CN213294705U

CN213294705U - System for production sodium metabisulfite

Info

Publication number: CN213294705U
Application number: CN202021017738.6U
Authority: CN
Inventors: 陈任远; 吴振山; 徐延忠; 刘大华
Original assignee: Jiangsu Deyitong Environmental Protection Technology Co ltd
Current assignee: Jiangsu Deyitong Environmental Protection Technology Co ltd
Priority date: 2020-06-05
Filing date: 2020-06-05
Publication date: 2021-05-28
Anticipated expiration: 2030-06-05

Abstract

The utility model discloses a system for production sodium metabisulfite relates to the chemical industry field, including first reactor, the second reactor, third reactor and soda storage bin, sulfur dioxide gas loops through first reactor, second reactor and third reactor, soda storage bin links to each other with join in marriage alkali groove and lye tank respectively, the output that joins in marriage the alkali groove links to each other with the upper portion of third reactor, the output of third reactor lower part passes through the third circulating pump respectively with the upper portion that is located the injection reactor at third reactor top and second reactor links to each other, the output of second reaction lower part passes through the second circulating pump and links to each other with the upper portion that is located the injection reactor at second reactor top and first reactor, the output of first reactor lower part links to each other with the injection reactor and the elutriation jar that are located the first reactor top respectively through the first circulating pump. The sodium metabisulfite prepared by the system has good quality, novel process flow and low energy consumption, and reduces the pollution to the environment.

Description

System for production sodium metabisulfite

Technical Field

The utility model relates to a chemical industry field, concretely relates to system for production sodium metabisulfite.

Background

China is a large country for resource production and consumption, however, the production and consumption also cause significant environmental problems, and in recent years, resource recovery type desulfurization technologies, such as organic amine desulfurization technology and activated carbon desulfurization technology, are applied in a large scale, and the desulfurization byproduct is SO 2. The traditional method is to prepare SO2 into sulfuric acid, the market demand is greatly influenced by regionality due to the surplus of sulfuric acid capacity at the present stage, the sulfuric acid is difficult to store and transport, the risk of expanding a warehouse exists, and the economic value is low, and the production of sodium metabisulfite by utilizing SO2 can realize good economic benefit and is a good method.

The traditional technology for producing sodium metabisulfite is characterized in that sulfur dioxide-containing gas sequentially passes through three stages of bubbling reaction kettles to generate sodium metabisulfite crystals, then the sodium metabisulfite crystals are centrifugally separated, mother liquor is added with soda ash to prepare alkali liquor, the alkali liquor returns to a three-stage reactor, and the crystals are dried to obtain the sodium metabisulfite. 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; the equipment SO2 has large emission and poor production environment. Therefore, it is necessary to provide a wet desulfurization apparatus that does not generate colored rain and smoke in response to the deficiencies of the prior art.

Disclosure of Invention

In order to overcome the deficiency among the prior art, the utility model provides a system for producing sodium metabisulfite, the sodium metabisulfite quality that this system made is good, and technological process is novel, the energy consumption is low.

In order to achieve the purpose, the system for producing the sodium metabisulfite comprises a first reactor and a second reactor, the system comprises a third reactor and a soda storage bin, sulfur dioxide gas sequentially passes through the first reactor, the second reactor and the third reactor, the soda storage bin is respectively connected with a soda tank and a soda tank, the output end of the soda tank is connected with the upper part of the third reactor, the output end of the lower part of the third reactor is respectively connected with a jet reactor positioned at the top of the third reactor and the upper part of the second reactor through a third circulating pump, the output end of the lower part of the second reactor is 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 the jet reactor positioned at the top of the first reactor and an elutriation tank through the first circulating pump, and the elutriation tank is sequentially connected with a centrifugal machine and a drying machine.

Preferably, the gas outlet of the upper part of the first reactor is connected with the injection reactor positioned at the upper part of the second reactor, the gas outlet of the upper part of the second reactor is connected with the injection reactor positioned at the upper part of the third reactor, and the gas outlet of the upper part of the third reactor discharges the gas to the outside.

Preferably, the first reactor, the second reactor and the third reactor are of a tower structure, wherein crystallizers are arranged inside the first reactor, the second reactor and the third reactor, a jet reactor is arranged at the top of each crystallizer, the lower portion of each crystallizer is communicated with the upper portion of the corresponding jet reactor through a circulating pump, a washing mechanism is further arranged at the top of each crystallizer, the washing mechanism is connected with the top of the next-stage jet reactor, and a raw material liquid interface used for receiving crystal slurry transported by the corresponding circulating pump is arranged at the upper portion of each crystallizer.

Preferably, 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 through an alkali liquor pump, and the output end of the bottom of the washing circulating tank is connected with the tail gas washing tower through a second tail gas washing circulating pump; 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 through a first tail gas washing circulation pump.

Preferably, pipelines for conveying fine crystals and centrifugal mother liquor are connected between the elutriation tank and the alkali distribution tank and between the centrifuge and the alkali distribution tank.

Preferably, a first soda ash conveyor and a second soda ash conveyor are respectively arranged on pipelines connecting the soda ash storage bin with the soda blending tank and the soda lye tank.

Preferably, 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.

Preferably, the injection reactor is sequentially provided with a discharge pipe, an expansion pipe, a throat pipe, a contraction pipe and an air inlet pipe from bottom to top, the top of the air inlet pipe is provided with a feed gas connector, the lower part of the air inlet pipe is provided with a liquid connector, the contraction angle of the contraction pipe is 10-60 degrees, the expansion angle of the expansion pipe is 10-60 degrees, the discharge pipe of the injection reactor extends out of the top cover of the crystallizer, and the extension length of the discharge pipe is 0.5-6 m.

Preferably, the foam remover is arranged at the middle lower part of the washing mechanism, a washing water interface is further arranged above the foam remover, and the top of the washing mechanism is a discharge port of the reaction tail gas.

The utility model discloses following beneficial effect has:

1) the utility model is suitable for preparing sodium metabisulfite from various gases containing sulfur dioxide, provides a process for preparing sodium metabisulfite from sulfur dioxide gas with low cost, and has good quality of by-products; 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 of the utility model is novel, safe, reliable and environment-friendly; the adopted device has simple structure and convenient maintenance;

3) the utility model discloses first reactor, second reactor, third party reactor adopt tower structure, and the resistance is little, and the reaction is thorough, and is reliable and stable, specially adapted large-scale production, and the tradition adopts tympanic bulla formula reation kettle, intermittent operation, and the high resistance of tympanic bulla liquid level is big.

4) The utility model discloses tail gas scrubbing tower is all collected in all equipment exhausts, carries out the alkali wash and handles, has retrieved the sulfur dioxide, and no sulfur dioxide spills over in the factory building, and the environment is good, no secondary pollution.

Drawings

The invention will be further described and illustrated with reference to the accompanying drawings.

FIG. 1 is a schematic view showing the overall structure of a system for producing sodium metabisulfite.

FIG. 2 is a schematic diagram of the crystallizer configuration of the first reactor of FIG. 1.

FIG. 3 is a schematic diagram of the configuration of the injection reactor of the sodium metabisulfite production system of FIG. 1.

Reference numerals: 101. producing a product; 102. soda ash; 103. sulfur dioxide 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. a liquid supplementing pump; 8. an alkali preparation tank; 9. a first soda ash conveyor; 10. a lye tank; 11. an alkaline liquid pump; 12. a second soda ash conveyor; 13. storing the soda ash in a warehouse; 14. a second tail gas washing circulating pump; 15. a washing circulation tank; 16. a first tail gas washing circulating pump; 17. a tail gas wash tower; 18. washing the tank; 19. a centrifuge; 20. a dryer; 21. a packaging machine; 22. the reactor was sparged.

Detailed Description

The technical solution of the present invention will be more clearly and completely explained by the description of the preferred embodiments of the present invention with reference to the accompanying drawings.

Examples

As shown in figure 1, the utility model discloses a system for producing sodium metabisulfite, including first reactor 5, second reactor 3, third reactor 1 and soda 102 warehouse, sulfur dioxide gas 103 loops through first reactor 5, second reactor 3 and third reactor 1 sequentially, soda 102 warehouse links to each other with alkali blending tank 8 and soda tank 10 respectively, the output of alkali blending tank 8 links to each other with the upper portion of third reactor 1, the output of the lower part of third reactor 1 links to each other with the upper portion of jet reactor 22 and second reactor 3 that are located the third reactor 1 top respectively through third circulating pump 2, the output of the lower part of second reaction links to each other with the upper portion of jet reactor 22 and first reactor 5 that are located the second reactor 3 top through second circulating pump 4, the reactor lower part is the thick liquid district, the upper portion is the mixing section, each reactor has the circulating pump that corresponds with it, the circulating pump extracts slurry containing sodium sulfite from the lower part of the reactor, the slurry and sulfur dioxide are in gas-liquid contact in the mixing section, the sodium metabisulfite slurry generated by absorbing sulfur dioxide gas 103 falls into the lower part of the reactor, residual tail gas is discharged from an exhaust port at the upper part of the reactor, the output end at the lower part of the first reactor 5 is respectively connected with a jet 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 sequentially connected with a centrifuge 19 and a dryer 20, the elutriation tank 18 is of a vertical cylinder structure in the embodiment, the volume of the elutriation tank 18 is 3-6 times of that of the first reactor 5, the discharged liquid of the first reactor 5 enters from the bottom of the elutriation tank 18 tangentially to generate turbulence effect, under the action of gravity and liquid recoil force, the coarse and fine separation and crystal concentration are realized, the high-concentration coarse, and (3) centrifugally separating the high-concentration coarse crystal slurry by using a centrifugal machine 19, wherein an airflow drying type is adopted for a drying machine 20, the air inlet temperature of the drying machine 20 is 130-160 ℃, the moisture on the surface of the crystal is evaporated to dryness, and then the solid powder is sent to a packaging machine 21 to be packaged into a bagged product 101.

As a technical optimization scheme of the utility model, as shown in figure 1 and figure 2, the gas output end on the upper portion of the first reactor 5 is connected with the injection reactor 22 on the upper portion of the second reactor 3, the gas output end on the upper portion of the second reactor 3 is connected with the injection reactor 22 on the upper portion of the third reactor 1, the gas output end on the upper portion of the third reactor 1 discharges gas out of the boundary, wherein the injection reactor 22 is provided with a discharge pipe from bottom to top in sequence, an expansion pipe, a choke, a contraction pipe and an air inlet pipe, the top of the air inlet pipe is provided with a raw material gas interface, the lower portion of the air inlet pipe is provided with a liquid interface, the contraction angle of the contraction pipe is 10-60 degrees, the expansion angle of the expansion pipe is 10-60 degrees, the discharge pipe of the injection reactor 22 extends out of the top cover of the crystallizer, the extension length is 0.5-6 m, a spray device, the air speed in the throat pipe is 10-50 m/s, and the gas sulfur dioxide reacts with the liquid sodium metabisulfite slurry and is discharged into the crystallizer through the expansion pipe and the discharge pipe.

As a technical optimization scheme of the utility model, as shown in fig. 1 and fig. 3, the first reactor 5, the second reactor 3 and the third reactor 1 are tower structures, wherein the first reactor 5, the second reactor 3 and the third reactor 1 are all internally provided with crystallizers, the top of the crystallizer is provided with a spray reactor 22, the lower part of the crystallizer is communicated with the upper part of the corresponding spray reactor 22 through a circulating pump, the top of the crystallizer is also provided with a washing mechanism, the middle lower part of the washing mechanism is provided with a defoaming device, and a washing water interface is also arranged above the defoaming device, the top of the washing mechanism is a discharge port of reaction tail gas, the discharge port of the reaction tail gas of the washing mechanism is connected with the top of the next-stage spray reactor 22, the upper part of the crystallizer is provided with a raw material liquid interface for receiving corresponding circulating pump to transport crystal slurry, the lower part of the crystallizer is a shrinkage 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, the conical surface structure and the sedimentation tube form a crystal discharge section, and the crystallizer is used for reacting.

As a technical optimization scheme of the present invention, as shown in fig. 1, a gas output end of the drying machine 20 is connected to the tail gas washing tower 17, and the tail gas washing tower 17 washes the tail gas discharged from the drying machine 20 to remove sulfur dioxide in the tail gas; the output of lye tank 10 bottom passes through lye pump 11 and links to each other with washing circulation tank 15, the output of washing circulation tank 15 bottom passes through second tail gas washing circulating pump 14 and links to each other with tail gas washing tower 17, the output of upper portion links to each other with washing circulation tank 15 in the tail gas washing tower 17, the output of tail gas washing tower 17 bottom passes through first tail gas washing circulating pump 16 and links to each other with tail gas washing tower 17 middle part and join in marriage alkaline vat 8 respectively, through lye washing, sulfur dioxide concentration in the tail gas is to discharging below 10ppm, the washing liquid that the washing produced is sent to and is joined in marriage alkaline vat 8 and recycle.

As a technical optimization scheme of the utility model, as shown in fig. 1, the elutriation tank 18 and join in marriage between the alkali groove 8, centrifuge 19 and join in marriage between the alkali groove 8 and all be connected with the pipeline that is used for transporting tiny crystal and centrifugal mother liquor, elutriation tank 18 upper portion exhaust tiny crystal and centrifuge 19 exhaust centrifugal mother liquor all can enter into through the pipeline and join in marriage in the alkali groove 8 and reuse.

As a technical optimization scheme of the present invention, as shown in fig. 1, a first soda 102 conveyor and a second soda 102 conveyor are respectively disposed on the pipelines connecting the soda tank 8 and the soda tank 10 in the soda 102 storage bin, so that the first soda 102 conveyor and the second soda 102 conveyor can respectively convey the soda 102 for the soda tank 8 and the soda tank 10.

The utility model provides a system's work flow of production sodium metabisulfite as follows:

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 103 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 1, and 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 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(8) and are reacted with sodium carbonate 102 to be converted into slurry containing sodium sulfite crystals; the high-quality crystal centrifuged is sent to a dryer 20 for drying;

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 a bagged product 101;

4. mixing soda, namely discharging the soda 102 to a soda 102 tank for storage, quantitatively feeding the soda 102 to a soda mixing tank 8, reacting the soda in the soda mixing tank 8 with centrifugal mother liquor, liquid discharged from an elutriation tank 18 and tail gas washing liquid, defoaming and degassing, and then sending 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 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 8 for reuse.

The above detailed description merely describes the preferred embodiments of the present invention and does not limit the scope of the present invention. Without departing from the design concept and spirit scope of the present invention, the ordinary skilled in the art should belong to the protection scope of the present invention according to the present invention provides the text description and drawings to the various modifications, replacements and improvements made by the technical solution of the present invention. The scope of protection of the present invention is determined by the claims.

Claims

1. A system for producing sodium metabisulfite is characterized by comprising a first reactor, a second reactor, a third reactor and a soda storage bin, wherein gas containing sulfur dioxide sequentially passes through the first reactor, the second reactor and the third reactor, the soda storage bin is respectively connected with a soda blending tank and a soda tank, the output end of the soda blending tank is connected with the upper part of the third reactor, the output end of the lower part of the third reactor is respectively connected with a jet reactor positioned at the top of the third reactor and the upper part of the second reactor through a third circulating pump, the output end of the lower part of the second reactor is 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 the jet reactor positioned at the top of the first reactor and a washing tank through the first circulating pump, the elutriation tank is connected with the centrifugal machine and the drying machine in sequence.

2. The system for producing sodium metabisulfite of claim 1 wherein the gas outlet of the upper portion of the first reactor is connected to a sparge reactor located in the upper portion of the second reactor, and the gas outlet of the upper portion of the second reactor is connected to a sparge reactor located in the upper portion of the third reactor, and the gas outlet of the upper portion of the third reactor exhausts the gas to the outside.

3. The system for producing sodium metabisulfite according to claim 2, wherein the first reactor, the second reactor and the third reactor are all tower-type structures, wherein crystallizers are arranged inside the first reactor, the second reactor and the third reactor, a spray reactor is arranged on the top of the crystallizers, the lower portion of each crystallizer is communicated with the upper portion of the corresponding spray reactor through a circulating pump, a washing mechanism is further arranged on the top of each crystallizer, the washing mechanism is connected with the top of the next spray reactor, and a raw material liquid interface for receiving the corresponding circulating pump to transport crystal slurry is arranged on the upper portion of each crystallizer.

4. The system for producing sodium metabisulfite of claim 1, wherein the gas output of the dryer is connected to a tail gas scrubber; the output end of the bottom of the lye tank is connected with the washing circulating tank through a lye pump, and the output end of the bottom of the washing circulating tank is connected with the tail gas washing tower through a second tail gas washing circulating pump; the output of upper portion links to each other with the washing circulation groove in the tail gas washing tower, the output of tail gas washing tower bottom links to each other with tail gas washing tower middle part and join in marriage alkaline groove respectively through first tail gas washing circulating pump.

5. The system for producing sodium metabisulfite of claim 1, wherein a pipeline for transporting fine crystals and a mother liquor of centrifugation is connected between the elutriation tank and the alkali-blending tank and between the centrifuge and the alkali-blending tank.

6. The system for producing sodium metabisulfite of claim 1, wherein the pipelines connecting the soda storage bin with the soda blending tank and the soda tank are respectively provided with a first soda conveyor and a second soda conveyor.

7. The system for producing sodium metabisulfite of claim 3, wherein the lower part of the crystallizer is a contracting conical structure, the contracting angle is 60-100 degrees, the lower part of the conical structure is connected with a settling tube, and the conical structure and the settling tube form a crystal discharge section.

8. The system for producing sodium metabisulfite according to claim 3, wherein the injection reactor is provided with a discharge pipe, an expansion pipe, a throat pipe, a contraction pipe and an air inlet pipe in sequence from bottom to top, the top of the air inlet pipe is provided with a raw material gas connector, the lower part of the air inlet pipe is provided with a liquid connector, the contraction angle of the contraction pipe is 10-60 degrees, the expansion angle of the expansion pipe is 10-60 degrees, the discharge pipe of the injection reactor extends out of the top cover of the crystallizer, and the extension length of the discharge pipe is 0.5-6 m.

9. The system for producing sodium metabisulfite according to claim 3, wherein a defoaming device is arranged at the middle lower part of the washing mechanism, a flushing water port is further arranged above the defoaming device, and the top of the washing mechanism is a discharge port of reaction tail gas.