CN112978768B - System for producing sodium metabisulfite and preparation method - Google Patents
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- CN112978768B CN112978768B CN201911285309.9A CN201911285309A CN112978768B CN 112978768 B CN112978768 B CN 112978768B CN 201911285309 A CN201911285309 A CN 201911285309A CN 112978768 B CN112978768 B CN 112978768B
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- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/14—Preparation of sulfites
- C01D5/145—Pyrosulfites or metabisulfites
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Abstract
The invention provides a system for producing sodium metabisulfite and a preparation method thereof, belonging to the field of chemical industry. The method comprises the steps that sulfur dioxide-containing gas sequentially passes through a first reactor, a second reactor and a third reactor, supersaturated sodium sulfite solution sequentially passes through the third reactor, the second reactor and the first reactor, and a large amount of sodium pyrosulfite is generated in the first reactor; when sodium sulfite completely reacts and reaches the reaction end point, crystal slurry containing sodium metabisulfite is extracted from the first reactor and sent to an elutriation tank, coarse crystal slurry is separated in a centrifuge, sodium sulfite slurry generated by adding soda ash into centrifugal mother liquor is sent to a third reactor, centrifugally separated solid wet material is sent to a drier for drying, and then packaged into a sodium metabisulfite product; and tail gas generated by drying is discharged after being subjected to alkali washing and dust removal by a tail gas tower, and washing liquid generated by washing the tail gas is sent to an alkali distribution tank and returns to the reactor. The sodium metabisulfite prepared by the method has the advantages of good quality, novel process flow, low energy consumption and wide popularization and use values.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a system for producing sodium metabisulfite and a preparation method thereof.
Background
China is a large country for resource production and consumption, but a great environmental problem is also generated during production and consumption. In recent years, resource recovery type desulfurization techniques, such as organic amine desulfurization techniques and activated carbon desulfurization techniques, have been applied in large scale, and the desulfurization by-product is SO 2 . The conventional method is to add SO 2 The sulfuric acid is prepared, the sulfuric acid capacity is surplus at the present stage in China, the market demand is greatly influenced regionally, the sulfuric acid is difficult to store and transport, the risk of storehouse expansion exists, the economic value is low, and SO is utilized 2 The production of sodium metabisulfite can realize good economic benefit, and is a good method.
A process for preparing sodium pyrosulfite includes such steps as passing the gas containing sulfur dioxide through three-stage bubbling reactor to generate sodium pyrosulfite crystal, centrifugal separation, preparing alkali solution from mother liquid and soda, returning it to three-stage reactor, and drying. Because the traditional process adopts a bubble reactor, the gas resistance is large, and the power consumption is large; each reaction kettle needs to be switched regularly, the gas pressure fluctuation is large, and the operation is complicated; the product quality is unstable, and the crystallization uniformity is not good; equipment SO 2 Large dispersion and discharge capacity and poor production environment.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a system for producing sodium metabisulfite and a preparation method thereof.
The purpose of the invention can be realized by the following technical scheme:
a system for producing sodium metabisulfite comprises a third reactor, a second reactor and a first reactor, wherein a soda storage bin is respectively connected with a soda preparation tank and a soda solution tank; the output end of the lower part of the second reactor is respectively connected with the jet reactor positioned at the top of the second reactor and the upper part of the first reactor through a second circulating pump; the output end of the lower part of the first reactor is respectively connected with a jet reactor and an elutriation tank which are positioned at the top of the first reactor through a first circulating pump; the elutriation tank is connected with the drier through the centrifugal machine in sequence.
In the technical scheme of the invention: the output end of the top of the elutriation tank and the liquid output end of the centrifuge are both connected with the alkali distribution tank.
In the technical scheme of the invention: the gas output end of the dryer is connected with the tail gas washing tower; the output end of the bottom of the alkali liquor tank is connected with the washing circulating tank, and the output end of the bottom of the washing circulating tank is connected with the tail gas washing tower; the output end of the middle upper part of the tail gas washing tower is connected with the washing circulation tank, and the output end of the bottom of the tail gas washing tower is respectively connected with the middle part of the tail gas washing tower and the alkali distribution tank.
The technical scheme of the invention is as follows: the sulfur dioxide gas output pipeline is connected with the injection reactor positioned on the upper portion of the first reactor, the gas output end at the top of the first reactor is connected with the injection reactor positioned on the upper portion of the second reactor, the gas output end at the upper portion of the second reactor is connected with the injection reactor positioned on the upper portion of the third reactor, and the gas output end at the top of the third reactor is discharged out of the room.
The technical scheme of the invention is as follows: the second reactor and the first reactor comprise crystallizers, the top of each crystallizer is provided with a jet reactor, the lower part of each crystallizer is connected with the upper part of the jet reactor through a circulating pump, and the top of each jet reactor is provided with a gas input system; the bottom of the crystallizer is a crystal discharge section, and the upper part of the crystallizer is also provided with a raw material liquid interface; the top of the crystallizer is also provided with a washing device for reaction tail gas, the lower middle part of the device is provided with a defoaming device, a washing water interface is also arranged above the defoaming device, and the top of the washing device is a discharge port for the reaction tail gas.
The technical scheme of the invention is as follows: the lower part of the crystallizer is a contracted conical surface structure, the included angle of the contraction is 60-100 degrees, the lower part of the conical surface structure is connected with a section of sedimentation tube, and the conical surface structure and the sedimentation tube form a crystal discharge section.
The technical scheme of the invention is as follows: the injection reactor is sequentially provided with a discharge pipe, an expansion pipe, a choke, a contraction pipe and an air inlet pipe from bottom to top, the top of the air inlet pipe is provided with a raw material gas connector, and the lower part of the air inlet pipe is provided with a liquid connector; the contraction angle of the contraction tube is 10-60 degrees, and the expansion angle of the expansion tube is 5-30 degrees; the discharge pipe of the jet reactor extends out of the top cover of the crystallizer, and the extension length of the discharge pipe is 1000-4000 mm.
A method for producing sodium metabisulfite by using the system comprises the following steps:
(1) Reaction and crystallization: sodium sulfite slurry sequentially passes through a third reactor, a second reactor and a first reactor, gas containing sulfur dioxide sequentially passes through the first reactor, the second reactor and the third reactor, sodium sulfite is completely reacted in the first reactor to produce supersaturation and generate a large amount of sodium metabisulfite crystals, tail gas is discharged from the third reactor, and slurry containing the sodium metabisulfite crystals is extracted from the first reactor and is sent to an elutriation tank;
(2) Crystal separation: the crystal slurry of the first reactor realizes the coarse and fine separation and concentration of crystals in the elutriation tank, and high-quality crystals are collected from the lower part of the elutriation tank and sent to a centrifuge; fine crystals and centrifugal mother liquor discharged from the upper part of the elutriation tank are sent to an alkali preparation tank and are converted into slurry containing sodium sulfite crystals through reaction with sodium carbonate; sending the high-quality crystal obtained by centrifugation to a dryer for drying;
(3) And (3) drying and packaging: exchanging heat between the centrifuged sodium metabisulfite crystals and hot air in a drier, evaporating the water on the surfaces of the crystals to dryness, and then conveying solid powder into a packaging machine to be packaged into a bagged product;
(4) Mixing soda, namely discharging the soda into a soda tank for storage, quantitatively feeding the soda into a soda mixing tank, reacting the soda with centrifugal mother liquor, liquid discharged from an elutriation tank and tail gas washing liquid in the soda mixing tank, defoaming and degassing, and then sending the reaction product to a third reactor;
(5) And (3) tail gas treatment, wherein tail gas discharged by each device and dry tail gas generated by drying are sent to a tail absorption tower, the tail gas is washed by alkali liquor, the concentration of sulfur dioxide in the tail gas is reduced to below 10ppm and discharged, and washing liquid generated by washing is sent to an alkali preparation tank for reuse.
The method comprises the following steps: the solid content of the circulating slurry of the first reactor, the second reactor and the third reactor is 5-30%, and the temperature is 40-60 ℃.
The method comprises the following steps: the volume of the elutriation tank is 3-6 times of that of the first reactor.
The method comprises the following steps: the sulfur dioxide-containing gas has a concentration of more than 3% and can be one or a combination of more than one of sulfur burning smoke, pyrite burning smoke, organic amine desulfurization regeneration sulfur dioxide gas and active carbon desulfurization regeneration sulfur dioxide gas.
The method comprises the following steps: first reactor, second reactor, third reactor adopt tower structure, and the reactor lower part is the thick liquid district, and upper portion is the mixing section, and every reactor has the circulating pump that corresponds with it, and the circulating pump extracts the thick liquid that contains sodium sulfite from the reactor lower part, and the thick liquid carries out gas-liquid contact with sulfur dioxide at the mixing section, absorbs the sodium metabisulfite thick liquid that sulfur dioxide gas produced and falls into the reactor lower part, and remaining tail gas is discharged from reactor upper portion gas vent.
The method comprises the following steps: the first reactor, the second reactor and the third reactor are in concurrent contact with the sodium sulfite slurry and the sulfur dioxide gas, and the resistance of the reactors is 3-8 kpa.
The method comprises the following steps: the elutriation tank is of a vertical cylinder structure, liquid discharged by the primary reactor enters the bottom of the elutriation tank tangentially to generate a turbulent flow effect, under the action of gravity and liquid recoil force, the coarse and fine separation and concentration of crystals are realized, high-concentration coarse crystal slurry is discharged to a centrifugal machine from the side surface of the lower part, and low-concentration fine crystal slurry is discharged to a liquid distribution tank from the upper part.
The method comprises the following steps: the dryer adopts an air flow drying type, and the air inlet temperature of the dryer is 130-160 ℃.
The method comprises the following steps: the alkali preparation tank is provided with a stirrer and a defoaming device, sodium carbonate, centrifugal mother liquor, liquid discharged from the elutriation tank and tail gas washing liquid are subjected to neutralization reaction to generate sodium sulfite, the sodium sulfite is defoamed and degassed and then is sent to a third reactor, the solid content of the alkali preparation tank is 5-30%, and the pH value is 5.0-7.0.
The invention has the beneficial effects that:
1) The invention is suitable for preparing sodium metabisulfite by various gases containing sulfur dioxide, provides a relatively economic process for preparing sodium metabisulfite by sulfur dioxide gases with low cost, and has good quality of byproducts; compared with the prior art, the comprehensive production cost is reduced by about 10 percent, the content of the main component of the byproduct is more than 97.5 percent and is far higher than 96.5 percent of the requirement of national standard superior products.
2) The process is novel, safe, reliable and environment-friendly; the adopted device has simple structure and convenient maintenance;
3) The first reactor, the second reactor and the third-party reactor adopt tower structures, have small resistance, complete reaction, stability and reliability, and are particularly suitable for large-scale production, while the bubbling type reaction kettle is adopted in the prior art, and is operated intermittently, and the bubbling liquid level has high resistance.
4) The exhaust gas of all the equipment is collected into the tail gas washing tower for alkali washing treatment, so that sulfur dioxide is recovered, no sulfur dioxide overflows from a factory building, the environment is good, and no secondary pollution is caused.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Wherein: FIG. 1: 101-product; 102-sodium carbonate; 103-sulfur dioxide gas; 104-reaction off-gas; 1-a third reactor; 2-a third circulation pump; 3-a second reactor; 4-a second circulation pump; 5-a first reactor; 6-a first circulation pump; 7-liquid supplement pump; 8-alkali preparation tank; 9-a first soda ash conveyor; 10-a lye tank; 11-lye pump; 12-a second soda ash conveyor; 13-soda ash storage; 14-a second tail gas washing circulating pump; 15-washing circulation tank; 16-a first tail gas washing circulating pump; 17-a tail gas wash column; 18-a elutriation tank; 19-a centrifuge; 20-a dryer; 21-packaging machine; 22-jet reactor.
FIG. 2 is a schematic structural view of a gas-liquid two-phase continuous reaction crystallization apparatus;
wherein: 23-crystal discharge section, 24-raw material liquid interface, 25-defoaming device, 26-washing water interface, and 27-discharge outlet of reaction tail gas.
FIG. 3 is a schematic view of the structure of a spray reactor.
Wherein: 28-raw material gas interface, 29-air inlet pipe, 30-contraction pipe, 31-throat pipe, 32-expansion pipe, 33-discharge pipe and 34-liquid interface.
Detailed Description
The invention is further illustrated by the following examples, without limiting the scope of the invention:
referring to fig. 1 to 3, a system for producing sodium metabisulfite comprises a third reactor 1, a second reactor 3 and a first reactor 5, wherein a soda storage bin 13 is respectively connected with a soda preparation tank 8 and a soda tank 10, the output end of the soda tank 10 is connected with the upper part of the third reactor 1, and the output end of the lower part of the third reactor 1 is respectively connected with a spray reactor 22 positioned at the top of the third reactor 1 and the upper part of the second reactor 3 through a third circulating pump 2; the output end of the lower part of the second reactor 3 is respectively connected with the jet reactor 22 positioned at the top of the second reactor 3 and the upper part of the first reactor 1 through a second circulating pump 4; the output end of the lower part of the first reactor 5 is respectively connected with a spray reactor 22 and an elutriation tank 18 which are positioned at the top of the first reactor 5 through a first circulating pump 6; the elutriation tank 18 is connected to a centrifuge 19 and a dryer 20 in this order.
The output end of the top of the elutriation tank 18 and the liquid output end of the centrifuge 19 are both connected with the alkali distribution tank 8.
The gas output end of the dryer 20 is connected with the tail gas washing tower 17; the output end of the bottom of the lye tank 10 is connected with a washing circulating tank 15, and the output end of the bottom of the washing circulating tank 15 is connected with a tail gas washing tower 17; the output end of the upper middle part of the tail gas washing tower 17 is connected with the washing circulation tank 15, and the output end of the bottom of the tail gas washing tower 17 is respectively connected with the middle part of the tail gas washing tower 17 and the alkali distribution tank 8.
The sulfur dioxide gas output pipeline is connected with the injection reactor 22 positioned on the upper portion of the first reactor 5, the gas output end at the top of the first reactor 5 is connected with the injection reactor 22 positioned on the upper portion of the second reactor 3, the gas output end at the upper portion of the second reactor 3 is connected with the injection reactor 22 positioned on the upper portion of the third reactor 1, and the gas output end at the top of the third reactor 1 is discharged to the outside.
The third reactor 1, the second reactor 3 and the first reactor 5 comprise crystallizers, the top of each crystallizer is provided with a jet reactor 22, the lower part of each crystallizer is connected with the upper part of the jet reactor 22 through a circulating pump, and the top of each jet reactor 22 is provided with a gas input system; the bottom of the crystallizer is a crystal discharge section 23, and the upper part of the crystallizer is also provided with a raw material liquid interface 24; the top of the crystallizer is also provided with a washing device for reaction tail gas, the middle lower part of the device is provided with a defoaming device 25, a flushing water interface 26 is also arranged above the defoaming device 25, and the top of the washing device is a discharge port 27 for the reaction tail gas.
The lower part of the crystallizer is a contracted conical surface structure, the contracted included angle is 60-100 degrees, the lower part of the conical surface structure is connected with a section of settling tube, and the conical surface structure and the settling tube form a crystal discharge section 23.
The jet reactor 22 is sequentially provided with a discharge pipe 33, an expansion pipe 32, a throat pipe 31, a contraction pipe 30 and an air inlet pipe 29 from bottom to top, the top of the air inlet pipe is provided with a raw material gas connector 28, and the lower part of the air inlet pipe 29 is provided with a liquid connector 34; the contraction angle of the contraction tube is 10-60 degrees, and the expansion angle of the expansion tube is 5-30 degrees; the discharge pipe 33 of the injection reactor 22 extends out of the top cover of the crystallizer, and the extension length of the discharge pipe is 1000-4000 mm.
A method for producing sodium metabisulfite by utilizing the system comprises the following steps:
(1) Reaction and crystallization: sodium sulfite slurry passes through the third reactor 1, the second reactor 3 and the first reactor 5 in sequence, sulfur dioxide-containing gas passes through the first reactor 5, the second reactor 3 and the third reactor 1 in sequence, sodium sulfite is completely reacted in the first reactor 5 to produce supersaturation and generate a large amount of sodium metabisulfite crystals, tail gas is discharged from the third reactor 3, and slurry containing the sodium metabisulfite crystals is extracted from the first reactor 5 and sent to an elutriation tank 18;
wherein: the solid content of the circulating slurry of the first reactor 5, the second reactor 3 and the third reactor 1 is 5-30%, and the temperature is 40-60 ℃. The first reactor, the second reactor and the third reactor are in concurrent contact with the sodium sulfite slurry and the sulfur dioxide gas, and the resistance of the reactors is 3-4 kpa.
(2) Crystal separation: the crystal slurry of the first reactor 5 realizes crystal thickness separation and crystal concentration in the elutriation tank 18, and high-quality crystals are extracted from the lower part of the elutriation tank 18 and sent to a centrifuge 19; fine crystals and centrifugal mother liquor discharged from the upper part of the elutriation tank 18 are sent to an alkali preparation tank 8 and are converted into slurry containing sodium sulfite crystals through reaction with sodium carbonate; the high-quality crystal centrifuged is sent to a dryer 20 for drying; the volume of the elutriation tank 18 is 3 to 6 times of the volume of the first reactor 5.
(3) And (3) drying and packaging: exchanging heat between the centrifuged sodium metabisulfite crystals and hot air in a dryer 20, evaporating the water on the surfaces of the crystals to dryness, and then feeding solid powder into a packaging machine 21 to be packaged into bagged products; the dryer adopts an air flow drying type, and the air inlet temperature of the dryer is 130-160 ℃.
(4) Mixing soda, namely discharging the soda into a soda tank for storage, quantitatively feeding the soda into a soda mixing tank, reacting the soda with centrifugal mother liquor, liquid discharged from an elutriation tank and tail gas washing liquid in a soda mixing tank 8, defoaming and degassing, and then sending the reaction product to a third reactor 1; the alkali preparation tank is provided with a stirrer and a defoaming device, sodium carbonate, centrifugal mother liquor, liquid discharged from the elutriation tank and tail gas washing liquid are subjected to neutralization reaction to generate sodium sulfite, the sodium sulfite is defoamed and degassed and then is conveyed to a third reactor, the solid content of the alkali preparation tank is 5-30%, and the pH value is 5.0-7.0.
(5) And (3) tail gas treatment, wherein tail gas discharged by each device and dry tail gas generated by drying are sent to a tail absorption tower 17, the tail gas is washed by alkali liquor, the concentration of sulfur dioxide in the tail gas is reduced to below 10ppm and discharged, and washing liquid generated by washing is sent to an alkali preparation tank for reuse.
Compared with the prior art, the comprehensive production cost is reduced by about 10 percent, the content of the main component of the byproduct is more than 97.5 percent and is far higher than 96.5 percent of the requirement of national standard superior products.
Claims (8)
1. The utility model provides a system for production sodium metabisulfite which characterized in that: the system comprises a third reactor (1), a second reactor (3) and a first reactor (5), wherein a soda storage bin (13) is respectively connected with a soda blending tank (8) and a soda tank (10), the output end of the soda blending tank (8) is connected with the upper part of the third reactor (1), and the output end of the lower part of the third reactor (1) is respectively connected with a third injection reactor positioned at the top of the third reactor (1) and the upper part of the second reactor (3) through a third circulating pump (2); the output end of the lower part of the second reactor (3) is respectively connected with the second jet reactor positioned at the top of the second reactor (3) and the upper part of the first reactor (5) through a second circulating pump (4); the output end of the lower part of the first reactor (5) is respectively connected with a first jet reactor and an elutriation tank (18) which are positioned at the top of the first reactor (5) through a first circulating pump (6); the elutriation tank (18) is connected with the drier (20) through a centrifugal machine (19) in sequence;
the gas output end of the dryer (20) is connected with the tail gas washing tower (17); the output end of the bottom of the lye tank (10) is connected with a washing circulating tank (15), and the output end of the bottom of the washing circulating tank (15) is connected with a tail gas washing tower (17); the output end of the middle upper part of the tail gas washing tower (17) is connected with the washing circulation tank (15), and the output end of the bottom of the tail gas washing tower (17) is respectively connected with the middle part of the tail gas washing tower (17) and the alkali distribution tank (8);
the jet reactor is sequentially provided with a discharge pipe (33), an expansion pipe (32), a throat pipe (31), a contraction pipe (30) and an air inlet pipe (29) from bottom to top, the top of the air inlet pipe is provided with a raw material gas connector (28), and the lower part of the air inlet pipe (29) is provided with a liquid connector (34); the contraction angle of the contraction pipe is 10 to 60 degrees, and the expansion angle of the expansion pipe is 5 to 30 degrees; the discharge pipe (33) of the jet reactor extends out of the top cover of the crystallizer, and the extension length of the discharge pipe is 1000-4000 mm.
2. The system for producing sodium metabisulfite of claim 1, wherein: the output end of the top of the elutriation tank (18) and the liquid output end of the centrifuge (19) are both connected with the alkali distribution tank (8).
3. The system for producing sodium metabisulfite of claim 1, wherein: the sulfur dioxide gas output pipeline is connected with a first injection reactor positioned on the upper portion of a first reactor (5), a gas output end at the top of the first reactor (5) is connected with a second injection reactor positioned on the upper portion of a second reactor (3), a gas output end on the upper portion of the second reactor (3) is connected with a third injection reactor positioned on the upper portion of a third reactor (1), and a gas output end at the top of the third reactor (1) is discharged out of the room.
4. The system for producing sodium metabisulfite of claim 3, wherein: the third reactor (1), the second reactor (3) and the first reactor (5) comprise crystallizers, the top of each crystallizer is provided with a jet reactor, the lower part of each crystallizer is connected with the upper part of the jet reactor through a circulating pump, and the top of each jet reactor is provided with a gas input system; the bottom of the crystallizer is a crystal discharge section (23), and the upper part of the crystallizer is also provided with a raw material liquid interface (24); the top of the crystallizer is also provided with a washing device for reaction tail gas, the middle lower part of the device is provided with a defoaming device (25), a washing water interface (26) is also arranged above the defoaming device (25), and the top of the washing device is a discharge port (27) for the reaction tail gas.
5. The system for producing sodium metabisulfite of claim 3, wherein: the lower part of the crystallizer is of a contracted conical surface structure, the included angle of the contraction is 60 to 100 degrees, the lower part of the conical surface structure is connected with a settling tube, and the conical surface structure and the settling tube form a crystal discharge section (23).
6. A method for producing sodium metabisulfite using the system of claim 1, wherein: the method comprises the following steps:
(1) Reaction and crystallization: sodium sulfite slurry sequentially passes through a third reactor (1), a second reactor (3) and a first reactor (5), sulfur dioxide-containing gas sequentially passes through the first reactor (5), the second reactor (3) and the third reactor (1), sodium sulfite is completely reacted in the first reactor (5) to generate supersaturation and generate a large amount of sodium metabisulfite crystals, tail gas is discharged from the third reactor (1), and the slurry containing the sodium metabisulfite crystals is extracted from the first reactor (5) and sent to an elutriation tank (18);
(2) Crystal separation: the crystal slurry of the first reactor (5) realizes the coarse and fine separation and concentration of crystals in the elutriation tank (18), and high-quality crystals are extracted from the lower part of the elutriation tank (18) and sent to a centrifuge (19); fine crystals and centrifugal mother liquor discharged from the upper part of the elutriation tank (18) are sent to an alkali preparation tank (8) and are converted into slurry containing sodium sulfite crystals through reaction with sodium carbonate; the high-quality crystal centrifuged out is sent to a dryer (20) for drying;
(3) And (3) drying and packaging: the centrifuged sodium metabisulfite crystals exchange heat with hot air in a drier (20), the water on the surfaces of the crystals is evaporated to dryness, and then solid powder is sent to a packaging machine (21) to be packaged into bagged products;
(4) Mixing soda, namely discharging the soda into a soda tank for storage, quantitatively feeding the soda into a soda mixing tank, reacting the soda with centrifugal mother liquor, liquid discharged from an elutriation tank and tail gas washing liquid in a soda mixing tank (8), defoaming and degassing, and then conveying the reaction product to a third reactor (1);
(5) And (3) tail gas treatment, wherein tail gas discharged by each device and dry tail gas generated by drying are sent to a tail gas washing tower (17), the tail gas is washed by alkali liquor, the concentration of sulfur dioxide in the tail gas is reduced to below 10ppm and discharged, and washing liquid generated by washing is sent to an alkali distribution tank for reuse.
7. The method of claim 6, wherein: the solid content of the circulating slurry of the first reactor (5), the second reactor (3) and the third reactor (1) is 5-30%, and the temperature is 40-60 ℃.
8. The method of claim 6, wherein: the volume of the elutriation tank (18) is 3~6 times of the volume of the first reactor (5).
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| PCT/CN2020/089516 WO2021114562A1 (en) | 2019-12-13 | 2020-05-10 | System and preparation method for producing sodium metabisulfite |
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| CN202909642U (en) * | 2012-10-24 | 2013-05-01 | 中国石油化工股份有限公司 | Gas mixing element and gas mixing device employing same |
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| CN205313114U (en) * | 2016-01-06 | 2016-06-15 | 宣城市楷昂化工有限公司 | Sodium metabisulfite apparatus for producing |
| CN107551599A (en) * | 2017-10-24 | 2018-01-09 | 东南大学 | Multistage feeding formula anti-solvent jet crystallization device and its jet crystallization method |
| CN211393883U (en) * | 2019-12-13 | 2020-09-01 | 南京工业大学 | System for production sodium metabisulfite |
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| CN112978768A (en) | 2021-06-18 |
| WO2021114562A1 (en) | 2021-06-17 |
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