CN114455558B - Deep arsenic removal system for arsenic-containing phosphoric acid - Google Patents
Deep arsenic removal system for arsenic-containing phosphoric acid Download PDFInfo
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- CN114455558B CN114455558B CN202210277478.3A CN202210277478A CN114455558B CN 114455558 B CN114455558 B CN 114455558B CN 202210277478 A CN202210277478 A CN 202210277478A CN 114455558 B CN114455558 B CN 114455558B
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- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 72
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 229910000147 aluminium phosphate Inorganic materials 0.000 title claims abstract description 48
- 238000006243 chemical reaction Methods 0.000 claims abstract description 74
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 30
- 238000005406 washing Methods 0.000 claims abstract description 28
- 230000001105 regulatory effect Effects 0.000 claims abstract description 20
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 239000007921 spray Substances 0.000 claims abstract description 4
- 238000005507 spraying Methods 0.000 claims description 16
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 13
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- 239000000376 reactant Substances 0.000 claims description 7
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 7
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 7
- CYQAYERJWZKYML-UHFFFAOYSA-N phosphorus pentasulfide Chemical compound S1P(S2)(=S)SP3(=S)SP1(=S)SP2(=S)S3 CYQAYERJWZKYML-UHFFFAOYSA-N 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 4
- 230000014759 maintenance of location Effects 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 238000005728 strengthening Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 11
- 239000000126 substance Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000011031 large-scale manufacturing process Methods 0.000 abstract description 3
- 239000003513 alkali Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 3
- 238000009388 chemical precipitation Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 229910052958 orpiment Inorganic materials 0.000 description 2
- 238000000053 physical method Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 229940127557 pharmaceutical product Drugs 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 231100000167 toxic agent Toxicity 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/18—Phosphoric acid
- C01B25/234—Purification; Stabilisation; Concentration
- C01B25/237—Selective elimination of impurities
- C01B25/238—Cationic impurities, e.g. arsenic compounds
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Removal Of Specific Substances (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention belongs to the technical field of efficient mixing and reaction of chemical industry, and particularly relates to a deep arsenic removal system for arsenic-containing phosphoric acid, which comprises an arsenic removal agent configuration tank, a primary reactor, an arsenic removal reaction tank and a washing tower; the top inlet of the dearsenization agent configuration groove is communicated with a dearsenization agent feeding pipe, the bottom outlet of the dearsenization agent configuration groove is communicated with a liquid inlet pipe of the primary reactor through a conveying pump and a first flow regulating valve pipeline, the upper side inlet of the primary reactor is communicated with an arsenic-containing phosphoric acid feeding pipe through a second flow regulating valve pipeline, the bottom outlet pipeline of the primary reactor is communicated with the top side inlet of the dearsenization reaction groove, the top side inlet of the dearsenization reaction groove is communicated with the lower part of the washing tower through a pipeline, one pipeline of the outlet of the washing tower is communicated with an upper spray pipe of the washing tower, and the other pipeline is communicated with the top of the dearsenization agent configuration groove; therefore, the invention has the unique advantages of low energy consumption, high efficiency, high reaction reliability and safety, controllable process and the like, and is suitable for large-scale production and popularization and application.
Description
Technical Field
The invention belongs to the technical field of efficient chemical mixing and reaction, and particularly relates to a deep arsenic removal system for arsenic-containing phosphoric acid.
Background
Arsenic is a toxic substance and causes great harm to human and animals. During phosphoric acid production, arsenic will dissolve in phosphoric acid, and either fertilizer, technical grade phosphoric acid or food grade phosphoric acid will be carried into the product and have a large impact on the quality of the subsequent phosphate product and be one of the more difficult impurities to remove. Particularly in the application of phosphoric acid to food grade additives and pharmaceutical products, arsenic content is particularly severely controlled.
As with other metal impurities, arsenic removal methods can be broadly divided into two categories, chemical precipitation and physical methods. The chemical method includes traditional coagulating sedimentation method and sulfide sedimentation method, while the physical method includes solvent extraction method, ion exchange method and crystallization method, etc., and in actual industrial production, chemical sedimentation method is mainly used for dearsenifying.
At present, the chemical precipitation method mainly comprises the steps of generating sodium sulfide solution and reacting with phosphoric acid to generate hydrogen sulfide gas, and sending the hydrogen sulfide gas into a two-stage arsenic removal tower under pressure to contact with phosphoric acid overflow for reaction, wherein the arsenic content in phosphoric acid after reaction can be as low as 0.5ppm. However, the dearsenifying tower has large volume, high investment, low mass transfer efficiency, poor controllability of the reaction process and larger potential safety hazard in actual production, so that a deep dearsenifying technology with high efficiency, low cost, safety and strong applicability needs to be developed.
Disclosure of Invention
The invention aims to solve the technical problems and provide a deep arsenic removal system for arsenic-containing phosphoric acid, which has high arsenic removal efficiency and strong applicability,
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
an arsenic-containing phosphoric acid deep arsenic removal system comprises an arsenic removal agent configuration tank 10, a primary reactor 30, an arsenic removal reaction tank 40 and a washing tower 50;
The top inlet of the dearsenifying agent configuration tank 10 is connected with a dearsenifying agent feeding pipe, the bottom outlet of the dearsenifying agent configuration tank 10 is communicated with a liquid inlet pipe 31 of the primary reactor 30 through a conveying pump 20 and a first flow regulating valve 80 pipeline, the upper side inlet of the primary reactor 30 is communicated with an arsenic-containing phosphoric acid feeding pipe through a second flow regulating valve 70 pipeline, the bottom outlet of the primary reactor 30 is communicated with the top side inlet of the dearsenifying reaction tank 40 through a pipeline, the top side inlet of the dearsenifying reaction tank 40 is communicated with the lower part of the washing tower 50 through a pipeline, the bottom of the washing tower 50 is divided into two paths through a washing tower circulating pump 60, one path is communicated with an upper spray pipe of the washing tower 50 through a pipeline, and the other path is communicated with the top of the dearsenifying agent configuration tank 10 through a pipeline;
stirring paddles are arranged in the dearsenifying agent preparation tank 10 and the dearsenifying reaction tank 40,
The top of the dearsenification reaction tank 40 is connected with an air cone (100) through a flange in a sealing way, an inlet at one side of the air cone 100 is communicated with a compressed air pipeline, and an outlet at the other side of the air cone 100 is communicated with the lower part of the washing tower 50 through a pressure regulating valve 90 pipeline;
The primary reactor 30 is a pipeline mixer, the upper part of the pipeline mixer is coaxially inserted with a liquid inlet pipe 31, spraying holes are uniformly formed in the axial direction of the liquid inlet pipe 31, more than 5 layers of baffle plates 32 are arranged on the lower part of the pipeline mixer, holes which are arranged in a triangular mode are formed in each baffle plate 32, and the holes in adjacent baffle plates 32 are arranged in a staggered mode.
When the system is in operation, the mass ratio of the arsenic-containing phosphoric acid to the dearsenifying agent is 100: 1-500:1, introducing into a primary reactor 30, wherein the arsenic-containing phosphoric acid is agricultural grade or above, the mass concentration of the phosphoric acid is 30% -64%, and the arsenic content is more than or equal to 1ppm;
Mixing and reacting in the primary reactor 30 to obtain a primary reactant, wherein the reaction temperature of the primary reactor 30 is 60-90 ℃ and the reaction pressure is 0.3-0.6 MPa;
The primary reactant is introduced into the dearsenification reaction tank 40 for strengthening reaction and gas-liquid separation, so as to obtain hydrogen sulfide gas and dearsenification phosphoric acid, wherein the arsenic content of the dearsenification phosphoric acid is less than or equal to 0.5ppm, the material retention time in the dearsenification reaction tank 40 is 3-5 min, the reaction temperature is 60-90 ℃, and the reaction pressure is 0.05-0.4 MPa.
Further, the dearsenization agent is one of sodium sulfide or phosphorus pentasulfide, wherein the mass concentration of the sodium sulfide or the phosphorus pentasulfide is 5% -20%.
Further, when the pipeline pressure measured by the pressure regulating valve 90 is less than or equal to 0.2MPa, the pressure regulating valve 90 is closed in a linkage manner, and compressed air is introduced into the dearsenification reaction tank 40 through a compressed air pipeline, so that the pressure of the air cone 100 at the top of the dearsenification reaction tank 40 is 0.5-0.8 MPa, and the pressure in the dearsenification reaction tank 40 is 0.05-0.4 MPa.
Further, the pipe diameter of the primary reactor 30 is 50 mm-350 mm, the length is 1000-5000 mm, 5 layers of baffle plates 32 are arranged at the lower part of the primary reactor 30, the distance between adjacent baffle plates 32 is 100-500 mm, and the aperture of an opening hole on each baffle plate 32 is 10-30 mm.
Further, the pipe diameter of the liquid inlet pipe 31 is 15 mm-60 mm, the length is 100-2000 mm, more than 5 layers of spraying holes are formed in the liquid inlet pipe 31, the distance between the spraying holes of adjacent layers is 50-200 mm, and each layer of spraying holes comprises 4 spraying holes uniformly distributed along the axial direction of the liquid inlet pipe 31.
The beneficial effects of the invention include:
The invention discloses a deep arsenic removal system for arsenic-containing phosphoric acid, which has the following advantages: firstly, the primary reactor is a pipeline mixer, the reaction time and the reaction pressure can be fully ensured by the slender pipeline of the pipeline mixer, the overflow of hydrogen sulfide is prevented, secondly, the equipment volume of the pipeline mixer is small, the investment cost is low, thirdly, a baffle plate with holes in the primary reactor is coaxially inserted into the upper part of the primary reactor, a liquid inlet pipe is coaxially inserted into the upper part of the primary reactor, spraying holes are uniformly formed in the axial direction of the liquid inlet pipe, so that the desulfurizing agent and the arsenic-containing phosphoric acid solution are fully mixed, the sufficient contact reaction of the desulfurizing agent and the arsenic-containing phosphoric acid is realized, hydrogen sulfide is generated, meanwhile, the hydrogen sulfide is directly and effectively contacted and reacted with trace As in the arsenic-containing phosphoric acid solution, and insoluble sediment As2S3 and/or As2S5 particles are generated in the high-efficiency mixed primary reactor; fully stirring the primary reactant in the arsenic removal reaction tank by using a stirring paddle, and carrying out intensified reaction in the arsenic removal reaction tank under the pressure of 0.05-0.4 MPa, so that insoluble precipitate As2S3 and/or As2S5 is further generated by further reaction under the condition that the arsenic content in the arsenic removal phosphoric acid is very low, thereby further reducing the arsenic content in the arsenic removal phosphoric acid, wherein the arsenic content is 0.5ppm, and the arsenic removal rate reaches 98.33%;
Fourth, the upper part of the dearsenifying reaction tank is sealed by an air cone, so that the aim of avoiding leakage of H2S gas is fulfilled;
Fifth, in the industrial production process of the invention, unreacted hydrogen sulfide gas is discharged from the top of the dearsenification reaction tank, and is absorbed by the alkali liquor of the washing tower and then used as the configuration liquid of the dearsenification agent configuration tank, and the configuration liquid is returned to the system for continuous use, so that the environmental pollution and the safety risk can be effectively reduced.
Therefore, on one hand, the primary reactor for realizing the efficient mixing reaction has the unique advantages of low energy consumption, high efficiency, high reaction reliability and safety, guaranteed process controllability and product selectivity, small equipment volume and low investment cost;
On the other hand, unreacted hydrogen sulfide gas is discharged from the top of the dearsenification reaction tank, is absorbed by the alkali liquor of the washing tower and is used as the configuration liquor of the dearsenification agent configuration tank, and the return system is used continuously, and the top of the dearsenification reaction tank is sealed by an air cone, so that green and safe production is realized, great economic benefits are expected to be brought, and the dearsenification agent configuration tank is suitable for large-scale production and popularization and application.
Drawings
FIG. 1 is a system diagram of a deep arsenic removal system for arsenic-containing phosphoric acid according to the present invention.
FIG. 2 is a schematic diagram of the structure of the primary reactor of the present invention.
FIG. 3 is a schematic view of the structure of the liquid inlet pipe of the present invention.
Fig. 4 is A-A view of fig. 3.
FIG. 5 is a top view of the baffle plate of the present invention.
FIG. 6 is an enlarged view of the top gas cone of the dearsenification reaction tank according to the present invention.
Reference numerals illustrate: wherein: 10-an dearsenicator configuration tank; 20-dearsenifying agent is configured with a groove delivery pump; 30-a high-efficiency mixing primary reactor; 40-dearsenifying reaction tank; 50-a washing tower; 60-a scrubber circulation pump; 70-a second flow regulating valve; 80-a first flow regulating valve; 90-pressure regulating valve and 100-air cone.
Detailed Description
The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the detailed description is presented by way of example only and is not intended to limit the invention.
Examples
An arsenic-containing phosphoric acid deep arsenic removal system comprises an arsenic removal agent configuration tank 10, a primary reactor 30, an arsenic removal reaction tank 40 and a washing tower 50;
The top inlet of the dearsenifying agent configuration tank 10 is connected with a dearsenifying agent feeding pipe, the bottom outlet of the dearsenifying agent configuration tank 10 is communicated with a liquid inlet pipe 31 of the primary reactor 30 through a conveying pump 20 and a first flow regulating valve 80 pipeline, the upper side inlet of the primary reactor 30 is communicated with an arsenic-containing phosphoric acid feeding pipe through a second flow regulating valve 70 pipeline, the bottom outlet of the primary reactor 30 is communicated with the top side inlet of the dearsenifying reaction tank 40 through a pipeline, the top side inlet of the dearsenifying reaction tank 40 is communicated with the lower part of the washing tower 50 through a pipeline, the bottom of the washing tower 50 is divided into two paths through a washing tower circulating pump 60, one path is communicated with an upper spray pipe of the washing tower 50 through a pipeline, and the other path is communicated with the top of the dearsenifying agent configuration tank 10 through a pipeline;
stirring paddles are arranged in the dearsenifying agent preparation tank 10 and the dearsenifying reaction tank 40,
The top of the dearsenification reaction tank 40 is connected with an air cone 100 through a flange in a sealing way, an inlet at one side of the air cone 100 is communicated with a compressed air pipeline, and an outlet at the other side of the air cone 100 is communicated with the lower part of the washing tower 50 through a pressure regulating valve 90 pipeline;
The primary reactor 30 is a pipeline mixer, the upper part of the pipeline mixer is coaxially inserted with a liquid inlet pipe 31, spraying holes are uniformly formed in the axial direction of the liquid inlet pipe 31, more than 5 layers of baffle plates 32 are arranged on the lower part of the pipeline mixer, holes which are arranged in a triangular mode are formed in each baffle plate 32, and the holes in adjacent baffle plates 32 are arranged in a staggered mode.
The dearsenization agent is one of sodium sulfide or phosphorus pentasulfide, wherein the mass concentration of the sodium sulfide or the phosphorus pentasulfide is 5% -20%.
When the pipeline pressure measured by the pressure regulating valve 90 is less than or equal to 0.2MPa, the pressure regulating valve 90 is closed in a linkage way, compressed air is introduced into the dearsenification reaction tank 40 through a compressed air pipeline, so that the pressure of an air cone 100 at the top of the dearsenification reaction tank 40 is 0.5-0.8 MPa, and the pressure in the dearsenification reaction tank 40 is 0.05-0.4 MPa.
The pipe diameter of the primary reactor 30 is 50 mm-350 mm, the length is 1000-5000 mm, 5 layers of baffle plates 32 are arranged at the lower part of the primary reactor 30, the distance between every two adjacent baffle plates 32 is 100-500 mm, and the aperture of an opening hole on each baffle plate 32 is 10-30 mm.
The pipe diameter of the liquid inlet pipe 31 is 15 mm-60 mm, the length is 100-2000 mm, more than 5 layers of spraying holes are formed in the liquid inlet pipe 31, the distance between the spraying holes of adjacent layers is 50-200 mm, and each layer of spraying holes comprises 4 spraying holes uniformly distributed along the axial direction of the liquid inlet pipe 31.
When the system is in operation, the mass ratio of the arsenic-containing phosphoric acid to the dearsenifying agent is 110:1, introducing the arsenic-containing phosphoric acid into a first-stage reactor 30, wherein the mass concentration of the phosphoric acid is 45%, and the arsenic content is more than or equal to 1ppm;
mixing and reacting in the primary reactor 30 to obtain a primary reactant, wherein the reaction temperature of the primary reactor 30 is 75 ℃ and the reaction pressure is 0.5MPa;
the primary reactant is introduced into the dearsenification reaction tank 40 for strengthening reaction and gas-liquid separation to obtain hydrogen sulfide gas and dearsenification phosphoric acid, wherein the arsenic content of the dearsenification phosphoric acid is 0.5ppm, the dearsenification rate is 98.33%, the material retention time in the dearsenification reaction tank 40 is 5min, the reaction temperature is 70 ℃, and the reaction pressure is 0.15MPa.
H2S gas from an outlet at one side of the top of the washing tower 50 is absorbed by alkali liquor of the washing tower 50 and then is used as configuration liquid of the dearsenification agent configuration tank 10, so that recycling is realized;
The liquid from the bottom of the dearsenification reaction tank 40 is sent to a filtering facility for liquid-solid separation to obtain dearsenified phosphoric acid, which is used as raw material for producing industrial grade phosphoric acid and food grade phosphoric acid.
Therefore, on one hand, the primary reactor 30 for realizing the efficient mixing reaction has the unique advantages of low energy consumption, high efficiency, high reaction reliability and safety, guaranteed process controllability and product selectivity, small equipment volume and low investment cost;
on the other hand, unreacted hydrogen sulfide gas is discharged from the top of the dearsenification reaction tank 40, is absorbed by alkali liquor of the washing tower 50 and is used as configuration liquor of the dearsenification agent configuration tank 10, and the return system is used continuously, and the top of the dearsenification reaction tank 40 is sealed by the gas cone 100, so that green and safe production is realized, great economic benefits are expected, and the dearsenification reaction tank is suitable for large-scale production and popularization and application.
It will be readily appreciated by those skilled in the art that the foregoing description is merely a preferred embodiment of the invention and is not intended to limit the invention, but any modifications, equivalents, improvements or alternatives falling within the spirit and principles of the invention are intended to be included within the scope of the invention.
Claims (5)
1. An arsenic-containing phosphoric acid deep dearsenification system is characterized in that: comprises an arsenic removal agent configuration tank (10), a primary reactor (30), an arsenic removal reaction tank (40) and a washing tower (50);
The top inlet of the dearsenifying agent configuration groove (10) is communicated with a dearsenifying agent feeding pipe, the bottom outlet of the dearsenifying agent configuration groove (10) is communicated with a liquid inlet pipe (31) of the primary reactor (30) through a conveying pump (20) and a first flow regulating valve (80) pipeline, the upper side inlet of the primary reactor (30) is communicated with an arsenic-containing phosphoric acid feeding pipe through a second flow regulating valve (70) pipeline, the bottom outlet of the primary reactor (30) is communicated with the top side inlet of the dearsenifying reaction groove (40) through a pipeline, the top side inlet of the dearsenifying reaction groove (40) is communicated with the lower part of the washing tower (50) through a pipeline, the bottom of the washing tower (50) is divided into two paths after passing through a washing tower circulating pump (60), one path is communicated with the upper spray pipe of the washing tower (50) through a pipeline, and the other path is communicated with the top of the dearsenifying agent configuration groove (10) through a pipeline;
stirring paddles are arranged in the dearsenifying agent configuration tank (10) and the dearsenifying reaction tank (40),
The top of the dearsenifying reaction tank (40) is connected with an air cone (100) through a flange in a sealing way, an inlet at one side of the air cone (100) is communicated with a compressed air pipeline, and an outlet at the other side of the air cone (100) is communicated with the lower part of the washing tower (50) through a pressure regulating valve (90) pipeline;
The primary reactor (30) is a pipeline mixer, the upper part of the pipeline mixer is coaxially inserted with a liquid inlet pipe (31), spraying holes are uniformly formed in the axial direction of the liquid inlet pipe (31), more than 5 layers of baffle plates (32) are arranged at the lower part of the pipeline mixer, the holes in triangular arrangement are formed in each baffle plate (32), and the holes in adjacent baffle plates (32) are staggered;
When the system is in operation, the mass ratio of the arsenic-containing phosphoric acid to the dearsenifying agent is 100: 1-500:1 is introduced into a primary reactor (30), wherein the mass concentration of the phosphoric acid is 30-64% and the arsenic content is more than or equal to 1ppm;
mixing and reacting in the primary reactor (30) to obtain a primary reactant, wherein the reaction temperature of the primary reactor (30) is 60-90 ℃ and the reaction pressure is 0.3-0.6 MPa;
the primary reactant is introduced into an arsenic removal reaction tank (40) for strengthening reaction and gas-liquid separation, so as to obtain hydrogen sulfide gas and arsenic removal phosphoric acid, wherein the arsenic content of the arsenic removal phosphoric acid is less than or equal to 0.5ppm, the retention time of materials in the arsenic removal reaction tank (40) is 3-5 min, the reaction temperature is 60-90 ℃, and the reaction pressure is 0.05-0.4 MPa.
2. The deep arsenic removal system for arsenic-containing phosphoric acid according to claim 1, wherein: the dearsenization agent is one of sodium sulfide or phosphorus pentasulfide, wherein the mass concentration of the sodium sulfide or the phosphorus pentasulfide is 5% -20%.
3. The deep arsenic removal system for arsenic-containing phosphoric acid according to claim 1, wherein: when the pipeline pressure measured by the pressure regulating valve (90) is less than or equal to 0.2MPa, the pressure regulating valve (90) is closed in a linkage way, compressed air is introduced into the dearsenification reaction tank (40) through a compressed air pipeline, so that the pressure of an air cone (100) at the top of the dearsenification reaction tank (40) is 0.5-0.8 MPa, and the pressure in the dearsenification reaction tank (40) is 0.05-0.4 MPa.
4. The deep arsenic removal system for arsenic-containing phosphoric acid according to claim 1, wherein: the pipe diameter of the primary reactor (30) is 50-350 mm, the length of the primary reactor is 1000-800 mm, 5 layers of baffle plates (32) are arranged at the lower part of the primary reactor (30), the distance between every two adjacent baffle plates (32) is 100-500 mm, and the aperture of an opening on each baffle plate (32) is 10-30 mm.
5. The deep arsenic removal system for arsenic-containing phosphoric acid according to claim 1, wherein: the pipe diameter of the liquid inlet pipe (31) is 15 mm-60 mm, the length of the liquid inlet pipe is 100-2000 mm, more than 5 layers of spraying holes are formed in the liquid inlet pipe (31), the distance between the spraying holes of adjacent layers is 50-200 mm, and each layer of spraying holes comprises 4 spraying holes uniformly distributed along the axial direction of the liquid inlet pipe (31).
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| CN103011106A (en) * | 2012-12-27 | 2013-04-03 | 广西明利化工有限公司 | Production device of food-grade phosphoric acid |
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| CN103011106A (en) * | 2012-12-27 | 2013-04-03 | 广西明利化工有限公司 | Production device of food-grade phosphoric acid |
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| Title |
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| SK静态混合器对工业磷酸脱砷的过程强化研究;任新林;梅毅;冯梦黎;李柏扬;吕武华;问亚玲;王驰;何德东;化工学报;20181231(第0s2期);全文 * |
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