CN114053837A - Method for recovering hydrogen chloride gas in tail gas generated in incineration of chlorine-containing waste - Google Patents
Method for recovering hydrogen chloride gas in tail gas generated in incineration of chlorine-containing waste Download PDFInfo
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- CN114053837A CN114053837A CN202111429508.XA CN202111429508A CN114053837A CN 114053837 A CN114053837 A CN 114053837A CN 202111429508 A CN202111429508 A CN 202111429508A CN 114053837 A CN114053837 A CN 114053837A
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
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Abstract
The invention belongs to the technical field of chemical industry, and particularly relates to a method for recovering hydrogen chloride gas in incineration tail gas of chlorine-containing waste. The method of the invention comprises the following steps: s1: rapidly cooling the incineration flue gas, introducing the incineration flue gas into the lower part of the lower section circulating absorption section of the washing tower, and introducing clear water from the top of the washing tower; s2: liquid passes through an upper section absorption section, a middle section circulating absorption section and a lower section circulating absorption section of the water washing tower in sequence under the action of overflow; s3: hydrochloric acid is extracted from the bottom of the washing tower, and tail gas is discharged from the top of the washing tower; s4: the hydrochloric acid in the step S3 is introduced into a hydrochloric acid desorption tower; s5: dilute hydrochloric acid is extracted from the bottom of the hydrochloric acid desorption tower, and then the extracted dilute hydrochloric acid is introduced into the lower section circulating absorption section; s6: and hydrogen chloride gas is extracted from the top of the hydrochloric acid desorption tower. The invention provides a method for recovering hydrogen chloride gas in incineration tail gas of chlorine-containing waste by multi-stage absorption of hydrogen chloride in flue gas and full desorption of hydrogen chloride gas.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a method for recovering hydrogen chloride gas in incineration tail gas of chlorine-containing waste.
Background
The resource recovery technology of the chlorine-containing waste is mainly a heat treatment technology, including incineration, cracking, gasification and the like. Incineration can decompose chlorine-containing waste into inorganic carbon dioxide, water, hydrogen chloride, chlorine and a small amount of nitrogen oxides. At present, most of hydrogen chloride gas in incineration flue gas is absorbed by water, and then the hydrogen chloride gas which is not completely absorbed is removed by alkali washing. Since the amount of hydrogen chloride gas in the incineration off-gas is less than 4% (v), the conventional technique is hydrochloric acid obtained by absorbing hydrogen chloride in the flue gas with water. However, hydrochloric acid in chemical industry is excessive, and the produced hydrochloric acid is difficult to treat and has poor economical efficiency. Therefore, the recovery of hydrogen chloride gas in the incineration exhaust gas as a raw material is a core technology for resource recycling of chlorine-containing wastes.
The invention adopts a multi-section combined tower to absorb the hydrogen chloride in the incineration tail gas to obtain high-concentration hydrochloric acid, and then the hydrochloric acid is desorbed to generate HCl gas which can be used as a raw material, no hydrochloric acid is generated, and the invention has considerable economic and social benefits.
Disclosure of Invention
In order to solve the above problems in the prior art, the present invention aims to provide a method for recovering hydrogen chloride gas from incineration tail gas of chlorine-containing waste by multi-stage absorption of hydrogen chloride in flue gas and sufficient desorption of hydrogen chloride gas.
The technical scheme adopted by the invention is as follows:
a method for recovering hydrogen chloride gas in tail gas generated in the incineration of chlorine-containing wastes comprises the following steps:
s1: rapidly cooling the incineration flue gas, introducing the incineration flue gas into the lower part of the lower section circulating absorption section of the washing tower, and introducing clear water from the top of the washing tower;
s2: liquid passes through an upper section absorption section, a middle section circulating absorption section and a lower section circulating absorption section of the water washing tower in sequence under the action of overflow;
s3: hydrochloric acid is extracted from the bottom of the washing tower, and tail gas is discharged from the top of the washing tower;
s4: the hydrochloric acid in the step S3 is introduced into a hydrochloric acid desorption tower;
s5: dilute hydrochloric acid is extracted from the bottom of the hydrochloric acid desorption tower, and then the extracted dilute hydrochloric acid is introduced into the lower section circulating absorption section;
s6: and hydrogen chloride gas is extracted from the top of the hydrochloric acid desorption tower.
The invention divides the water washing tower into three sections, and circulates liquid in the middle section and the lower section, so that hydrochloric acid discharged from the hydrochloric acid pipeline fully absorbs hydrogen chloride in flue gas in the three sections, thereby improving the concentration of hydrochloric acid product and reducing the content of hydrogen chloride in tail gas.
The liquid in the middle section circulating absorption section of the invention circulates in the middle section circulating absorption section, the overflowing liquid enters the lower section circulating absorption section, the liquid in the lower section circulating absorption section circulates in the lower section circulating absorption section, and part of the liquid is discharged by the hydrochloric acid pipeline. Therefore, the liquid can be circulated for a long time in the middle-section circulating absorption section and the lower-section circulating absorption section, the liquid is ensured to absorb the hydrogen chloride in the flue gas as much as possible, the concentration of the finished hydrochloric acid is further improved, and the 31 percent finished hydrochloric acid is finally prepared.
And (3) introducing the high-concentration hydrochloric acid prepared by the water washing tower into a hydrochloric acid desorption tower for desorption to generate hydrogen chloride gas. The dilute hydrochloric acid after the hydrogen chloride gas is analyzed is introduced into the lower circulating absorption section for absorbing the hydrogen chloride in the tail gas, so that the whole system is free from hydrochloric acid generation, is completely balanced, and has considerable economic and social benefits.
In a preferred embodiment of the present invention, when the liquid passes through the lower cyclic absorption stage in step S2, the analyzed diluted hydrochloric acid and a part of the liquid that has passed through the lower cyclic absorption stage and absorbed hydrogen chloride are returned to the lower liquid distributor in the lower cyclic absorption stage. The liquid absorbing the hydrogen chloride by the lower circulating absorption section and the resolved dilute hydrochloric acid are conveyed to the lower liquid distributor by the lower hydrochloric acid conveying pump, so that the liquid absorbing the hydrogen chloride in the flue gas at the upper section and the middle section can absorb the hydrogen chloride in the flue gas at the lower section in a circulating manner, and clear water is not introduced into the lower section, thereby ensuring that the concentration of the hydrochloric acid is gradually increased from top to bottom and ensuring that the concentration of the hydrochloric acid discharged from a hydrochloric acid pipeline meets the requirement. And moreover, the diluted hydrochloric acid after desorption is introduced into the lower-section liquid return pipeline, so that no hydrochloric acid is generated in the system, and the system is completely balanced.
In a preferred embodiment of the present invention, in step S2, a part of the liquid absorbed hydrogen chloride by passing through the lower circulating absorption section is cooled before being returned to the lower liquid distributor. And (3) sending out a part of the hydrochloric acid generated from the bottom of the water washing tower as finished hydrochloric acid, and continuously and circularly absorbing hydrogen chloride in the flue gas by a part of the hydrochloric acid. The hydrogen chloride gas is dissolved into exothermic reaction, the heat released by the dissolution can be taken away by a first-level hydrochloric acid cooler, and the absorption temperature is controlled to be below 40 ℃.
In a preferred embodiment of the present invention, in step S2, the liquid flowing down from the lower liquid distributor passes through the lower packing. The lower section of the filler can reduce the speed of the flue gas and the liquid, and ensure that the liquid can fully absorb the hydrogen chloride in the lower section of the flue gas in the lower section of the filler.
As a preferable scheme of the present invention, in step S2, when the liquid passes through the middle-stage circulation absorption section, the liquid absorbing hydrogen chloride through the middle-stage circulation absorption section is sent back to the middle-stage liquid distributor in the middle-stage circulation absorption section; the liquid in the middle section circulating absorption section falls into the bottom of the middle section tower and overflows to the lower section circulating absorption section from the gas lift pipe. The liquid absorbing the hydrogen chloride by the middle section circulating absorption section is conveyed to the middle section liquid distributor by the middle section hydrochloric acid conveying pump, so that the liquid absorbing the hydrogen chloride in the upper section flue gas can absorb the hydrogen chloride in the middle section flue gas in a circulating manner, instead of introducing clean water into the middle section, the concentration of the hydrochloric acid is ensured to be increased gradually from top to bottom, and the concentration of the hydrochloric acid discharged from a hydrochloric acid pipeline is ensured to meet the requirement.
The flue gas rises from the riser, avoids the middle tower bottom to cause stopping to the flue gas. The liquid can be temporarily stored in the area enclosed by the middle tower bottom, the riser and the water washing tower, and the middle hydrochloric acid delivery pump can be ensured to pump the liquid in the middle tower bottom to the middle liquid distributor. The liquid is accumulated in the bottom of the middle tower to a certain degree and overflows from the riser, thereby ensuring that the liquid entering the lower section passes through the upper section and the middle section to fully absorb the hydrogen chloride in the flue gas. Three sections of absorption areas of the hydrogen chloride water washing tower share one tower body, and liquid in the tower overflows in a multi-stage gravity mode without a pump for conveying the liquid.
In a preferred embodiment of the present invention, in step S2, the liquid having absorbed hydrogen chloride via the middle-stage circulation absorption stage is cooled before being returned to the middle-stage liquid distributor. The hydrogen chloride gas is dissolved into exothermic reaction, the heat released by the dissolution can be taken away by a secondary hydrochloric acid cooler, and the absorption temperature is controlled to be below 20 ℃.
As a preferable aspect of the present invention, in step S2, the liquid flowing down from the middle stage liquid distributor passes through the middle stage packing. The middle section filler can reduce the speed of flue gas and liquid, guarantees that liquid can fully absorb the hydrogen chloride in the flue gas of middle section in the middle section filler.
In a preferred embodiment of the present invention, in step S2, the liquid above the gas-lifting tube is blocked by the liquid-blocking cap, and an overflow gap is left between the liquid-blocking cap and the gas-lifting tube. The liquid blocking cap can block liquid flowing down from the upper part, so that the liquid flowing down from the upper-section absorption section and the middle-section liquid distributor can only enter the bottom of the middle-section tower, and the liquid in the middle section can circularly absorb hydrogen chloride in the flue gas in the middle section.
In a preferred embodiment of the present invention, in step S2, clean water is introduced into the upper side of the sieve plate while the liquid passes through the upper stage absorption stage. Desalted clear water is continuously added into the tower plates, and hydrogen chloride in tail gas is contacted with fresh water to finish the final hydrogen chloride washing absorption, so that the hydrogen chloride content entering alkali washing is further reduced, and the consumption of liquid alkali is reduced. The make-up quantity of the clean water is the same as the water quantity taken away by the finished hydrochloric acid, and the system balance is kept.
In a preferred embodiment of the present invention, in step S6, the analyzed hydrogen chloride gas is condensed to separate water, and the obtained hydrogen chloride gas is returned to the apparatus and used.
As a preferable scheme of the present invention, in step S5, heat exchange is performed between hydrochloric acid before being introduced into the hydrochloric acid desorption tower and dilute hydrochloric acid extracted from the bottom of the hydrochloric acid desorption tower; part of dilute hydrochloric acid extracted from the bottom of the hydrochloric acid desorption tower is reboiled and then sent back to the bottom of the hydrochloric acid desorption tower. And the dilute hydrochloric acid is conveyed to a lower section circulating absorption pipeline through a dilute hydrochloric acid conveying pump and is used for absorbing hydrogen chloride in the tail gas. The hydrochloric acid in the hydrochloric acid pipeline and the dilute hydrochloric acid in the dilute hydrochloric acid conveying pipeline exchange heat fully in the hydrochloric acid preheater, so that the temperature of the hydrochloric acid in the hydrochloric acid pipeline is increased, and the hydrogen chloride gas can be analyzed conveniently; and the temperature of the dilute hydrochloric acid in the dilute hydrochloric acid conveying pipeline is reduced so as to ensure that the dilute hydrochloric acid can fully absorb the hydrogen chloride in the flue gas in the water washing tower.
The invention has the beneficial effects that:
1. the invention divides the water washing tower into three sections, and circulates liquid in the middle section and the lower section, so that hydrochloric acid discharged from the hydrochloric acid pipeline fully absorbs hydrogen chloride in flue gas in the three sections, thereby improving the concentration of hydrochloric acid product and reducing the content of hydrogen chloride in tail gas.
2. The liquid in the middle section circulating absorption section of the invention circulates in the middle section circulating absorption section, the overflowing liquid enters the lower section circulating absorption section, the liquid in the lower section circulating absorption section circulates in the lower section circulating absorption section, and part of the liquid is discharged by the hydrochloric acid pipeline. Therefore, the liquid can be circulated for a long time in the middle-section circulating absorption section and the lower-section circulating absorption section, the liquid is ensured to absorb the hydrogen chloride in the flue gas as much as possible, the concentration of the finished hydrochloric acid is further improved, and the 31 percent finished hydrochloric acid is finally prepared.
3. And (3) introducing the high-concentration hydrochloric acid prepared by the water washing tower into a hydrochloric acid desorption tower for desorption to generate hydrogen chloride gas. The dilute hydrochloric acid after the hydrogen chloride gas is analyzed is introduced into the lower circulating absorption section for absorbing the hydrogen chloride in the tail gas, so that the whole system is free from hydrochloric acid generation, is completely balanced, and has considerable economic and social benefits.
Drawings
FIG. 1 is a flow chart of a method of the present invention;
FIG. 2 is a schematic diagram of the architecture of a system used in the present invention;
in the figure, 1-water washing tower; 2-an upper absorption section; 3-middle section circulating absorption section; 4-lower section circulating absorption section; 5-water inlet pipe; 6-hydrochloric acid pipeline; 7-hydrochloric acid desorption tower; an 8-hydrogen chloride generation line; 9-dilute hydrochloric acid conveying pipeline; 11-an incineration flue gas inlet; 12-exhaust gas outlet; 21-sieve plate; 31-middle tower bottom; 32-riser; 33-a middle-section liquid return pipeline; 34-a middle section liquid distributor; 35-a middle hydrochloric acid delivery pump; 36-secondary hydrochloric acid cooler; 37-middle section packing; 38-liquid blocking cap; 41-lower section liquid return pipeline; 42-lower section liquid distributor; 43-lower hydrochloric acid transfer pump; 44-first stage hydrochloric acid cooler; 45-lower section packing; 81-hydrogen chloride cooler; 91-hydrochloric acid preheater; 92-dilute hydrochloric acid delivery pump; 93-dilute hydrochloric acid return line; 94-reboiler.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
As shown in fig. 1, the method for recovering hydrogen chloride gas from tail gas generated by burning chlorine-containing wastes of the embodiment comprises the following steps:
s1: rapidly cooling the incineration flue gas, introducing the incineration flue gas into the lower part of a lower circulating absorption section 4 of the washing tower 1, and introducing clear water from the top of the washing tower 1;
s2: liquid passes through an upper section absorption section 2, a middle section circulating absorption section 3 and a lower section circulating absorption section 4 of the water washing tower 1 in sequence under the action of overflow;
s3: hydrochloric acid is extracted from the bottom of the water scrubber 1, and tail gas is discharged from the top of the water scrubber 1;
s4: the hydrochloric acid in the step S3 is introduced into a hydrochloric acid desorption tower 7;
s5: dilute hydrochloric acid is extracted from the bottom of the hydrochloric acid desorption tower 7, and then the extracted dilute hydrochloric acid is introduced into the lower section circulating absorption section 4;
s6: hydrogen chloride gas is extracted from the top of the hydrochloric acid desorption tower 7.
According to the invention, the water washing tower 1 is divided into three sections, and the liquid is circulated in the middle section and the lower section, so that the hydrochloric acid discharged from the hydrochloric acid pipeline 6 can fully absorb the hydrogen chloride in the flue gas in the three sections, thereby improving the concentration of the hydrochloric acid product and reducing the content of the hydrogen chloride in the tail gas.
The liquid in the middle circulating absorption section 3 of the invention circulates in the middle circulating absorption section 3, the overflowed liquid enters the lower circulating absorption section 4, the liquid in the lower circulating absorption section 4 circulates in the lower circulating absorption section 4, and part of the liquid is discharged by the hydrochloric acid pipeline 6. Therefore, the liquid can be circulated for a long time in the middle-section circulating absorption section 3 and the lower-section circulating absorption section 4, the liquid is ensured to absorb the hydrogen chloride in the flue gas as much as possible, the concentration of the finished hydrochloric acid is further improved, and the 31 percent finished hydrochloric acid is finally prepared.
The high-concentration hydrochloric acid prepared by the water washing tower 1 is introduced into a hydrochloric acid desorption tower 7 to be desorbed to generate hydrogen chloride gas. The dilute hydrochloric acid after the hydrogen chloride gas is analyzed is introduced into the lower circulating absorption section 4 to be used for absorbing the hydrogen chloride in the tail gas, so that the whole system is free from hydrochloric acid generation, the system is completely balanced, and the economic and social benefits are considerable.
Specifically, in step S2, when the liquid passes through the lower cyclic absorption stage 4, the analyzed diluted hydrochloric acid and a part of the liquid that has passed through the lower cyclic absorption stage 4 and absorbed hydrogen chloride are returned to the lower liquid distributor 42 in the lower cyclic absorption stage 4. The liquid absorbing the hydrogen chloride by the lower circulating absorption section 4 and the resolved dilute hydrochloric acid are then conveyed to the lower liquid distributor 42 by the lower hydrochloric acid conveying pump 43, so that the liquid absorbing the hydrogen chloride in the flue gas of the upper section and the middle section can absorb the hydrogen chloride in the flue gas of the lower section in a circulating manner, and clear water is not introduced into the lower section, thereby ensuring that the concentration of the hydrochloric acid is gradually increased from top to bottom and ensuring that the concentration of the hydrochloric acid discharged from the hydrochloric acid pipeline 6 meets the requirement. Moreover, the diluted hydrochloric acid after desorption is introduced into the lower liquid return pipeline 41, so that no hydrochloric acid is generated in the system, and the system is completely balanced.
Part of the liquid which has absorbed hydrogen chloride through the lower circulating absorption section 4 is cooled before being sent back to the lower liquid distributor 42. And (3) sending out a part of hydrochloric acid generated from the bottom of the water washing tower 1 as finished hydrochloric acid, and continuously and circularly absorbing hydrogen chloride in the flue gas by a part of hydrochloric acid. The hydrogen chloride gas is dissolved into exothermic reaction, the heat released by the dissolution can be taken away by a first-stage hydrochloric acid cooler 44, and the absorption temperature is controlled to be below 40 ℃.
The liquid flowing down from the lower liquid distributor 42 passes through the lower packing 45. The lower section packing 45 can reduce the speed of the flue gas and the liquid, and ensure that the liquid can fully absorb the hydrogen chloride in the lower section flue gas in the lower section packing 45.
Specifically, in step S2, when the liquid passes through the middle-stage circulation absorption section 3, the liquid absorbing hydrogen chloride through the middle-stage circulation absorption section 3 is sent back to the middle-stage liquid distributor 34 in the middle-stage circulation absorption section 3; the liquid in the middle circulating absorption section 3 falls into the bottom 31 of the middle circulating absorption section and overflows to the lower circulating absorption section 4 from the gas lift pipe 32. The liquid absorbing the hydrogen chloride by the middle section circulating absorption section 3 is conveyed to the middle section liquid distributor 34 by the middle section hydrochloric acid conveying pump 35, so that the liquid absorbing the hydrogen chloride in the upper section flue gas can absorb the hydrogen chloride in the middle section flue gas in a circulating manner, instead of introducing clean water into the middle section, the concentration of the hydrochloric acid is ensured to be increased gradually from top to bottom, and the concentration of the hydrochloric acid discharged from the hydrochloric acid pipeline 6 is ensured to meet the requirement.
The flue gas rises from the gas rising pipe 32, and the middle tower bottom is prevented from blocking the flue gas. The liquid can be temporarily stored in the area enclosed by the middle tower bottom, the riser 32 and the water washing tower 1, and the middle-section hydrochloric acid delivery pump 35 can be ensured to pump the liquid in the middle tower bottom to the middle-section liquid distributor 34. The liquid accumulated in the middle tower bottom 31 overflows from the gas lift pipe 32 to a certain extent, so that the liquid entering the lower section is ensured to pass through the upper section and the middle section to fully absorb the hydrogen chloride in the flue gas. Three sections of absorption areas of the hydrogen chloride water washing tower 1 share one tower body, and liquid in the tower overflows in a multi-stage gravity mode without a pump for conveying the liquid.
The liquid which has absorbed hydrogen chloride through the middle circulating absorption section 3 is cooled before being sent back to the middle liquid distributor 34. The hydrogen chloride gas is dissolved into exothermic reaction, the heat released by the dissolution can be taken away by the secondary hydrochloric acid cooler 36, and the absorption temperature is controlled to be below 20 ℃.
The liquid flowing down from the middle section liquid distributor 34 passes through the middle section packing 37. The middle section filler 37 can reduce the speed of the flue gas and the liquid, and ensure that the liquid can fully absorb the hydrogen chloride in the middle section flue gas in the middle section filler 37.
Liquid above the riser 32 is blocked by the liquid blocking cap 38, leaving an overflow gap between the liquid blocking cap 38 and the riser 32. The liquid blocking cap 38 can block the liquid flowing down from the upper part, so that the liquid flowing down from the upper-section absorption section 2 and the middle-section liquid distributor 34 can only enter the bottom 31 of the middle-section tower, and the liquid in the middle section can circularly absorb the hydrogen chloride in the flue gas in the middle section.
Specifically, in step S2, when the liquid passes through the upper stage absorption stage 2, clean water is introduced to the upper side of the sieve plate 21. Desalted clear water is continuously added into the tower plates, and hydrogen chloride in tail gas is contacted with fresh water to finish the final hydrogen chloride washing absorption, so that the hydrogen chloride content entering alkali washing is further reduced, and the consumption of liquid alkali is reduced. The make-up quantity of the clean water is the same as the water quantity taken away by the finished hydrochloric acid, and the system balance is kept.
Specifically, in step S6, the analyzed hydrogen chloride gas is condensed to separate water, and the obtained hydrogen chloride gas is returned to the apparatus and used.
In step S5, heat exchange is performed between the hydrochloric acid before being introduced into the hydrochloric acid desorption tower 7 and the dilute hydrochloric acid extracted from the bottom of the hydrochloric acid desorption tower 7; part of dilute hydrochloric acid extracted from the bottom of the hydrochloric acid desorption tower 7 is reboiled and then sent back to the bottom of the hydrochloric acid desorption tower 7. The dilute hydrochloric acid is sent to the lower section circulating absorption pipeline through the dilute hydrochloric acid delivery pump 92 for absorbing the hydrogen chloride in the tail gas. The hydrochloric acid in the hydrochloric acid pipeline 6 and the dilute hydrochloric acid in the dilute hydrochloric acid conveying pipeline 9 exchange heat fully in the hydrochloric acid preheater 91, so that the temperature of the hydrochloric acid in the hydrochloric acid pipeline 6 is increased, and the analysis of hydrogen chloride gas is facilitated; and the temperature of the dilute hydrochloric acid in the dilute hydrochloric acid conveying pipeline 9 is reduced so as to ensure that the dilute hydrochloric acid fully absorbs the hydrogen chloride in the flue gas in the water washing tower 1.
As shown in fig. 2, the system used in the present invention:
comprises a water washing tower 1, wherein the lower section of the water washing tower 1 is provided with an incineration flue gas inlet 11, and the top of the water washing tower 1 is provided with a tail gas outlet 12; the washing tower 1 is provided with an upper section absorption section 2, a middle section circulating absorption section 3 and a lower section circulating absorption section 4 from top to bottom, the upper section absorption section 2 is connected with a water inlet pipe 5, and the lower section circulating absorption section 4 is connected with a hydrochloric acid pipeline 6; the other end of the hydrochloric acid pipeline 6 is connected with a hydrochloric acid desorption tower 7, the top of the hydrochloric acid desorption tower 7 is connected with a hydrogen chloride generation pipeline 8, the bottom of the hydrochloric acid desorption tower 7 is connected with a dilute hydrochloric acid conveying pipeline 9, and the other end of the dilute hydrochloric acid conveying pipeline 9 is connected with the lower section circulating absorption section 4.
According to the invention, the water washing tower 1 is divided into three sections, and the liquid is circulated in the middle section and the lower section, so that the hydrochloric acid discharged from the hydrochloric acid pipeline 6 can fully absorb the hydrogen chloride in the flue gas in the three sections, thereby improving the concentration of the hydrochloric acid product and reducing the content of the hydrogen chloride in the tail gas.
The liquid in the middle circulating absorption section 3 of the invention circulates in the middle circulating absorption section 3, the overflowed liquid enters the lower circulating absorption section 4, the liquid in the lower circulating absorption section 4 circulates in the lower circulating absorption section 4, and part of the liquid is discharged by the hydrochloric acid pipeline 6. Therefore, the liquid can be circulated for a long time in the middle-section circulating absorption section 3 and the lower-section circulating absorption section 4, the liquid is ensured to absorb the hydrogen chloride in the flue gas as much as possible, the concentration of the finished hydrochloric acid is further improved, and the 31 percent finished hydrochloric acid is finally prepared.
The high-concentration hydrochloric acid prepared by the water washing tower 1 is introduced into a hydrochloric acid desorption tower 7 to be desorbed to generate hydrogen chloride gas. The dilute hydrochloric acid after the hydrogen chloride gas is analyzed is introduced into the lower circulating absorption section 4 to be used for absorbing the hydrogen chloride in the tail gas, so that the whole system is free from hydrochloric acid generation, the system is completely balanced, and the economic and social benefits are considerable.
Specifically, the lower circulating absorption section 4 includes a lower liquid return pipeline 41, one end of the lower liquid return pipeline 41 is connected to the bottom of the water washing tower 1, the other end of the lower liquid return pipeline 41 is connected to a lower liquid distributor 42, the lower liquid distributor 42 is located below the lower circulating absorption section 3, a lower hydrochloric acid delivery pump 43 is installed on the lower liquid return pipeline 41, the hydrochloric acid pipeline 6 is connected to the lower liquid return pipeline 41, and the dilute hydrochloric acid delivery pipeline 9 is connected to the lower liquid return pipeline 41. The liquid absorbing the hydrogen chloride by the lower circulating absorption section 4 and the resolved dilute hydrochloric acid are then conveyed to the lower liquid distributor 42 by the lower hydrochloric acid conveying pump 43, so that the liquid absorbing the hydrogen chloride in the flue gas of the upper section and the middle section can absorb the hydrogen chloride in the flue gas of the lower section in a circulating manner, and clear water is not introduced into the lower section, thereby ensuring that the concentration of the hydrochloric acid is gradually increased from top to bottom and ensuring that the concentration of the hydrochloric acid discharged from the hydrochloric acid pipeline 6 meets the requirement. Moreover, the diluted hydrochloric acid after desorption is introduced into the lower liquid return pipeline 41, so that no hydrochloric acid is generated in the system, and the system is completely balanced.
The lower-section liquid return pipeline 41 is also provided with a first-stage hydrochloric acid cooler 44. And (3) sending out a part of hydrochloric acid generated from the bottom of the water washing tower 1 as finished hydrochloric acid, and continuously and circularly absorbing hydrogen chloride in the flue gas by a part of hydrochloric acid. The hydrogen chloride gas is dissolved into exothermic reaction, the heat released by the dissolution can be taken away by the first-stage hydrochloric acid cooler 44, and the absorption temperature is controlled to be about 20 ℃.
The washing tower 1 is also provided with a lower section filler 45, and the lower section filler 45 is positioned between the incineration flue gas inlet 11 and the lower section liquid distributor 42. The lower section packing 45 can reduce the speed of the flue gas and the liquid, and ensure that the liquid can fully absorb the hydrogen chloride in the lower section flue gas in the lower section packing 45.
Specifically, the middle-section circulating absorption section 3 comprises a middle-section tower bottom 31, the middle-section tower bottom 31 is positioned above the lower-section circulating absorption section 4, and a riser 32 is connected to the middle-section tower bottom 31; middle section circulation absorption section 3 still includes middle section liquid return pipeline 33, and the one end of middle section liquid return pipeline 33 is connected in the position that water scrubber 1 is close to middle section bottom of the tower 31 from the upside, and the other end that liquid pipeline 33 was returned to the middle section is connected with middle section liquid distributor 34, and middle section liquid distributor 34 is located 2 below of upper segment absorption section, installs middle section hydrochloric acid delivery pump 35 on the liquid pipeline 33 is returned to the middle section. The liquid absorbing the hydrogen chloride by the middle section circulating absorption section 3 is conveyed to the middle section liquid distributor 34 by the middle section hydrochloric acid conveying pump 35, so that the liquid absorbing the hydrogen chloride in the upper section flue gas can absorb the hydrogen chloride in the middle section flue gas in a circulating manner, instead of introducing clean water into the middle section, the concentration of the hydrochloric acid is ensured to be increased gradually from top to bottom, and the concentration of the hydrochloric acid discharged from the hydrochloric acid pipeline 6 is ensured to meet the requirement.
The flue gas rises from the gas rising pipe 32, and the middle tower bottom is prevented from blocking the flue gas. The liquid can be temporarily stored in the area enclosed by the middle tower bottom, the riser 32 and the water washing tower 1, and the middle-section hydrochloric acid delivery pump 35 can be ensured to pump the liquid in the middle tower bottom to the middle-section liquid distributor 34. The liquid accumulated in the middle tower bottom 31 overflows from the gas lift pipe 32 to a certain extent, so that the liquid entering the lower section is ensured to pass through the upper section and the middle section to fully absorb the hydrogen chloride in the flue gas. Three sections of absorption areas of the hydrogen chloride water washing tower 1 share one tower body, and liquid in the tower overflows in a multi-stage gravity mode without a pump for conveying the liquid.
And a secondary hydrochloric acid cooler 36 is also arranged on the middle-section liquid return pipeline 33. The hydrogen chloride gas is dissolved into exothermic reaction, the heat released by the dissolution can be taken away by the secondary hydrochloric acid cooler 36, and the absorption temperature is controlled to be about 20 ℃.
The washing tower 1 is also provided with a middle section filler 37, and the middle section filler 37 is positioned between the gas lift pipe 32 and the middle section liquid distributor 34. The middle section filler 37 can reduce the speed of the flue gas and the liquid, and ensure that the liquid can fully absorb the hydrogen chloride in the middle section flue gas in the middle section filler 37.
A liquid blocking cap 38 is arranged on the upper side of the gas rising pipe 32, and a gap is reserved between the liquid blocking cap 38 and the gas rising pipe 32. The liquid blocking cap 38 can block the liquid flowing down from the upper part, so that the liquid flowing down from the upper-section absorption section 2 and the middle-section liquid distributor 34 can only enter the bottom 31 of the middle-section tower, and the liquid in the middle section can circularly absorb the hydrogen chloride in the flue gas in the middle section.
Specifically, upper segment absorbs section 2 and includes sieve 21, and sieve 21 is located 3 upsides of middle section circulation absorption section, and inlet tube 5 is located the sieve 21 upside. Desalted clear water is continuously added into the tower plates, and hydrogen chloride in tail gas is contacted with fresh water to finish the final hydrogen chloride washing absorption, so that the hydrogen chloride content entering alkali washing is further reduced, and the consumption of liquid alkali is reduced. The make-up quantity of the clean water is the same as the water quantity taken away by the finished hydrochloric acid, and the system balance is kept.
Specifically, a hydrogen chloride cooler 81 is connected to the hydrogen chloride production line 8. The analyzed hydrogen chloride gas is condensed to separate water, and the obtained hydrogen chloride is sent back to the device for utilization.
The hydrochloric acid pipeline 6 is connected with a hydrochloric acid preheater 91, the dilute hydrochloric acid conveying pipeline 9 passes through the hydrochloric acid preheater 91, the dilute hydrochloric acid conveying pipeline 9 is connected with a dilute hydrochloric acid conveying pump 92, the dilute hydrochloric acid conveying pipeline 9 is also connected with a dilute hydrochloric acid return pipeline 93, the other end of the dilute hydrochloric acid return pipeline 93 is connected to the lower section of the hydrochloric acid desorption tower 7, and the dilute hydrochloric acid return pipeline 93 is connected with a reboiler 94.
The dilute hydrochloric acid is sent to the lower section circulating absorption pipeline through the dilute hydrochloric acid delivery pump 92 for absorbing the hydrogen chloride in the tail gas. The hydrochloric acid in the hydrochloric acid pipeline 6 and the dilute hydrochloric acid in the dilute hydrochloric acid conveying pipeline 9 exchange heat fully in the hydrochloric acid preheater 91, so that the temperature of the hydrochloric acid in the hydrochloric acid pipeline 6 is increased, and the analysis of hydrogen chloride gas is facilitated; and the temperature of the dilute hydrochloric acid in the dilute hydrochloric acid conveying pipeline 9 is reduced so as to ensure that the dilute hydrochloric acid fully absorbs the hydrogen chloride in the flue gas in the water washing tower 1.
Note that a valve is installed in the hydrochloric acid line 6.
The upper part of the washing tower 1 is a clear water absorption area tower tray section. The tray can be operated under the working condition of smaller liquid flow to maintain the water balance of the system and avoid the excessive hydrochloric acid generated by large water consumption. And tail gas obtained after hydrogen chloride is absorbed in the middle section of the water washing tower 1 enters a clear water absorption area. Clear water is continuously added into the tower plates, and hydrogen chloride in tail gas is contacted with fresh water to finish the final hydrogen chloride washing absorption, so that the hydrogen chloride content entering alkali washing is further reduced, and the consumption of liquid alkali is reduced. The make-up quantity of the clean water is the same as the water quantity taken away by the finished hydrochloric acid, and the system balance is kept.
The concentration of the hydrogen chloride in the flue gas is in direct proportion to the concentration of the acid obtained by absorption, and the lower the concentration of the absorption liquid is, the more beneficial to the absorption of the hydrogen chloride is. The concentration of the hydrogen chloride in the flue gas is gradually reduced from bottom to top along the concentration partition of the water washing tower 1, the concentration of the absorption liquid of the water washing tower 1 is gradually increased from top to bottom, and the tail gas and the absorption liquid form a concentration gradient, so that the absorption of the hydrogen chloride is facilitated, and the content of the hydrogen chloride in the tail gas after water washing is reduced.
The three sections of absorption areas of the water washing tower 1 share one tower body, and liquid in the tower is designed to overflow from top to bottom by gravity flow. Compared with a multi-tower type, the device has the advantages of small quantity of equipment, small occupied area and no need of controlling liquid levels in different absorption areas.
Hydrochloric acid obtained from the bottom of the water washing tower 1 is preheated by dilute acid at the bottom of the hydrochloric acid analysis tower, then the hydrochloric acid is sent to the hydrochloric acid analysis tower, chlorinated hydrogen in the hydrochloric acid is analyzed out through steam heating, the analyzed gas at the top of the tower is separated from water through condensation, the obtained hydrogen chloride is sent back to the device for utilization, and the dilute acid obtained from the tower bottom is sent to the water washing tower 1 after being cooled by the hydrochloric acid sent from the water washing tower 1 and then is sent back to the water washing tower 1 for absorbing the hydrogen chloride in the incineration tail gas. The whole system is balanced, and no redundant hydrochloric acid is generated.
The invention is not limited to the above alternative embodiments, and any other various forms of products can be obtained by anyone in the light of the present invention, but any changes in shape or structure thereof, which fall within the scope of the present invention as defined in the claims, fall within the scope of the present invention.
Claims (10)
1. A method for recovering hydrogen chloride gas in tail gas generated in the incineration of chlorine-containing wastes is characterized by comprising the following steps:
s1: rapidly cooling incineration flue gas, introducing the incineration flue gas into the lower part of a lower circulating absorption section (4) of a water washing tower (1), and introducing clear water from the top of the water washing tower (1);
s2: liquid passes through an upper section absorption section (2), a middle section circulating absorption section (3) and a lower section circulating absorption section (4) of the water washing tower (1) in sequence under the action of overflow;
s3: hydrochloric acid is extracted from the bottom of the water scrubber (1), and tail gas is discharged from the top of the water scrubber (1);
s4: the hydrochloric acid in the step S3 is introduced into a hydrochloric acid desorption tower (7);
s5: dilute hydrochloric acid is extracted from the bottom of the hydrochloric acid desorption tower (7), and then the extracted dilute hydrochloric acid is introduced into the lower section circulating absorption section (4);
s6: hydrogen chloride gas is extracted from the top of the hydrochloric acid desorption tower (7).
2. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration tail gas as claimed in claim 1, wherein in step S2, when the liquid passes through the lower circulating absorption section (4), the desorbed dilute hydrochloric acid and part of the liquid passing through the lower circulating absorption section (4) for absorbing hydrogen chloride are returned to the lower liquid distributor (42) in the lower circulating absorption section (4).
3. The method for recovering hydrogen chloride gas from tail gas generated by incineration of chlorine-containing wastes as claimed in claim 2, characterized in that in step S2, the liquid partially absorbed with hydrogen chloride by passing through the lower circulating absorption stage (4) is cooled before being sent back to the lower liquid distributor (42).
4. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration off-gas as claimed in claim 2, wherein in step S2, the liquid flowing down from the lower liquid distributor (42) passes through the lower packing (45).
5. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration off-gas as claimed in claim 1, wherein in step S2, the liquid absorbing hydrogen chloride through the middle-cycle absorbing stage (3) is returned to the middle-cycle liquid distributor (34) in the middle-cycle absorbing stage (3) while the liquid passes through the middle-cycle absorbing stage (3); the liquid in the middle section circulating absorption section (3) falls into the bottom (31) of the middle section tower and overflows to the lower section circulating absorption section (4) from the gas lift pipe (32).
6. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration tail gas as claimed in claim 5, characterized in that in step S2, the liquid absorbed hydrogen chloride by the middle circulation absorption section (3) is cooled before being sent back to the middle liquid distributor (34).
7. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration off-gas as claimed in claim 5, characterized in that in step S2, the liquid flowing down from the middle stage liquid distributor (34) passes through the middle stage packing (37).
8. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration off-gas as claimed in claim 5, characterized in that in step S2, the liquid above the lift tube (32) is blocked by the liquid-blocking cap (38), leaving an overflow gap between the liquid-blocking cap (38) and the lift tube (32).
9. The method for recovering hydrogen chloride gas from tail gas generated by incineration of chlorine-containing wastes as claimed in claim 1, wherein in step S2, clean water is introduced into the upper side of the sieve plate (21) while passing through the upper absorption stage (2).
10. The method for recovering hydrogen chloride gas from chlorine-containing waste incineration tail gas as claimed in any one of claims 1 to 9, characterized in that in step S5, heat exchange is performed between hydrochloric acid before being introduced into the hydrochloric acid desorption tower (7) and dilute hydrochloric acid withdrawn from the bottom of the hydrochloric acid desorption tower (7); part of dilute hydrochloric acid extracted from the bottom of the hydrochloric acid desorption tower (7) is reboiled and then sent back to the bottom of the hydrochloric acid desorption tower (7).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253606A (en) * | 2022-08-16 | 2022-11-01 | 无锡雪浪环境科技股份有限公司 | Comprehensive hazardous waste incineration flue gas treatment method |
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| EP1789160A1 (en) * | 2004-09-13 | 2007-05-30 | Basf Aktiengesellschaft | Method for separating hydrogen chloride and phosgene |
| CN101348534A (en) * | 2007-07-17 | 2009-01-21 | 王凯勋 | Method for realizing hydrochloric acid closed cycle and precluding mercury pollution in polychloroethylene production |
| CN111701404A (en) * | 2020-04-30 | 2020-09-25 | 中国成达工程有限公司 | Hydrogen chloride absorption treatment method and device and application |
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- 2021-11-29 CN CN202111429508.XA patent/CN114053837A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1789160A1 (en) * | 2004-09-13 | 2007-05-30 | Basf Aktiengesellschaft | Method for separating hydrogen chloride and phosgene |
| CN101348534A (en) * | 2007-07-17 | 2009-01-21 | 王凯勋 | Method for realizing hydrochloric acid closed cycle and precluding mercury pollution in polychloroethylene production |
| CN111701404A (en) * | 2020-04-30 | 2020-09-25 | 中国成达工程有限公司 | Hydrogen chloride absorption treatment method and device and application |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115253606A (en) * | 2022-08-16 | 2022-11-01 | 无锡雪浪环境科技股份有限公司 | Comprehensive hazardous waste incineration flue gas treatment method |
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