CN113912011A - Method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas - Google Patents
Method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas Download PDFInfo
- Publication number
- CN113912011A CN113912011A CN202111430599.9A CN202111430599A CN113912011A CN 113912011 A CN113912011 A CN 113912011A CN 202111430599 A CN202111430599 A CN 202111430599A CN 113912011 A CN113912011 A CN 113912011A
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- section
- liquid
- tail gas
- absorption section
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 382
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 239000000460 chlorine Substances 0.000 title claims abstract description 29
- 229910052801 chlorine Inorganic materials 0.000 title claims abstract description 29
- 238000004064 recycling Methods 0.000 title claims abstract description 19
- 238000004056 waste incineration Methods 0.000 title claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 175
- 238000010521 absorption reaction Methods 0.000 claims abstract description 124
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 78
- 229910001868 water Inorganic materials 0.000 claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 63
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000003546 flue gas Substances 0.000 claims abstract description 62
- 238000005406 washing Methods 0.000 claims abstract description 58
- 238000000034 method Methods 0.000 claims abstract description 16
- 239000002699 waste material Substances 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 238000007599 discharging Methods 0.000 claims abstract description 4
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 91
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 91
- 238000012856 packing Methods 0.000 claims description 12
- 239000011347 resin Substances 0.000 claims description 8
- 229920005989 resin Polymers 0.000 claims description 8
- 238000001179 sorption measurement Methods 0.000 claims description 8
- 239000005416 organic matter Substances 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 4
- 125000004122 cyclic group Chemical group 0.000 abstract description 2
- 239000000945 filler Substances 0.000 description 12
- 239000003513 alkali Substances 0.000 description 9
- 230000000903 blocking effect Effects 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000004090 dissolution Methods 0.000 description 6
- 239000013505 freshwater Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 206010015137 Eructation Diseases 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2045—Hydrochloric acid
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention belongs to the technical field of chemical industry, and particularly relates to a method for producing 31% hydrochloric acid by recycling incineration tail gas of chlorine-containing waste. The technical scheme is as follows: a method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid 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: part of hydrochloric acid flowing out of the bottom of the water washing tower after passing through the lower section of the circulating absorption section is extracted to be used as finished hydrochloric acid; and discharging tail gas from the top of the water washing tower. The invention provides a method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas by adopting a multi-section combined tower for cyclic absorption to improve the concentration of hydrochloric acid.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a method for producing 31% hydrochloric acid by recycling 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 tail gas is less than 4% (v), the hydrochloric acid concentration obtained by absorbing hydrogen chloride in the flue gas with water is low, and the hydrochloric acid concentration obtained by recovering hydrogen chloride gas in the incineration tail gas is about 18%. Since the concentration of industrial finished hydrochloric acid is 31%, the dilute hydrochloric acid of 18% -21% is difficult to be industrially applied, cannot be sold as a commodity, and is difficult to be processed by other methods. 31 percent of finished hydrochloric acid is prepared by introducing high-purity hydrogen chloride gas for absorption or 31 percent of finished hydrochloric acid is prepared by absorbing the diluted hydrochloric acid after analysis. However, hydrochloric acid in the chemical industry is excessive, and if 31% of finished hydrochloric acid is prepared by introducing high-purity hydrogen chloride gas for absorption, the actually produced hydrochloric acid amount is more and the high-purity hydrogen chloride gas is wasted. The dilute hydrochloric acid analysis process is complex, high in energy consumption and poor in economical efficiency. Therefore, optimizing the hydrogen chloride absorption process in the incineration tail gas to produce 31% of finished hydrochloric acid is a core technology for recycling chlorine-containing wastes.
The invention adopts a multi-section combined tower to absorb the hydrogen chloride in the incineration tail gas, greatly reduces the water consumption and the hydrogen chloride in the tail gas, and simultaneously improves the concentration of hydrochloric acid produced by absorbing HCl by reducing the temperature of a water washing tower, so that 31 percent of finished hydrochloric acid can be obtained, and the invention has considerable economic and social benefits.
Disclosure of Invention
In order to solve the problems in the prior art, the invention aims to provide a method for producing 31% hydrochloric acid by using the recovered chlorine-containing waste incineration tail gas, which adopts a multi-section combined tower for cyclic absorption to improve the concentration of the hydrochloric acid.
The technical scheme adopted by the invention is as follows:
a method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid 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: part of hydrochloric acid flowing out of the bottom of the water washing tower after passing through the lower section of the circulating absorption section is extracted to be used as finished hydrochloric acid; and discharging tail gas from the top of the water washing 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 a finished hydrochloric acid pipeline fully absorbs hydrogen chloride in flue gas in the three sections, thereby improving the concentration of the 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 finished 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.
In a preferred embodiment of the present invention, in step S2, a part of the hydrochloric acid flowing out from the bottom of the water washing column is returned to the lower liquid distributor in the lower circulating absorption stage. The liquid absorbing the hydrogen chloride by the lower circulating absorption section is 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, instead of introducing clean water into the lower 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 finished hydrochloric acid pipeline is ensured to meet the requirement.
In a preferred embodiment of the present invention, in step S3, the extracted hydrochloric acid is passed through a resin adsorption column to remove free chlorine and a small amount of organic substances. And removing free chlorine and a small amount of organic matters of the hydrochloric acid by a resin adsorption tower to obtain the finished hydrochloric acid.
In a preferred embodiment of the present invention, in step S2, the hydrochloric acid is cooled while returning a part of the extracted hydrochloric acid 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 about 20 ℃.
In a preferred embodiment of the present invention, in step S2, after part of the extracted hydrochloric acid is returned to the lower liquid distributor, the liquid is passed 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 finished 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.
The invention has the beneficial effects that:
1. the water washing tower is divided into three sections, so that hydrochloric acid discharged from a finished hydrochloric acid pipeline fully absorbs hydrogen chloride in flue gas in the three sections, the concentration of the hydrochloric acid is improved, and the content of the hydrogen chloride in tail gas is reduced.
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 finished 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.
Drawings
FIG. 1 is a flow chart of a method of the present invention;
FIG. 2 is a schematic diagram of the structure of a combined column 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-finished hydrochloric acid 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-a resin adsorption column; 45-first order hydrochloric acid cooler; 46-lower packing.
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 producing 31% hydrochloric acid by recycling the tail gas from incineration of chlorine-containing waste 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: part of hydrochloric acid flowing out of the bottom of the water washing tower 1 after passing through the lower circulating absorption section 4 is extracted to be used as finished hydrochloric acid; and discharging tail gas from the top of the water washing tower 1.
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 finished 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 section circulating absorption section 3 of the invention circulates in the middle section circulating absorption section 3, the overflowed liquid enters the lower section circulating absorption section 4, the liquid in the lower section circulating absorption section 4 circulates in the lower section circulating absorption section 4, and part of the liquid is discharged from the finished product 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.
Specifically, in step S2, a part of the hydrochloric acid flowing out of the bottom of the water scrubber 1 is returned to the lower liquid distributor 42 in the lower circulating absorption stage 4. The liquid absorbing the hydrogen chloride by the lower circulating absorption section 4 is 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, instead of introducing clean water into the lower 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 finished hydrochloric acid pipeline 6 is ensured to meet the requirement.
In step S3, the withdrawn hydrochloric acid is passed through a resin adsorption column 44 to remove free chlorine and a small amount of organic matter. Free chlorine and a small amount of organic matters of the hydrochloric acid are removed by a resin adsorption tower 44 to obtain the finished hydrochloric acid.
In step S2, the hydrochloric acid is cooled while returning a part of the extracted hydrochloric acid 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 the first-stage hydrochloric acid cooler 45, and the absorption temperature is controlled to be about 20 ℃.
In step S2, after a part of the extracted hydrochloric acid is returned to the lower liquid distributor 42, the liquid is passed through the lower packing 46. The lower section packing 46 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 46.
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 finished product 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.
In step S2, the liquid having absorbed hydrogen chloride via the middle-stage circulation absorption stage 3 is cooled before being sent back to the middle-stage 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 ℃.
In step S2, the liquid flowing down from the middle-stage liquid distributor 34 passes through the middle-stage 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.
In step S2, liquid is blocked from above the draft tube 32 by the liquid deflector cap 38, leaving an overflow gap between the liquid deflector cap 38 and the draft tube 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.
As shown in fig. 2, the combined tower used in this example:
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 circulation absorption section 3 and a lower section circulation 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 circulation absorption section 4 is connected with a finished hydrochloric acid pipeline 6.
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 finished 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 section circulating absorption section 3 of the invention circulates in the middle section circulating absorption section 3, the overflowed liquid enters the lower section circulating absorption section 4, the liquid in the lower section circulating absorption section 4 circulates in the lower section circulating absorption section 4, and part of the liquid is discharged from the finished product 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 lower circulating absorption section 4 comprises a lower liquid return pipeline 41, one end of the lower liquid return pipeline 41 is connected with the bottom of the water washing tower 1, the other end of the lower liquid return pipeline 41 is connected with a lower liquid distributor 42, the lower liquid distributor 42 is positioned below the lower circulating absorption section 3, a lower hydrochloric acid delivery pump 43 is mounted on the lower liquid return pipeline 41, and the finished hydrochloric acid pipeline 6 is connected to the lower liquid return pipeline 41. The liquid absorbing the hydrogen chloride by the lower circulating absorption section 4 is 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, instead of introducing clean water into the lower 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 finished hydrochloric acid pipeline 6 is ensured to meet the requirement.
Wherein, a resin adsorption tower 44 is arranged on the finished product hydrochloric acid pipeline 6. Free chlorine and a small amount of organic matters of the hydrochloric acid are removed by a resin adsorption tower 44 to obtain the finished hydrochloric acid.
And a primary hydrochloric acid cooler 45 is also arranged on the lower liquid return pipeline 41. 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 45, and the absorption temperature is controlled to be about 20 ℃.
The washing tower 1 is also provided with a lower section of filler 46, and the lower section of filler 46 is positioned between the incineration flue gas inlet 11 and the lower section of liquid distributor 42. The lower section packing 46 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 46.
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 gas raising pipe 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 finished product 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.
Wherein, a secondary hydrochloric acid cooler 36 is also installed on the middle-section liquid returning 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 below 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.
The upper section absorbing section 2 comprises a sieve plate 21, the sieve plate 21 is positioned on the upper side of the middle section circulating absorbing section 3, and the water inlet pipe 5 is positioned on 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.
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.
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 recycling tail gas generated by incineration of chlorine-containing waste to produce 31% hydrochloric acid 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: part of hydrochloric acid flowing out of the bottom of the water washing tower (1) after passing through the lower section circulating absorption section (4) is extracted to be used as finished hydrochloric acid; and (3) discharging tail gas from the top of the water washing tower (1).
2. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 1, characterized in that in step S2, part of the hydrochloric acid flowing out of the bottom of the water wash tower (1) is returned to the lower liquid distributor (42) in the lower circulating absorption section (4).
3. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 1, characterized in that in step S3, the produced hydrochloric acid is passed through a resin adsorption tower (44) to remove free chlorine and a small amount of organic matter.
4. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 2, characterized in that in step S2, the hydrochloric acid is cooled while returning part of the mined hydrochloric acid to the lower liquid distributor (42).
5. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 2, characterized in that in step S2, after part of the mined hydrochloric acid is returned to the lower liquid distributor (42), the liquid is passed through the lower packing (46).
6. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 1, characterized in that in step S2, when the liquid passes through the middle-cycle absorption section (3), the liquid absorbing hydrogen chloride through the middle-cycle absorption section (3) is sent back to the middle-cycle liquid distributor (34) in the middle-cycle absorption section (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).
7. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 6, characterized in that in step S2, the liquid absorbed hydrogen chloride by the middle-cycle absorption section (3) is cooled before being sent back to the middle-cycle liquid distributor (34).
8. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 6, characterized in that in step S2, the liquid flowing down from the middle stage liquid distributor (34) passes through the middle stage packing (37).
9. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to claim 6, characterized in that in step S2, the 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).
10. The method for recycling chlorine-containing waste incineration tail gas to produce 31% hydrochloric acid according to any one of claims 1 to 9, characterized in that in step S2, clear water is introduced into the upper side of the sieve plate (21) while the liquid passes through the upper absorption section (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111430599.9A CN113912011A (en) | 2021-11-29 | 2021-11-29 | Method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111430599.9A CN113912011A (en) | 2021-11-29 | 2021-11-29 | Method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113912011A true CN113912011A (en) | 2022-01-11 |
Family
ID=79248096
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111430599.9A Pending CN113912011A (en) | 2021-11-29 | 2021-11-29 | Method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113912011A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116036800A (en) * | 2023-01-09 | 2023-05-02 | 中国成达工程有限公司 | Method and system for treating and utilizing chlorinated tail gas |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003261306A (en) * | 2002-03-08 | 2003-09-16 | Sumitomo Chem Co Ltd | Method for separating gaseous chlorine and hydrogen chloride |
| CN101235160A (en) * | 2006-12-30 | 2008-08-06 | 仇晓丰 | Hydrogen chloride whole reclaiming zero discharging technique and device for PVC producing process |
| CN101549247A (en) * | 2009-04-29 | 2009-10-07 | 上海宝钢工程技术有限公司 | Absorption tower technical method of multi-stage spraying and desorbing ammonia in gas |
| CN102198361A (en) * | 2011-05-19 | 2011-09-28 | 蒋超 | Hydrogen chloride tail gas recovery equipment |
| CN102557861A (en) * | 2011-12-30 | 2012-07-11 | 中国成达工程有限公司 | Gas and liquid-phase mercury efficient recycling and hydrochloric acid fully-closed loop circulation technology of acetylene-method vinyl chloride device |
| CN110360577A (en) * | 2019-08-16 | 2019-10-22 | 江苏鼎新环保科技有限公司 | A kind of processing system of liquid waste incineration containing chlorine |
| CN210186789U (en) * | 2019-06-06 | 2020-03-27 | 苏州艾特斯环保设备有限公司 | High-temperature hydrogen chloride waste gas treatment device with ionic membrane |
-
2021
- 2021-11-29 CN CN202111430599.9A patent/CN113912011A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003261306A (en) * | 2002-03-08 | 2003-09-16 | Sumitomo Chem Co Ltd | Method for separating gaseous chlorine and hydrogen chloride |
| CN101235160A (en) * | 2006-12-30 | 2008-08-06 | 仇晓丰 | Hydrogen chloride whole reclaiming zero discharging technique and device for PVC producing process |
| CN101549247A (en) * | 2009-04-29 | 2009-10-07 | 上海宝钢工程技术有限公司 | Absorption tower technical method of multi-stage spraying and desorbing ammonia in gas |
| CN102198361A (en) * | 2011-05-19 | 2011-09-28 | 蒋超 | Hydrogen chloride tail gas recovery equipment |
| CN102557861A (en) * | 2011-12-30 | 2012-07-11 | 中国成达工程有限公司 | Gas and liquid-phase mercury efficient recycling and hydrochloric acid fully-closed loop circulation technology of acetylene-method vinyl chloride device |
| CN210186789U (en) * | 2019-06-06 | 2020-03-27 | 苏州艾特斯环保设备有限公司 | High-temperature hydrogen chloride waste gas treatment device with ionic membrane |
| CN110360577A (en) * | 2019-08-16 | 2019-10-22 | 江苏鼎新环保科技有限公司 | A kind of processing system of liquid waste incineration containing chlorine |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116036800A (en) * | 2023-01-09 | 2023-05-02 | 中国成达工程有限公司 | Method and system for treating and utilizing chlorinated tail gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104474849B (en) | Acid regeneration acid gas absorbs and tail gas emission system and Application way thereof | |
| CN102060406A (en) | Closed-loop processing integrated process for high-efficiency air stripping and tail-gas ammonia recycling of ammonia-nitrogen wastewater | |
| CN113912011A (en) | Method for producing 31% hydrochloric acid by recycling chlorine-containing waste incineration tail gas | |
| CN102992351A (en) | Method and device for purifying ammonia recovered from coal chemical industry wastewater | |
| CN114053837A (en) | Method for recovering hydrogen chloride gas in tail gas generated in incineration of chlorine-containing waste | |
| CN220926287U (en) | System for reducing ammonia content of heavy alkali in sodium carbonate production process | |
| CN110127615A (en) | Mannheim proeess produces the online purification process of hydrochloric acid in Process of Potassium Sulfate | |
| CN216273101U (en) | Combined tower for producing 31% hydrochloric acid by recovering chlorine-containing waste incineration tail gas | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN213433774U (en) | Organic tail gas purification system | |
| CN108671747A (en) | A kind of method and system discharging recycling purification helium in exhaust gas from preform sintering furnace | |
| CN105480948B (en) | A kind of aliphatic acid or fat acyl chloride chlorination production byproduct in process object hydrogen chloride circulation utilization method and system | |
| CN109232171B (en) | Method for completely removing acidic substances in crude vinyl chloride gas | |
| CN216273100U (en) | System for retrieve hydrogen chloride gas in chlorine waste burns tail gas | |
| CN201101938Y (en) | Completely recycling system for hydrogen chloride in industry gas | |
| CN212417897U (en) | Device for accelerating parking replacement of vinyl acetate production system | |
| CN202265523U (en) | Production system for coking crude phenol | |
| CN213101516U (en) | Hydrogen chloride absorbs processing apparatus | |
| CN204727616U (en) | For ammonia decontamination system and the phenol ammonia recovery unit thereof of crushed coal pressure gasifying sewage treatment process | |
| CN211384500U (en) | Power plant desulfurization system | |
| CN103523798A (en) | Improved device and method for dephenolization and desulfuration according to ammonium hydroxide washing method | |
| CN208949058U (en) | A kind of coal gasification phenol wastewater ammonia still process extraction multiple treating system | |
| CN209771799U (en) | Comprehensive recycling system for PVC (polyvinyl chloride) waste alkali and gas burning kiln waste gas | |
| CN216223692U (en) | Chloroethylene purification device | |
| CN217855394U (en) | Hydrogen fluoride gas absorbing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20220111 |