CN109758874B - Environment-friendly process for purifying tail gas in potassium sulfate production - Google Patents
Environment-friendly process for purifying tail gas in potassium sulfate production Download PDFInfo
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- CN109758874B CN109758874B CN201910181822.7A CN201910181822A CN109758874B CN 109758874 B CN109758874 B CN 109758874B CN 201910181822 A CN201910181822 A CN 201910181822A CN 109758874 B CN109758874 B CN 109758874B
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- 238000000034 method Methods 0.000 title claims abstract description 60
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 53
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 title claims abstract description 30
- 229910052939 potassium sulfate Inorganic materials 0.000 title claims abstract description 30
- 235000011151 potassium sulphates Nutrition 0.000 title claims abstract description 30
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 297
- 238000010521 absorption reaction Methods 0.000 claims abstract description 261
- 238000005406 washing Methods 0.000 claims abstract description 254
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 216
- 239000007788 liquid Substances 0.000 claims abstract description 159
- 238000001816 cooling Methods 0.000 claims abstract description 63
- 239000002253 acid Substances 0.000 claims abstract description 58
- 239000000498 cooling water Substances 0.000 claims abstract description 56
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 25
- 229910002804 graphite Inorganic materials 0.000 claims abstract description 25
- 239000010439 graphite Substances 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims description 203
- 239000011552 falling film Substances 0.000 claims description 109
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 53
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 44
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 44
- 238000011084 recovery Methods 0.000 claims description 19
- 239000011265 semifinished product Substances 0.000 claims description 18
- 239000012071 phase Substances 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 239000007791 liquid phase Substances 0.000 claims description 10
- 239000000110 cooling liquid Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 7
- 239000000047 product Substances 0.000 claims description 6
- 239000008213 purified water Substances 0.000 claims description 3
- 239000001117 sulphuric acid Substances 0.000 claims description 3
- 235000011149 sulphuric acid Nutrition 0.000 claims description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides an environment-friendly process for purifying tail gas in potassium sulfate production, which carries out tail gas treatment through tail gas treatment equipment, wherein the tail gas treatment equipment comprises a tail gas conveying pipeline, a graphite cooler, a primary washing tower group, a secondary washing tower group, a primary absorption tower group, a secondary absorption tower group, a gas-liquid separator, an acid making bucket, a hydrochloric acid intermediate tank and a water circulation cooling assembly, and the process flow of the environment-friendly process comprises tail gas cooling, acid B production, acid A production, dilute hydrochloric acid production and cooling water circulation. And meets the environmental protection requirements of energy conservation and emission reduction.
Description
Technical Field
The invention relates to the technical field of potassium sulfate production, in particular to an environment-friendly process for purifying tail gas in potassium sulfate production.
Background
The potassium sulfate is an important chlorine-free potassium fertilizer containing sulfur and potassium elements, can be used in a plurality of fields, and has wide market demand.
The existing potassium sulfate production method mostly adopts the Mannheim method, and a large amount of hydrogen chloride tail gas can be generated in the process of producing the potassium sulfate and can be used as a production raw material of a byproduct, namely hydrochloric acid. The existing potassium sulfate production enterprises are poor in matched treatment equipment, only provide primary cooling and washing of hydrogen chloride tail gas, and the prepared hydrochloric acid is poor in quality and poor in sales route, and the tail gas treatment is incomplete, so that the emission requirement is not met, extra purification is needed, the treatment cost is improved, and the profit of byproducts is low.
Disclosure of Invention
Aiming at the problems, the invention provides an environment-friendly process for purifying tail gas in potassium sulfate production.
The specific technical scheme is as follows:
the environment-friendly process for purifying the tail gas generated in the production of potassium sulfate is characterized in that tail gas treatment is carried out by tail gas treatment equipment, and the process flow of the environment-friendly process comprises tail gas cooling, acid B production, acid A production, dilute hydrochloric acid production and cooling water circulation.
The tail gas treatment equipment comprises a tail gas conveying pipeline, a graphite cooler, a primary washing tower group, a secondary washing tower group, a primary absorption tower group, a secondary absorption tower group, a gas-liquid separator, an acid making water bucket, a hydrochloric acid intermediate tank and a water circulating cooling assembly, wherein the primary washing tower group is formed by connecting 2 sulfuric acid gas washing towers in series, the secondary washing tower group is formed by connecting 4 sulfuric acid gas washing towers in series, the primary absorption tower group is formed by connecting 3 falling film absorption tower groups, the secondary absorption tower group is formed by connecting 2 falling film absorption tower groups, the hydrochloric acid intermediate tank comprises an A-level hydrochloric acid intermediate tank and a B-level hydrochloric acid intermediate tank, and the water circulating cooling assembly comprises a water return bucket, a circulating water tank, a hot water pump group, a water cooling tower, a cold water pump group, a cooling water storage tank and a water distributor;
the tail gas conveying pipeline is communicated with the Mannheim reaction furnace and receives tail gas discharged by the Mannheim reaction furnace, the graphite cooler comprises a tail gas inlet a1, a cooling liquid inlet a2, a steam outlet a3 and a cooling outlet a4, the tail gas inlet a1 is communicated with the tail gas conveying pipeline and receives the tail gas, the cooling liquid inlet a2 is communicated with the water distributor, the steam outlet a3 is communicated with the water return hopper, and the cooling outlet a4 is communicated with the primary washing tower group;
the sulfuric acid gas washing tower comprises a washing inlet B1, an acid liquid inlet and outlet B2, a washing outlet B3 and a circulating pipeline B4, the sulfuric acid gas washing tower in a primary washing tower group is divided into a washing tower number B1 and a washing tower number B2 according to the front and back positions, the washing inlet B1 of the washing tower number B1 is communicated with a cooling outlet a4 of a graphite cooler, an acid liquid inlet and outlet B2 of the washing tower number B1 is communicated with an acid liquid inlet and outlet B2 of the washing tower number B2, a washing outlet B3 of the washing tower number B1 is communicated with a washing inlet B1 of the washing tower number B2, and two ends of the circulating pipeline B4 are respectively communicated with the top and the tail of the sulfuric acid gas washing tower, and is provided with a hydrochloric acid pump, a secondary cooling pipeline is connected on a circulating pipeline B4 of the No. B1 washing tower, a B-level hydrochloric acid conveying pipeline is connected on a circulating pipeline B4 of the No. B2 washing tower, the secondary cooling pipeline is communicated with a graphite cooler, and the B-level hydrochloric acid conveying pipeline is communicated with a B-level hydrochloric acid intermediate tank;
the 3 groups of falling film absorption tower groups forming the primary absorption tower group are sequentially connected in parallel, the 2 groups of falling film absorption tower groups forming the secondary absorption tower group are sequentially connected in parallel, and the falling film absorption tower group is formed by connecting 1 primary falling film absorption tower and 1 secondary falling film absorption tower in series;
in the primary absorption tower group, the primary falling film absorption tower comprises a falling film inlet c1, an absorption liquid inlet c2, an absorption liquid outlet c3, a tail gas outlet c4 and a circulating inlet c5, the secondary falling film absorption tower comprises a falling film inlet d1, an absorption liquid inlet d2, an absorption liquid outlet d3 and a tail gas outlet d4, the falling film inlet c1 of the primary falling film absorption tower is communicated with a washing outlet B3 of a No. B2 washing tower through a pipeline, the absorption liquid inlet c2 is communicated with a water distributor, the absorption liquid outlet c3 is communicated with an A-level hydrochloric acid intermediate tank, the tail gas outlet c4 is communicated with the falling film inlet d1 of the secondary falling film absorption tower, the absorption liquid inlet d2 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet d3 is communicated with a circulating inlet c5, and the tail gas outlet d4 is communicated with a secondary absorption pipeline;
in the secondary absorption tower group, the primary falling film absorption tower comprises a falling film inlet c6, an absorption liquid inlet c7, an absorption liquid outlet c8, a tail gas outlet c9 and a circulating inlet c10, the secondary falling film absorption tower comprises a falling film inlet d6, an absorption liquid inlet d7, an absorption liquid outlet d8 and a tail gas outlet d9, the falling film inlet c6 of the primary falling film absorption tower is communicated with a secondary absorption pipeline, the absorption liquid inlet c7 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet c8 is communicated with a rewashing pipeline, the tail gas outlet c9 is communicated with a falling film inlet d6 of the secondary falling film absorption tower, the absorption liquid inlet d7 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet d8 is communicated with a circulating inlet c10, and the tail gas outlet d9 is communicated with a gas-liquid separator;
the gas-liquid separator comprises a separation inlet e1, a gas-phase outlet e2 and a liquid-phase outlet e3, the separation inlet e1 is communicated with a tail gas outlet d9 through a pipeline, the gas-phase outlet e2 is communicated with a residual gas recovery pipeline, the liquid-phase outlet e3 is communicated with a second rewashing pipeline, exhaust pipes are arranged at the tops of the A-level hydrochloric acid intermediate tank and the B-level hydrochloric acid intermediate tank and are communicated with the residual gas recovery pipeline, and an HCL fan is arranged on the residual gas recovery pipeline;
the sulfuric acid gas washing tower in the secondary washing tower group is divided into a washing tower No. B3, a washing tower No. B4, a washing tower No. B5 and a washing tower No. B6 according to the front and back positions, in the secondary absorption tower group, an absorption liquid outlet c8 of a first-level falling film absorption tower on 2 groups of falling film absorption tower groups is respectively communicated with washing inlets B1 of the washing tower No. B4 and the washing tower No. B3 through a first rewashing pipeline, a gas phase outlet e2 of an exhaust pipe and a gas-liquid separator is communicated with a washing inlet B1 of the washing tower No. B3 through a residual gas recovery pipeline, a liquid phase outlet e3 of the gas-liquid separator is communicated with a washing inlet B6865 of the washing tower No. B3 through a second rewashing pipeline, a washing inlet B1 of the washing tower No. B6 is communicated with a process water pipeline, a washing outlet B3 of the washing tower No. B3 is communicated with a washing inlet B1 of the washing tower No. B4, a washing outlet B828653 of the washing tower is communicated with a washing tower No. B828653, a washing outlet B3 of the No. B5 washing tower is communicated with a washing inlet B1 of the No. B6 washing tower, and acid liquor inlets and outlets B2 of the adjacent 2 washing towers are communicated with each other;
in the secondary washing tower group, the circulating pipelines B4 of the washing tower No. B3, the washing tower No. B4, the washing tower No. B5 and the washing tower No. B6 are connected with unsaturated acid liquid pipelines, the acid making water barrel comprises a barrel inlet, an upper layer liquid outlet and a lower layer liquid outlet, the barrel inlet is communicated with an unsaturated acid liquid pipeline, the upper layer liquid outlet is communicated with a washing inlet B1 of a No. B3 washing tower through a pipeline, the lower layer liquid outlet is communicated with a cooling tower, the cooling tower comprises a feed port f1, a cooling water inlet f2, a steam outlet f3 and a discharge port f4, the feed port f1 is communicated with a lower liquid outlet, the cooling water inlet f2 is communicated with a water distributor, the steam outlet f3 is communicated with a water return hopper, the discharge port f4 is communicated with an unsaturated absorption liquid conveying pipeline, and the absorption liquid inlet d2 of the secondary falling film absorption tower in the primary absorption tower group and the secondary absorption tower group is communicated through a plurality of conveying branch pipes;
in the water circulation cooling assembly, the water return hopper receives water vapor and condenses the water vapor into hot water, the circulation water tank consists of a hot water tank and a cold water tank, the water return hopper is communicated with the hot water tank and is communicated with a cooling water tower through a hot water pump set, a water outlet of the cooling water tower is communicated with the cold water tank and is communicated with a cooling water storage tank through a cold water pump set, and the cooling water storage tank is communicated with a water distributor and supplies cooling water.
The environment-friendly process for purifying the tail gas generated in the production of potassium sulfate comprises the following specific processes:
(1) cooling tail gas: hydrogen chloride tail gas discharged by a Mannheim reaction furnace enters a graphite cooler through a tail gas conveying pipeline and a tail gas inlet a1 for cooling, cooling water is supplied by a water circulation cooling assembly, and enters the graphite cooler through a water distributor and a cooling liquid inlet a2, hydrogen chloride tail gas is dissolved into the cooling water and generates a large amount of heat to generate crude hydrochloric acid and generate a large amount of water vapor, the crude hydrochloric acid and part of hydrogen chloride tail gas which is not dissolved in water enter a primary washing tower group through a cooling outlet a4, and the water vapor enters a water return hopper through a vapor outlet a3 to be condensed into hot water;
(2) b, acid production: the crude hydrochloric acid and part of hydrogen chloride tail gas entering the primary washing tower set in the step (1) sequentially enter a washing tower B1 and a washing tower B2 for serial continuous washing to remove sulfuric acid gas, the washing tower B1 and the washing tower B2 can also independently carry out circulating washing through a circulating pipeline B4, when the washing is finished, bottom liquid of the washing tower B1 and the washing tower B2 are semi-finished products of the grade B hydrochloric acid, a small amount of hydrogen chloride gas discharged from a washing outlet B3 of the washing tower B2 enters the primary absorption tower set, the semi-finished products of the grade B hydrochloric acid enter a grade B hydrochloric acid intermediate tank through a grade B hydrochloric acid conveying pipeline, and after the pH value is adjusted to be 6-9, finished products of the grade B hydrochloric acid are obtained and can be sold in a tank;
(3) a, acid production: a small amount of hydrogen chloride gas entering the primary absorption tower group synchronously enters the 3 groups of parallel falling film absorption tower groups, is absorbed by absorption liquid in the primary falling film absorption tower and the secondary falling film absorption tower to obtain an A-grade hydrochloric acid semi-finished product, and a very small amount of hydrogen chloride gas is introduced into the secondary absorption tower group through a secondary absorption pipeline; the absorption liquid is dilute hydrochloric acid, which is supplied by an unsaturated absorption liquid conveying pipeline, and the obtained A-grade hydrochloric acid semi-finished product is introduced into an A-grade hydrochloric acid intermediate tank, and after the pH value is adjusted, the A-grade hydrochloric acid finished product is obtained and can be stored for sale;
(4) production of dilute hydrochloric acid: the method comprises the following steps that a very small amount of hydrogen chloride gas introduced into a secondary absorption tower set is absorbed by absorption liquid, at the moment, the bottom liquid in the secondary absorption tower set is a diluted hydrochloric acid semi-finished product, the diluted hydrochloric acid semi-finished product is introduced into the secondary washing tower set through a first rewashing pipeline and a second rewashing pipeline, the trace hydrogen chloride gas is discharged by the secondary absorption tower set and is separated by a gas-liquid separator and then is introduced into the secondary absorption tower set, wherein the separated trace hydrogen chloride gas firstly converges into a residual gas recovery pipeline, and hydrogen chloride gas possibly remaining in an A-grade hydrochloric acid intermediate tank and a B-grade hydrochloric acid intermediate tank converges into the residual gas recovery pipeline through an exhaust pipe and finally is introduced into a B3 washing tower of the secondary absorption tower set through an HCL fan; after being washed in series by 4 sulphuric acid gas washing towers to obtain dilute hydrochloric acid, then the dilute hydrochloric acid is led into and stored in an acid making bucket, the concentration of the dilute hydrochloric acid in the acid making bucket can be adjusted by adding water or concentrated hydrochloric acid to ensure that the concentration of the dilute hydrochloric acid is between 10 and 31 percent, and then the dilute hydrochloric acid enters an unsaturated absorption liquid conveying pipeline through a lower liquid outlet of the acid making bucket to provide the dilute hydrochloric acid for a primary absorption tower group and a secondary absorption tower group;
(5) cooling water circulation: the first-stage falling film absorption tower is provided with a gas phase outlet c0, which is originated from the exothermic reaction of hydrogen chloride and water, the first-stage falling film absorption tower can accumulate a large amount of water vapor, the water vapor is discharged into a water return hopper through a gas phase outlet c0, and is condensed into hot water together with the water vapor in the step (1), and then the hot water enters a hot water tank, is sent into a water cooling tower through a hot water pump set, is sent into a cold water tank after being cooled, is sent into a cooling water storage tank through a cold water pump set, and provides cooling water for a graphite cooler and the first-stage falling film absorption tower through a water distributor.
The environment-friendly process for purifying the tail gas in potassium sulfate production comprises the step of connecting at least 2 hot water pumps in parallel to form the hot water pump group.
The environment-friendly process for purifying the tail gas in potassium sulfate production comprises the step of connecting at least 2 cold water pumps in parallel to form the cold water pump set.
The environment-friendly process for purifying the tail gas in the potassium sulfate production comprises the step of connecting at least 2 high-level storage tanks in parallel to form the cooling water storage tank.
In the environment-friendly process for purifying the tail gas in the potassium sulfate production, in the primary absorption tower set and the secondary absorption tower set, the process of absorbing the hydrogen chloride gas by the absorption liquid can be independently performed between the primary falling film absorption tower and the secondary falling film absorption tower of the same falling film absorption tower set in a circulating manner, so that the absorption rate of the hydrogen chloride gas is improved.
In the environment-friendly process for purifying the tail gas in the potassium sulfate production, the liquid levels in the sulfuric acid gas washing towers connected through the acid liquid inlet and outlet b2 in the primary washing tower set and the secondary washing tower set are consistent.
The environment-friendly process for purifying the tail gas in the potassium sulfate production process is characterized in that the number of the HCL fans is at least 2, and the HCL fans are connected in parallel.
The environment-friendly process for purifying the tail gas in the potassium sulfate production process is characterized in that overflow pipes are arranged above the high-level storage tank and communicated with the cold water tank.
In the environment-friendly process for purifying the tail gas in the potassium sulfate production, the process water pipeline is separated from the water circulating cooling assembly to provide process water for the No. B6 washing tower, and the process water is purified water or dilute hydrochloric acid.
The environment-friendly process for purifying the tail gas in the potassium sulfate production comprises the steps of arranging hydrochloric acid pumps below the A-level hydrochloric acid intermediate tank and the B-level hydrochloric acid intermediate tank, and communicating the A-level hydrochloric acid storage tank and the B-level hydrochloric acid storage tank through the hydrochloric acid pumps respectively.
The invention has the beneficial effects that:
the invention provides an environment-friendly process for purifying tail gas in potassium sulfate production, which carries out tail gas treatment through tail gas treatment equipment, wherein the tail gas treatment equipment comprises a tail gas conveying pipeline, a graphite cooler, a primary washing tower group, a secondary washing tower group, a primary absorption tower group, a secondary absorption tower group, a gas-liquid separator, an acid making bucket, a hydrochloric acid intermediate tank and a water circulation cooling assembly, and the process flow of the environment-friendly process comprises tail gas cooling, acid B production, acid A production, dilute hydrochloric acid production and cooling water circulation. And meets the environmental protection requirements of energy conservation and emission reduction.
Drawings
FIG. 1 is a schematic view of a tail gas treatment apparatus.
Fig. 2 is a water circulation cooling module.
Fig. 3 is a schematic diagram of the connection of a graphite cooler to a primary scrubber tower set.
FIG. 4 is a schematic diagram of a hydrochloric acid intermediate tank.
Fig. 5 is a schematic view of the connection of the primary absorption tower set and the secondary absorption tower set.
Fig. 6 is a schematic view of a primary absorber tower stack.
Fig. 7 is a schematic view of a secondary absorber tower set.
FIG. 8 is a schematic view showing the connection of the secondary absorption tower set, the gas-liquid separator and the acid making water tank.
Detailed Description
In order to make the technical scheme of the invention clearer and clearer, the invention is further described with reference to the accompanying drawings, and any scheme obtained by carrying out equivalent replacement and conventional reasoning on the technical characteristics of the technical scheme of the invention falls into the protection scope of the invention.
In the water circulation cooling assembly, the water return hopper receives water vapor and condenses the water vapor into hot water, the circulation water tank consists of a hot water tank and a cold water tank, the water return hopper is communicated with the hot water tank and is communicated with a cooling water tower through a hot water pump set, a water outlet of the cooling water tower is communicated with the cold water tank and is communicated with a cooling water storage tank through a cold water pump set, and the cooling water storage tank is communicated with a water distributor and supplies cooling water.
The reference numbers illustrate: 1. a water return hopper; 2. a circulating water tank; 3. a water cooling tower; 4. a hot water pump set; 5. a cold water pump set; 6. a cooling water storage tank; 41. a tail gas conveying pipeline; 45. a hot water tank; 46. a cold water tank; 47. a process water line; 49. a water distributor; 50. a gas-liquid separator; 51. a water barrel for preparing acid; 52. a hydrochloric acid intermediate tank; 53. an A-grade hydrochloric acid intermediate tank; 54. a B-level hydrochloric acid intermediate tank; 55. a hydrochloric acid pump; 56. recooling the pipeline; 57. a B-level hydrochloric acid delivery pipeline; 58. an unsaturated absorption liquid delivery pipe; 59. a secondary absorption conduit; 60. washing the pipeline again; 61. a residual gas recovery pipeline; 62. washing the pipeline again; 63. an exhaust pipe; 64. a HCL fan; 65. a barrel inlet; 66. an upper layer liquid outlet; 67. a lower layer liquid outlet; 68. an overflow pipe; 73. an A-grade hydrochloric acid storage tank; 74. a B-level hydrochloric acid storage tank; 75. a cooling tower; 76. an unsaturated acid pipeline; A. a graphite cooler; B. a sulfuric acid gas washing tower; C. a first-stage falling film absorption tower; D. a secondary falling film absorption tower;
the self-numbering technical scheme is that the noun is as follows: a tail gas inlet a 1; coolant inlet a 2; vapor outlet a 3; cooling outlet a 4; wash inlet b 1; an acid inlet and outlet b 2; a wash outlet b 3; the circulation line b 4; falling film inlet c 1; an absorption liquid inlet c 2; an absorption liquid outlet c 3; an off-gas outlet c 4; a recycle inlet c 5; falling film inlet d 1; an absorption liquid inlet d 2; an absorption liquid outlet d 3; an off-gas outlet d 4; separation inlet e 1; a gas phase outlet e 2; a liquid phase outlet e 3; feed port f 1; a cooling water inlet f 2; a vapor outlet f 3; a discharge port f 4; washing tower No. B1; washing tower No. B2; washing tower No. B3; washing tower No. B4; washing tower No. B5; washing tower No. B6.
Examples
The environment-friendly process for purifying the tail gas generated in the potassium sulfate production is characterized in that the tail gas treatment is carried out by tail gas treatment equipment, and the process flow of the environment-friendly process comprises tail gas cooling, acid B production, acid A production, dilute hydrochloric acid production and cooling water circulation.
The tail gas treatment equipment comprises a tail gas conveying pipeline, a graphite cooler, a primary washing tower group, a secondary washing tower group, a primary absorption tower group, a secondary absorption tower group, a gas-liquid separator, an acid making water bucket, a hydrochloric acid intermediate tank and a water circulating cooling assembly, wherein the primary washing tower group is formed by connecting 2 sulfuric acid gas washing towers in series, the secondary washing tower group is formed by connecting 4 sulfuric acid gas washing towers in series, the primary absorption tower group is formed by connecting 3 falling film absorption tower groups, the secondary absorption tower group is formed by connecting 2 falling film absorption tower groups, the hydrochloric acid intermediate tank comprises an A-level hydrochloric acid intermediate tank and a B-level hydrochloric acid intermediate tank, and the water circulating cooling assembly comprises a water return bucket, a circulating water tank, a hot water pump group, a water cooling tower, a cold water pump group, a cooling water storage tank and a water distributor;
the tail gas conveying pipeline is communicated with the Mannheim reaction furnace and receives tail gas discharged by the Mannheim reaction furnace, the graphite cooler comprises a tail gas inlet a1, a cooling liquid inlet a2, a steam outlet a3 and a cooling outlet a4, the tail gas inlet a1 is communicated with the tail gas conveying pipeline and receives the tail gas, the cooling liquid inlet a2 is communicated with the water distributor, the steam outlet a3 is communicated with the water return hopper, and the cooling outlet a4 is communicated with the primary washing tower group;
the sulfuric acid gas washing tower comprises a washing inlet B1, an acid liquid inlet and outlet B2, a washing outlet B3 and a circulating pipeline B4, the sulfuric acid gas washing tower in a primary washing tower group is divided into a washing tower number B1 and a washing tower number B2 according to the front and back positions, the washing inlet B1 of the washing tower number B1 is communicated with a cooling outlet a4 of a graphite cooler, an acid liquid inlet and outlet B2 of the washing tower number B1 is communicated with an acid liquid inlet and outlet B2 of the washing tower number B2, a washing outlet B3 of the washing tower number B1 is communicated with a washing inlet B1 of the washing tower number B2, and two ends of the circulating pipeline B4 are respectively communicated with the top and the tail of the sulfuric acid gas washing tower, and is provided with a hydrochloric acid pump, a secondary cooling pipeline is connected on a circulating pipeline B4 of the No. B1 washing tower, a B-level hydrochloric acid conveying pipeline is connected on a circulating pipeline B4 of the No. B2 washing tower, the secondary cooling pipeline is communicated with a graphite cooler, and the B-level hydrochloric acid conveying pipeline is communicated with a B-level hydrochloric acid intermediate tank;
the 3 groups of falling film absorption tower groups forming the primary absorption tower group are sequentially connected in parallel, the 2 groups of falling film absorption tower groups forming the secondary absorption tower group are sequentially connected in parallel, and the falling film absorption tower group is formed by connecting 1 primary falling film absorption tower and 1 secondary falling film absorption tower in series;
in the primary absorption tower group, the primary falling film absorption tower comprises a falling film inlet c1, an absorption liquid inlet c2, an absorption liquid outlet c3, a tail gas outlet c4 and a circulating inlet c5, the secondary falling film absorption tower comprises a falling film inlet d1, an absorption liquid inlet d2, an absorption liquid outlet d3 and a tail gas outlet d4, the falling film inlet c1 of the primary falling film absorption tower is communicated with a washing outlet B3 of a No. B2 washing tower through a pipeline, the absorption liquid inlet c2 is communicated with a water distributor, the absorption liquid outlet c3 is communicated with an A-level hydrochloric acid intermediate tank, the tail gas outlet c4 is communicated with the falling film inlet d1 of the secondary falling film absorption tower, the absorption liquid inlet d2 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet d3 is communicated with a circulating inlet c5, and the tail gas outlet d4 is communicated with a secondary absorption pipeline;
in the secondary absorption tower group, the primary falling film absorption tower comprises a falling film inlet c6, an absorption liquid inlet c7, an absorption liquid outlet c8, a tail gas outlet c9 and a circulating inlet c10, the secondary falling film absorption tower comprises a falling film inlet d6, an absorption liquid inlet d7, an absorption liquid outlet d8 and a tail gas outlet d9, the falling film inlet c6 of the primary falling film absorption tower is communicated with a secondary absorption pipeline, the absorption liquid inlet c7 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet c8 is communicated with a rewashing pipeline, the tail gas outlet c9 is communicated with a falling film inlet d6 of the secondary falling film absorption tower, the absorption liquid inlet d7 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet d8 is communicated with a circulating inlet c10, and the tail gas outlet d9 is communicated with a gas-liquid separator;
the gas-liquid separator comprises a separation inlet e1, a gas-phase outlet e2 and a liquid-phase outlet e3, the separation inlet e1 is communicated with a tail gas outlet d9 through a pipeline, the gas-phase outlet e2 is communicated with a residual gas recovery pipeline, the liquid-phase outlet e3 is communicated with a second rewashing pipeline, exhaust pipes are arranged at the tops of the A-level hydrochloric acid intermediate tank and the B-level hydrochloric acid intermediate tank and are communicated with the residual gas recovery pipeline, and an HCL fan is arranged on the residual gas recovery pipeline;
the sulfuric acid gas washing tower in the secondary washing tower group is divided into a washing tower No. B3, a washing tower No. B4, a washing tower No. B5 and a washing tower No. B6 according to the front and back positions, in the secondary absorption tower group, an absorption liquid outlet c8 of a first-level falling film absorption tower on 2 groups of falling film absorption tower groups is respectively communicated with washing inlets B1 of the washing tower No. B4 and the washing tower No. B3 through a first rewashing pipeline, a gas phase outlet e2 of an exhaust pipe and a gas-liquid separator is communicated with a washing inlet B1 of the washing tower No. B3 through a residual gas recovery pipeline, a liquid phase outlet e3 of the gas-liquid separator is communicated with a washing inlet B6865 of the washing tower No. B3 through a second rewashing pipeline, a washing inlet B1 of the washing tower No. B6 is communicated with a process water pipeline, a washing outlet B3 of the washing tower No. B3 is communicated with a washing inlet B1 of the washing tower No. B4, a washing outlet B828653 of the washing tower is communicated with a washing tower No. B828653, a washing outlet B3 of the No. B5 washing tower is communicated with a washing inlet B1 of the No. B6 washing tower, and acid liquor inlets and outlets B2 of the adjacent 2 washing towers are communicated with each other;
in the secondary washing tower group, the circulating pipelines B4 of the washing tower No. B3, the washing tower No. B4, the washing tower No. B5 and the washing tower No. B6 are connected with unsaturated acid liquid pipelines, the acid making water barrel comprises a barrel inlet, an upper layer liquid outlet and a lower layer liquid outlet, the barrel inlet is communicated with an unsaturated acid liquid pipeline, the upper layer liquid outlet is communicated with a washing inlet B1 of a No. B3 washing tower through a pipeline, the lower layer liquid outlet is communicated with a cooling tower, the cooling tower comprises a feed port f1, a cooling water inlet f2, a steam outlet f3 and a discharge port f4, the feed port f1 is communicated with a lower liquid outlet, the cooling water inlet f2 is communicated with a water distributor, the steam outlet f3 is communicated with a water return hopper, the discharge port f4 is communicated with an unsaturated absorption liquid conveying pipeline, and the absorption liquid inlet d2 of the secondary falling film absorption tower in the primary absorption tower group and the secondary absorption tower group is communicated through a plurality of conveying branch pipes;
in the water circulation cooling assembly, the water return hopper receives water vapor and condenses the water vapor into hot water, the circulation water tank consists of a hot water tank and a cold water tank, the water return hopper is communicated with the hot water tank and is communicated with a cooling water tower through a hot water pump set, a water outlet of the cooling water tower is communicated with the cold water tank and is communicated with a cooling water storage tank through a cold water pump set, and the cooling water storage tank is communicated with a water distributor and supplies cooling water.
The environment-friendly process for purifying the tail gas generated in the production of potassium sulfate comprises the following specific processes:
(1) cooling tail gas: hydrogen chloride tail gas discharged by a Mannheim reaction furnace enters a graphite cooler through a tail gas conveying pipeline and a tail gas inlet a1 for cooling, cooling water is supplied by a water circulation cooling assembly, and enters the graphite cooler through a water distributor and a cooling liquid inlet a2, hydrogen chloride tail gas is dissolved into the cooling water and generates a large amount of heat to generate crude hydrochloric acid and generate a large amount of water vapor, the crude hydrochloric acid and part of hydrogen chloride tail gas which is not dissolved in water enter a primary washing tower group through a cooling outlet a4, and the water vapor enters a water return hopper through a vapor outlet a3 to be condensed into hot water;
(2) b, acid production: the crude hydrochloric acid and part of hydrogen chloride tail gas entering the primary washing tower set in the step (1) sequentially enter a washing tower B1 and a washing tower B2 for serial continuous washing to remove sulfuric acid gas, the washing tower B1 and the washing tower B2 can also independently carry out circulating washing through a circulating pipeline B4, when the washing is finished, bottom liquid of the washing tower B1 and the washing tower B2 are semi-finished products of the grade B hydrochloric acid, a small amount of hydrogen chloride gas discharged from a washing outlet B3 of the washing tower B2 enters the primary absorption tower set, the semi-finished products of the grade B hydrochloric acid enter a grade B hydrochloric acid intermediate tank through a grade B hydrochloric acid conveying pipeline, and after the pH value is adjusted to be 6-9, finished products of the grade B hydrochloric acid are obtained and can be sold in a tank;
(3) a, acid production: a small amount of hydrogen chloride gas entering the primary absorption tower group synchronously enters the 3 groups of parallel falling film absorption tower groups, is absorbed by absorption liquid in the primary falling film absorption tower and the secondary falling film absorption tower to obtain an A-grade hydrochloric acid semi-finished product, and a very small amount of hydrogen chloride gas is introduced into the secondary absorption tower group through a secondary absorption pipeline; the absorption liquid is dilute hydrochloric acid, which is supplied by an unsaturated absorption liquid conveying pipeline, and the obtained A-grade hydrochloric acid semi-finished product is introduced into an A-grade hydrochloric acid intermediate tank, and after the pH value is adjusted, the A-grade hydrochloric acid finished product is obtained and can be stored for sale;
(4) production of dilute hydrochloric acid: the method comprises the following steps that a very small amount of hydrogen chloride gas introduced into a secondary absorption tower set is absorbed by absorption liquid, at the moment, the bottom liquid in the secondary absorption tower set is a diluted hydrochloric acid semi-finished product, the diluted hydrochloric acid semi-finished product is introduced into the secondary washing tower set through a first rewashing pipeline and a second rewashing pipeline, the trace hydrogen chloride gas is discharged by the secondary absorption tower set and is separated by a gas-liquid separator and then is introduced into the secondary absorption tower set, wherein the separated trace hydrogen chloride gas firstly converges into a residual gas recovery pipeline, and hydrogen chloride gas possibly remaining in an A-grade hydrochloric acid intermediate tank and a B-grade hydrochloric acid intermediate tank converges into the residual gas recovery pipeline through an exhaust pipe and finally is introduced into a B3 washing tower of the secondary absorption tower set through an HCL fan; after being washed in series by 4 sulphuric acid gas washing towers to obtain dilute hydrochloric acid, then the dilute hydrochloric acid is led into and stored in an acid making bucket, the concentration of the dilute hydrochloric acid in the acid making bucket can be adjusted by adding water or concentrated hydrochloric acid to ensure that the concentration of the dilute hydrochloric acid is between 10 and 31 percent, and then the dilute hydrochloric acid enters an unsaturated absorption liquid conveying pipeline through a lower liquid outlet of the acid making bucket to provide the dilute hydrochloric acid for a primary absorption tower group and a secondary absorption tower group;
(5) cooling water circulation: the first-stage falling film absorption tower is provided with a gas phase outlet c0, which is originated from the exothermic reaction of hydrogen chloride and water, the first-stage falling film absorption tower can accumulate a large amount of water vapor, the water vapor is discharged into a water return hopper through a gas phase outlet c0, and is condensed into hot water together with the water vapor in the step (1), and then the hot water enters a hot water tank, is sent into a water cooling tower through a hot water pump set, is sent into a cold water tank after being cooled, is sent into a cooling water storage tank through a cold water pump set, and provides cooling water for a graphite cooler and the first-stage falling film absorption tower through a water distributor.
The system comprises a hot water pump set, a cold water pump set and a cooling water storage tank, wherein the hot water pump set is formed by connecting at least 2 hot water pumps in parallel, the cold water pump set is formed by connecting at least 2 cold water pumps in parallel, and the cooling water storage tank is formed by connecting at least 2 high-level storage tanks in parallel;
in the primary absorption tower group and the secondary absorption tower group, the process of absorbing the hydrogen chloride gas by the absorption liquid can be independently carried out between the primary falling film absorption tower and the secondary falling film absorption tower of the same falling film absorption tower group in a circulating manner, so that the absorption rate of the hydrogen chloride gas is improved;
in the primary washing tower group and the secondary washing tower group, the liquid levels of the bottom liquid in the sulfuric acid gas washing tower connected through an acid liquid inlet and outlet b2 are consistent;
the number of the HCL fans is at least 2, the HCL fans are connected in parallel, overflow pipes are arranged above the high-level storage tank, and the overflow pipes are communicated with the cold water tank;
the process water pipeline is separated from the water circulating cooling assembly to provide process water for a No. B6 washing tower, the process water is purified water or dilute hydrochloric acid, hydrochloric acid pumps are arranged below the A-level hydrochloric acid intermediate tank and the B-level hydrochloric acid intermediate tank and are respectively communicated with the A-level hydrochloric acid storage tank and the B-level hydrochloric acid storage tank through the hydrochloric acid pumps.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are also included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (6)
1. An environment-friendly process for purifying tail gas generated in potassium sulfate production is characterized in that tail gas treatment is carried out by tail gas treatment equipment, and the process flow of the environment-friendly process comprises tail gas cooling, acid B production, acid A production, dilute hydrochloric acid production and cooling water circulation;
the tail gas treatment equipment comprises a tail gas conveying pipeline, a graphite cooler, a primary washing tower set, a secondary washing tower set, a primary absorption tower set, a secondary absorption tower set, a gas-liquid separator, an acid making water bucket, a hydrochloric acid intermediate tank and a water circulating cooling assembly, wherein the primary washing tower set is formed by connecting 2 sulfuric acid gas washing towers in series, the secondary washing tower set is formed by connecting 4 sulfuric acid gas washing towers in series, the primary absorption tower set is formed by connecting 3 falling film absorption tower sets, the secondary absorption tower set is formed by connecting 2 falling film absorption tower sets, the hydrochloric acid intermediate tank comprises an A-level hydrochloric acid intermediate tank and a B-level hydrochloric acid intermediate tank, and the water circulating cooling assembly comprises a water return bucket, a circulating water tank, a hot water pump set, a cooling water tower, a cold water pump set, a cooling water storage tank and a water distributor;
the tail gas conveying pipeline is communicated with the Mannheim reaction furnace and receives tail gas discharged by the Mannheim reaction furnace, the graphite cooler comprises a tail gas inlet a1, a cooling liquid inlet a2, a steam outlet a3 and a cooling outlet a4, the tail gas inlet a1 is communicated with the tail gas conveying pipeline and receives the tail gas, the cooling liquid inlet a2 is communicated with the water distributor, the steam outlet a3 is communicated with the water return hopper, and the cooling outlet a4 is communicated with the primary washing tower group;
the sulfuric acid gas washing tower comprises a washing inlet B1, an acid liquid inlet and outlet B2, a washing outlet B3 and a circulating pipeline B4, the sulfuric acid gas washing tower in a primary washing tower group is divided into a washing tower number B1 and a washing tower number B2 according to the front and back positions, the washing inlet B1 of the washing tower number B1 is communicated with a cooling outlet a4 of a graphite cooler, an acid liquid inlet and outlet B2 of the washing tower number B1 is communicated with an acid liquid inlet and outlet B2 of the washing tower number B2, a washing outlet B3 of the washing tower number B1 is communicated with a washing inlet B1 of the washing tower number B2, and two ends of the circulating pipeline B4 are respectively communicated with the top and the tail of the sulfuric acid gas washing tower, and is provided with a hydrochloric acid pump, a secondary cooling pipeline is connected on a circulating pipeline B4 of the No. B1 washing tower, a B-level hydrochloric acid conveying pipeline is connected on a circulating pipeline B4 of the No. B2 washing tower, the secondary cooling pipeline is communicated with a graphite cooler, and the B-level hydrochloric acid conveying pipeline is communicated with a B-level hydrochloric acid intermediate tank;
the 3 groups of falling film absorption tower groups forming the primary absorption tower group are sequentially connected in parallel, the 2 groups of falling film absorption tower groups forming the secondary absorption tower group are sequentially connected in parallel, and the falling film absorption tower group is formed by connecting 1 primary falling film absorption tower and 1 secondary falling film absorption tower in series;
in the primary absorption tower group, the primary falling film absorption tower comprises a falling film inlet c1, an absorption liquid inlet c2, an absorption liquid outlet c3, a tail gas outlet c4 and a circulating inlet c5, the secondary falling film absorption tower comprises a falling film inlet d1, an absorption liquid inlet d2, an absorption liquid outlet d3 and a tail gas outlet d4, the falling film inlet c1 of the primary falling film absorption tower is communicated with a washing outlet B3 of a No. B2 washing tower through a pipeline, the absorption liquid inlet c2 is communicated with a water distributor, the absorption liquid outlet c3 is communicated with an A-level hydrochloric acid intermediate tank, the tail gas outlet c4 is communicated with the falling film inlet d1 of the secondary falling film absorption tower, the absorption liquid inlet d2 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet d3 is communicated with a circulating inlet c5, and the tail gas outlet d4 is communicated with a secondary absorption pipeline;
in the secondary absorption tower group, the primary falling film absorption tower comprises a falling film inlet c6, an absorption liquid inlet c7, an absorption liquid outlet c8, a tail gas outlet c9 and a circulating inlet c10, the secondary falling film absorption tower comprises a falling film inlet d6, an absorption liquid inlet d7, an absorption liquid outlet d8 and a tail gas outlet d9, the falling film inlet c6 of the primary falling film absorption tower is communicated with a secondary absorption pipeline, the absorption liquid inlet c7 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet c8 is communicated with a rewashing pipeline, the tail gas outlet c9 is communicated with a falling film inlet d6 of the secondary falling film absorption tower, the absorption liquid inlet d7 is communicated with an unsaturated absorption liquid conveying pipeline, the absorption liquid outlet d8 is communicated with a circulating inlet c10, and the tail gas outlet d9 is communicated with a gas-liquid separator;
the gas-liquid separator comprises a separation inlet e1, a gas-phase outlet e2 and a liquid-phase outlet e3, the separation inlet e1 is communicated with a tail gas outlet d9 through a pipeline, the gas-phase outlet e2 is communicated with a residual gas recovery pipeline, the liquid-phase outlet e3 is communicated with a second rewashing pipeline, exhaust pipes are arranged at the tops of the A-level hydrochloric acid intermediate tank and the B-level hydrochloric acid intermediate tank and are communicated with the residual gas recovery pipeline, and an HCL fan is arranged on the residual gas recovery pipeline;
the sulfuric acid gas washing tower in the secondary washing tower group is divided into a washing tower No. B3, a washing tower No. B4, a washing tower No. B5 and a washing tower No. B6 according to the front and back positions, in the secondary absorption tower group, an absorption liquid outlet c8 of a first-level falling film absorption tower on 2 groups of falling film absorption tower groups is respectively communicated with washing inlets B1 of the washing tower No. B4 and the washing tower No. B3 through a first rewashing pipeline, a gas phase outlet e2 of an exhaust pipe and a gas-liquid separator is communicated with a washing inlet B1 of the washing tower No. B3 through a residual gas recovery pipeline, a liquid phase outlet e3 of the gas-liquid separator is communicated with a washing inlet B6865 of the washing tower No. B3 through a second rewashing pipeline, a washing inlet B1 of the washing tower No. B6 is communicated with a process water pipeline, a washing outlet B3 of the washing tower No. B3 is communicated with a washing inlet B1 of the washing tower No. B4, a washing outlet B828653 of the washing tower is communicated with a washing tower No. B828653, a washing outlet B3 of the No. B5 washing tower is communicated with a washing inlet B1 of the No. B6 washing tower, and acid liquor inlets and outlets B2 of the adjacent 2 washing towers are communicated with each other;
in the secondary washing tower group, the circulating pipelines B4 of the washing tower No. B3, the washing tower No. B4, the washing tower No. B5 and the washing tower No. B6 are connected with unsaturated acid liquid pipelines, the acid making water barrel comprises a barrel inlet, an upper layer liquid outlet and a lower layer liquid outlet, the barrel inlet is communicated with an unsaturated acid liquid pipeline, the upper layer liquid outlet is communicated with a washing inlet B1 of a No. B3 washing tower through a pipeline, the lower layer liquid outlet is communicated with a cooling tower, the cooling tower comprises a feed port f1, a cooling water inlet f2, a steam outlet f3 and a discharge port f4, the feed port f1 is communicated with a lower liquid outlet, the cooling water inlet f2 is communicated with a water distributor, the steam outlet f3 is communicated with a water return hopper, the discharge port f4 is communicated with an unsaturated absorption liquid conveying pipeline, and the absorption liquid inlet d2 of the secondary falling film absorption tower in the primary absorption tower group and the secondary absorption tower group is communicated through a plurality of conveying branch pipes;
in the water circulation cooling assembly, the water return hopper receives water vapor and condenses the water vapor into hot water, the circulation water tank consists of a hot water tank and a cold water tank, the water return hopper is communicated with the hot water tank and is communicated with a cooling water tower through a hot water pump set, a water outlet of the cooling water tower is communicated with the cold water tank and is communicated with a cooling water storage tank through a cold water pump set, and the cooling water storage tank is communicated with a water distributor and supplies cooling water;
the environment-friendly process for treating the tail gas by using the tail gas treatment equipment comprises the following specific process steps:
(1) cooling tail gas: hydrogen chloride tail gas discharged by a Mannheim reaction furnace enters a graphite cooler through a tail gas conveying pipeline and a tail gas inlet a1 for cooling, cooling water is supplied by a water circulation cooling assembly, and enters the graphite cooler through a water distributor and a cooling liquid inlet a2, hydrogen chloride tail gas is dissolved into the cooling water and generates a large amount of heat to generate crude hydrochloric acid and generate a large amount of water vapor, the crude hydrochloric acid and part of hydrogen chloride tail gas which is not dissolved in water enter a primary washing tower group through a cooling outlet a4, and the water vapor enters a water return hopper through a vapor outlet a3 to be condensed into hot water;
(2) b, acid production: the crude hydrochloric acid and part of hydrogen chloride tail gas entering the primary washing tower set in the step (1) sequentially enter a washing tower B1 and a washing tower B2 for serial continuous washing to remove sulfuric acid gas, the washing tower B1 and the washing tower B2 can also independently carry out circulating washing through a circulating pipeline B4, when the washing is finished, bottom liquid of the washing tower B1 and the washing tower B2 are semi-finished products of the grade B hydrochloric acid, a small amount of hydrogen chloride gas discharged from a washing outlet B3 of the washing tower B2 enters the primary absorption tower set, the semi-finished products of the grade B hydrochloric acid enter a grade B hydrochloric acid intermediate tank through a grade B hydrochloric acid conveying pipeline, and after the pH value is adjusted to be 6-9, finished products of the grade B hydrochloric acid are obtained and can be sold in a tank;
(3) a, acid production: a small amount of hydrogen chloride gas entering the primary absorption tower group synchronously enters the 3 groups of parallel falling film absorption tower groups, is absorbed by absorption liquid in the primary falling film absorption tower and the secondary falling film absorption tower to obtain an A-grade hydrochloric acid semi-finished product, and a very small amount of hydrogen chloride gas is introduced into the secondary absorption tower group through a secondary absorption pipeline; the absorption liquid is dilute hydrochloric acid, which is supplied by an unsaturated absorption liquid conveying pipeline, and the obtained A-grade hydrochloric acid semi-finished product is introduced into an A-grade hydrochloric acid intermediate tank, and after the pH value is adjusted, the A-grade hydrochloric acid finished product is obtained and can be stored for sale;
(4) production of dilute hydrochloric acid: the method comprises the following steps that a very small amount of hydrogen chloride gas introduced into a secondary absorption tower set is absorbed by absorption liquid, at the moment, the bottom liquid in the secondary absorption tower set is a diluted hydrochloric acid semi-finished product, the diluted hydrochloric acid semi-finished product is introduced into the secondary washing tower set through a first rewashing pipeline and a second rewashing pipeline, the trace hydrogen chloride gas is discharged by the secondary absorption tower set and is separated by a gas-liquid separator and then is introduced into the secondary absorption tower set, wherein the separated trace hydrogen chloride gas firstly converges into a residual gas recovery pipeline, and hydrogen chloride gas possibly remaining in an A-grade hydrochloric acid intermediate tank and a B-grade hydrochloric acid intermediate tank converges into the residual gas recovery pipeline through an exhaust pipe and finally is introduced into a B3 washing tower of the secondary absorption tower set through an HCL fan; after being washed in series by 4 sulphuric acid gas washing towers to obtain dilute hydrochloric acid, then the dilute hydrochloric acid is led into and stored in an acid making bucket, the concentration of the dilute hydrochloric acid in the acid making bucket can be adjusted by adding water or concentrated hydrochloric acid to ensure that the concentration of the dilute hydrochloric acid is between 10 and 31 percent, and then the dilute hydrochloric acid enters an unsaturated absorption liquid conveying pipeline through a lower liquid outlet of the acid making bucket to provide the dilute hydrochloric acid for a primary absorption tower group and a secondary absorption tower group;
(5) cooling water circulation: the first-stage falling film absorption tower is provided with a gas phase outlet c0, which is originated from the exothermic reaction of hydrogen chloride and water, the first-stage falling film absorption tower can accumulate a large amount of water vapor, the water vapor is discharged into a water return hopper through a gas phase outlet c0, and is condensed into hot water together with the water vapor in the step (1), and then the hot water enters a hot water tank, is sent into a water cooling tower through a hot water pump set, is sent into a cold water tank after being cooled, is sent into a cooling water storage tank through a cold water pump set, and provides cooling water for a graphite cooler and the first-stage falling film absorption tower through a water distributor.
2. The environment-friendly process for purifying tail gas in potassium sulfate production according to claim 1, wherein the hot water pump group is formed by connecting at least 2 hot water pumps in parallel, the cold water pump group is formed by connecting at least 2 cold water pumps in parallel, and the cooling water storage tank is formed by connecting at least 2 high-level storage tanks in parallel.
3. The environment-friendly process for purifying tail gas in potassium sulfate production as claimed in claim 2, wherein in the primary absorption tower set and the secondary absorption tower set, the process of absorbing hydrogen chloride gas by absorption liquid can be independently performed in a circulating manner between the primary falling film absorption tower and the secondary falling film absorption tower of the same falling film absorption tower set, so as to improve the absorption rate of hydrogen chloride gas.
4. The environment-friendly process for purifying tail gas in potassium sulfate production as claimed in claim 3, wherein the primary scrubber group and the secondary scrubber group have the same bottom liquid level in the sulfuric acid gas scrubber connected through the acid liquid inlet and outlet b 2.
5. The environment-friendly process for purifying tail gas in potassium sulfate production according to claim 3, wherein the number of the HCL fans is at least 2, the HCL fans are connected in parallel, overflow pipes are arranged above the high-level storage tanks, and the overflow pipes are communicated with the cold water tank.
6. The environment-friendly process for purifying tail gas in potassium sulfate production as claimed in claim 3, wherein the process water pipeline is separated from the water circulation cooling assembly to provide process water for a No. B6 washing tower, the process water is purified water, hydrochloric acid pumps are arranged below the A-grade hydrochloric acid intermediate tank and the B-grade hydrochloric acid intermediate tank, and the A-grade hydrochloric acid storage tank and the B-grade hydrochloric acid storage tank are respectively communicated through the hydrochloric acid pumps.
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| CN113213426A (en) * | 2021-03-03 | 2021-08-06 | 眉山友禾科技有限公司 | Preparation process of high-concentration hydrochloric acid |
| CN113620249B (en) * | 2021-08-04 | 2023-02-28 | 河北卓泰肥业有限公司 | Method and system for producing reagent hydrochloric acid by using Mannheim furnace tail gas |
| CN113666338B (en) * | 2021-09-14 | 2022-10-28 | 齐齐哈尔市茂尔农业有限公司 | Production device, heat dissipation mechanism and process flow of potassium sulfate byproduct hydrochloric acid by Mannheim method |
| CN114288841A (en) * | 2021-12-31 | 2022-04-08 | 山东三方化工集团有限公司 | Mannheim method potassium sulfate tail gas processing system |
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