump for pumping gas, D-3000 is an acid water circulating tank, LT-3000 is the remote transmission liquid level of the acid water circulating tank, P-3000 is a pump, PT-3000 is the outlet pressure of the P-3000, E-3000 is a heat exchanger, LT-3002 is the remote transmission liquid level of, TE-3000 is the remote temperature of the acid water out of the heat exchanger.
However, because the original salt contains 10-15 PPm of organic matters, the organic matters partially react with chlorine gas at the anode of the electrolytic cell, and the chlorine gas enters a chlorine treatment system to react again under the catalytic action of concentrated sulfuric acid to generate mixed organic matters such as chlorobenzene, bromobenzene and the like. Therefore, when dilute sulfuric acid is concentrated and sulfuric acid is recovered, organic matter carries inorganic salt mixture and enters the gas phase cooler along with hot steam, carried fog-like organic matter and inorganic salt mixture gas directly act on the heat exchange tube of the condenser, the heat exchange tube runs for a period of time to form a 2-millimeter covering layer, the service cycle of the condenser is greatly shortened, and meanwhile, the liquid phase pipeline of the cooler is blocked.
SUMMERY OF THE UTILITY MODEL
In view of this, the technical problem to be solved by the present invention is to provide a system for recovering and treating dilute sulfuric acid in chlor-alkali industry, which can eliminate organic matters and blockages.
The utility model provides a recovery processing system of dilute sulfuric acid of chlor-alkali industry, include:
the first dilute sulphuric acid standing tank is communicated with a chlorine drying device;
a dechlorination tower communicated with the first dilute sulphuric acid standing tank;
the condenser is communicated with the gas-phase outlet of the dechlorination tower;
the conveying pipeline is communicated with the outlet of the condenser;
the liquid seal tank is communicated with the conveying pipeline and is positioned below the condenser;
and the first vacuum pump is communicated with the liquid seal tank.
Preferably, the system also comprises an acid water circulating tank; and the acidic water circulation tank is communicated with the conveying pipeline and the liquid seal tank through a first vacuum pump.
Preferably, the device also comprises a heat exchanger; the inlet of the heat exchanger is communicated with the outlet of the acidic water circulating tank; and the outlet of the heat exchanger is communicated with the inlet of the acidic water circulating tank.
Preferably, the device also comprises a second dilute sulfuric acid standing tank; the inlet of the second dilute sulfuric acid standing tank is communicated with a chlorine gas drying device; the outlet of the second sulfuric acid standing tank is communicated with a dechlorination tower; the second dilute sulphuric acid standing tank is not communicated with the first sulphuric acid standing tank.
Preferably, the dilute sulfuric acid outlets of the first dilute sulfuric acid standing tank and the second dilute sulfuric acid standing tank are respectively and independently at least 500 mm higher than the bottom of the tank.
Preferably, the device also comprises a pH value adjusting tank; and the pH value adjusting tank is communicated with an outlet of the liquid seal tank.
Preferably, the conveying pipeline is a gravity-fed pipeline.
Preferably, the distance between the condenser and the liquid seal tank is more than 9.8 meters.
The utility model provides a recovery processing system of dilute sulfuric acid of chlor-alkali industry, include: the first dilute sulphuric acid standing tank is communicated with a chlorine drying device; a dechlorination tower communicated with the first dilute sulphuric acid standing tank; the condenser is communicated with the gas-phase outlet of the dechlorination tower; the conveying pipeline is communicated with the outlet of the condenser; the liquid seal tank is communicated with the conveying pipeline and is positioned below the condenser; and the first vacuum pump is communicated with the liquid seal tank. Compared with the prior art, the utility model discloses the jar that stews through dilute sulphuric acid earlier reduces the content of wherein organic matter and inorganic salt, reduces its adhering to the condenser, has improved the cooling effect, then makes the mixed condensate flow to the liquid seal jar through liquid gravity potential difference, also the greatly reduced influence to follow-up technology jam when further eliminating to the pipeline jam.
Drawings
FIG. 1 is a schematic structural diagram of a conventional dilute sulfuric acid concentration utilization system;
FIG. 2 is a schematic structural diagram of a dilute sulfuric acid recovery processing system in the chlor-alkali industry provided by the present invention;
fig. 3 is a schematic structural diagram of a dilute sulfuric acid standing tank of the recovery processing system of dilute sulfuric acid in the chlor-alkali industry provided by the utility model.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The utility model provides a recovery processing system of dilute sulfuric acid of chlor-alkali industry, include:
the first dilute sulphuric acid standing tank is communicated with a chlorine drying device;
a dechlorination tower communicated with the first dilute sulphuric acid standing tank;
the condenser is communicated with the gas-phase outlet of the dechlorination tower;
the conveying pipeline is communicated with the outlet of the condenser;
the liquid seal tank is communicated with the conveying pipeline and is positioned below the condenser E3002;
and the first vacuum pump is communicated with the liquid seal tank D-3001.
Referring to fig. 2 to fig. 3, fig. 2 is a schematic structural diagram of a recovery processing system for dilute sulfuric acid in the chlor-alkali industry provided by the present invention; FIG. 3 is a schematic structural view of a dilute sulfuric acid standing tank; in figure 2, D-4001 is a first dilute sulphuric acid standing tank, LE-4001 is a standing tank D-4001 remote transmission liquid level, D-4002 is a second dilute sulphuric acid standing tank, LE-4002 is a standing tank D-4002 remote transmission liquid level, P-3002 is a pump, C-3000 is a dechlorination tower, TI-3000 is the internal temperature of the dechlorination tower, PIC3000 is the gas remote transmission pressure in the pipeline, E3002 is a condenser, TE3003 is the circulating water temperature, D-3001 is a liquid seal tank, LT-3002 is the water seal tank D-3001 remote transmission liquid level, D-3000 is an acid water circulation tank, J-3000 is a first vacuum pump, LT-3000 is the acid water circulation tank remote transmission liquid level, P-3000 is a pump, PT-3000 is a pressure gauge, E-3000 is a heat exchanger, TE-3000 is the temperature after heat exchange, P-3002 is an external delivery pump, PT-3002 is a pressure gauge, PT-3003 is pressure gauge.
Sea salt required by chlor-alkali production generally contains less than 10PPm TOC and less than 15PPm at most, refined brine prepared from the sea salt is subjected to electrochemical reaction in an electrolytic cell, brine organic matters in an anode enter a chlorine drying device along with chlorine gas, and the reaction is carried out under the action of a drying agent concentrated sulfuric acid catalyst to obtain dry chlorine gas and dilute sulfuric acid containing the organic matters.
The utility model provides a recovery processing system of chlor-alkali industry dilute sulfuric acid includes the first dilute sulfuric acid jar that stews that is linked together with chlorine drying device. The chlorine alkali dilute sulfuric acid after chlorine drying can precipitate organic matters and inorganic salts in the chlorine alkali dilute sulfuric acid through standing, and the precipitate is discharged periodically, so that the content of the mixture of the organic matters and the inorganic salts in the system can be eliminated or reduced, and further, the adhesion to a cooler and the blockage to a liquid phase pipe are eliminated.
In order to improve the recovery treatment efficiency, the system preferably further comprises a second dilute sulfuric acid standing tank; the inlet of the second dilute sulfuric acid standing tank is communicated with the chlorine gas drying device, the second dilute sulfuric acid standing tank is not communicated with the first dilute sulfuric acid standing tank, namely the first dilute sulfuric acid standing tank and the second dilute sulfuric acid standing tank are in parallel relation, dilute sulfuric acid from the chlorine gas drying device can be alternately received, and each tank is preferably kept stand for 6 days to regularly remove precipitates so as to reduce organic matters and inorganic salt precipitates in the system.
In order to make room for the organic matters and inorganic salts which are precipitated, the dilute sulfuric acid outlets of the first dilute sulfuric acid standing tank and the second dilute sulfuric acid standing tank are respectively and independently at least 500 mm higher than the bottom of the tanks.
And dilute sulfuric acid outlets of the first dilute sulfuric acid standing tank and the second dilute sulfuric acid standing tank are respectively communicated with a dechlorinating tower. And (3) the standing dilute sulfuric acid enters a dechlorinating tower, is preheated by the countercurrent of steam and dilute sulfuric acid, and is evaporated by connecting the dilute sulfuric acid with an evaporator.
The gas phase outlet of the dechlorination tower is communicated with the condenser; the liquid phase outlet of the dechlorination tower is communicated with a sulfuric acid concentration device. The gas phase medium evaporated from dilute sulphuric acid by a dechlorinating tower enters a condenser for condensation; the condenser is preferably a tube still condenser; the vapor phase medium component distilled off by the dechlorination tower is preferably 126.9862 kg/h; 25kg/h of chlorine; 0.0138kg/h of a mixture of ferric sulfate and calcium sulfate which mainly comprises hexachlorobenzene, 1, 4-dibromo-2, 3,5, 6-tetrachlorobenzene and 1,3, 5-tribromo-2, 4, 6-trichlorobenzene and is partially mixed. The maximum total amount of gaseous medium evaporated from the dechlorination column was 153kg/h, the medium temperature was 85.8 ℃ and the pressure was-69.2 mbar. The flow velocity of the gas phase medium entering the heat exchange tube of the condenser is 5.6 m/s.
Because the gas phase entering the condenser is in a negative pressure state, the gas phase organic matter and organic salt mixture in the condenser can cover the condenser after being condensed to affect the cooling effect, meanwhile, the cooled liquid phase pipe contains inorganic salt and organic matter viscous liquid to block a liquid phase pipeline, the operation period of the device is seriously shortened, in order to avoid the blocking of the liquid phase pipeline in the condenser, the outlet of the condenser is communicated with a liquid seal tank through a conveying pipeline, and the liquid seal tank is positioned below the condenser; the distance between the condenser and the liquid seal tank is preferably more than 9.8 meters; the liquid seal tank is also communicated with a first vacuum pump, and preferably communicated with a suction port of the first vacuum pump, so that the liquid seal tank and the condenser keep the same negative pressure state, and the liquid condensed in the condenser automatically flows into the liquid seal tank by utilizing the gravity of the liquid, thereby eliminating the blockage of a pipeline and greatly reducing the influence on the blockage of a subsequent process; the conveying pipeline is preferably a gravity flow pipeline, so that the liquid can flow into the liquid seal tank without bending by utilizing the liquid gravity head; the liquid-sealed tank is preferably provided with an air inlet which can prevent the negative pressure and the interference to the gas phase pressure formed on the water-sealed tank when the material is delivered by the delivery pump P-3002.
According to the utility model, the device preferably also comprises an acid water circulation tank; the acidic water circulation tank is communicated with the conveying pipeline and the liquid seal tank through a first vacuum pump; the acid water circulation tank is communicated with an outlet of the first vacuum pump. The condenser contains organic matter, inorganic salt steam condensate water and a small amount of gas after being cooled, wherein the gas enters the circulating tank through the first vacuum pump, and most of the organic matter and the inorganic salt condensate water enter the liquid seal tank through the action of gravity (under the condition of equal negative pressure).
In the utility model, a heat exchanger is preferably further included; the inlet of the heat exchanger is communicated with the outlet of the acidic water circulating tank; the outlet of the heat exchanger is communicated with the inlet of the acidic water circulating tank; the heat energy contained in the gas can be further utilized by the heat exchanger.
According to the utility model, a second vacuum pump is preferably further included; the second vacuum pump is communicated with the liquid seal tank and the acidic water circulating tank and can send gas into the gas treatment system.
According to the utility model, a pH value adjusting tank is preferably also included; and the pH value adjusting tank is communicated with an outlet of the liquid seal tank. The pH value of the liquid is adjusted by the pH value adjusting tank, so that the water is recycled.
The utility model discloses the jar that stews earlier through dilute sulphuric acid reduces the content of wherein organic matter and inorganic salt, reduces its adhering to the condenser, has improved the cooling effect, then makes the mixed lime set flow to the liquid seal jar by oneself through liquid gravity potential difference, also the significantly reduced influence to follow-up technology jam when further eliminating to the pipeline jam.
In order to further illustrate the present invention, the following detailed description is made on a system for recovering and treating dilute sulfuric acid in chlor-alkali industry according to the present invention with reference to the following examples.
Example 1
See fig. 1 and 2.
The standing tanks D-4001 and D-4002 alternately receive dilute sulfuric acid from the chlorine drying device, and the standing tanks each receive dilute sulfuric acid for six days to periodically remove organic matters and inorganic salt precipitates in the precipitate reduction system.
Dilute sulfuric acid which is statically placed in the D-4001 tank and the D-4002 tank enters a dechlorinating tower in turn for treatment; the gas evaporated from the dechlorination tower enters a condenser E-3002 to cool down mixed condensate and enters a D-3001 tank. The D-3001 tank is connected with the suction inlet of the water flow vacuum pump J-3000, the same vacuum state is kept, and the mixed condensate cold from the condenser E-3002 automatically flows into the D-3001 tank. The liquid in the D-3001 tank is sent out by a pump P-3002, and the gas left after the condenser E-3002 is cooled enters the D-3000 tank by a water flow absorption pump J-3001 for recycling.
The modified E-3002 condenser is put into use in 2019 and 12 months, and is disassembled and inspected after continuous operation for 45 days, so that the attachments on the inner wall of the heat exchange tube are greatly reduced, and the modification effect is obvious. The influence of the attachments operating under the same working condition on the cooling effect of the E-3002 is eliminated. The absence of a blockage condition in the E-3002 to D-3001 conduits affects system operation.
Claims (8)
1. A recovery processing system of dilute sulfuric acid in chlor-alkali industry is characterized by comprising the following components:
the first dilute sulphuric acid standing tank is communicated with a chlorine drying device;
a dechlorination tower communicated with the first dilute sulphuric acid standing tank;
the condenser is communicated with the gas-phase outlet of the dechlorination tower;
the conveying pipeline is communicated with the outlet of the condenser;
the liquid seal tank is communicated with the conveying pipeline and is positioned below the condenser;
and the first vacuum pump is communicated with the liquid seal tank.
2. The recovery processing system of claim 1, further comprising an acid water recycle tank; and the acidic water circulation tank is communicated with the conveying pipeline and the liquid seal tank through a first vacuum pump.
3. The recovery processing system of claim 2, further comprising a heat exchanger; the inlet of the heat exchanger is communicated with the outlet of the acidic water circulating tank; and the outlet of the heat exchanger is communicated with the inlet of the acidic water circulating tank.
4. The recovery processing system of claim 1, further comprising a second dilute sulfuric acid rest tank; the inlet of the second dilute sulfuric acid standing tank is communicated with a chlorine gas drying device; the outlet of the second dilute sulfuric acid standing tank is communicated with a dechlorination tower; the second dilute sulphuric acid standing tank is not communicated with the first dilute sulphuric acid standing tank.
5. The recovery processing system of claim 4, wherein the dilute sulfuric acid outlets of the first and second dilute sulfuric acid rest tanks are each independently at least 500 mm above the tank bottom.
6. The recovery processing system of claim 1, further comprising a pH adjustment tank; and the pH value adjusting tank is communicated with an outlet of the liquid seal tank.
7. The recycling treatment system according to claim 1, wherein said transfer pipe is a gravity fed pipe.
8. The recovery processing system of claim 1, wherein the distance between the condenser and the liquid seal tank is greater than 9.8 meters.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020924458.7U CN212832849U (en) | 2020-05-27 | 2020-05-27 | Recovery processing system of chlor-alkali industry dilute sulfuric acid |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020924458.7U CN212832849U (en) | 2020-05-27 | 2020-05-27 | Recovery processing system of chlor-alkali industry dilute sulfuric acid |
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| CN212832849U true CN212832849U (en) | 2021-03-30 |
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| CN202020924458.7U Active CN212832849U (en) | 2020-05-27 | 2020-05-27 | Recovery processing system of chlor-alkali industry dilute sulfuric acid |
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