CN217732690U - Retrieve gaseous device of different concentration SO2 in follow waste liquid - Google Patents
Retrieve gaseous device of different concentration SO2 in follow waste liquid Download PDFInfo
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Abstract
The utility model discloses a retrieve different concentration SO from waste liquid 2 The gas device comprises a plurality of aeration tanks, a sulfur dioxide stripping tower and an external circulation device, wherein the sulfur dioxide stripping tower comprises a stripping tower tank body, and the lower part of the stripping tower tank body is provided with a nitrogen inlet; the top of the blow-off tower body is provided with a Venturi reactor, the aeration tank is connected with the sulfur dioxide blow-off tower through the Venturi reactor, and the outer side of the sulfur dioxide blow-off tower is connected with an external circulating device; the blow-off tower tank body is internally provided with a first layer of filler and a second layer of filler from top to bottom, the first layer of filler and the second layer of filler are arranged in parallel up and down, and the blow-off tower tank body is divided by the first layer of filler and the second layer of fillerThe device comprises an upper tank body, a middle tank body and a lower tank body, wherein a second-stage reaction circulating pump is arranged outside the stripping tower tank body, an inlet of the second-stage reaction circulating pump is connected with the lower tank body, and an outlet of the second-stage reaction circulating pump is connected with the middle tank body.
Description
Technical Field
The utility model relates to a resource chemical utilization technical field, concretely relates to sulfur dioxide of the different concentrations of preparation of spent acid and waste salt especially relates to a retrieve different from the waste liquidConcentration of SO 2 And (3) a gas device.
Background
In the production process of waste sodium sulfite in many industries, for example 3000 tons of 2-naphthol is produced every year, more than 500 tons of sodium sulfite are produced every year, and improper treatment can pollute water sources because of complex components, high COD and high chroma. And therefore can only be disposed of as hazardous waste. Similarly, the waste sulfuric acid generated in the titanium dioxide industry, the nonferrous metal industry, the steel and metal pickling industry and the like in China every year is in the level of thousands of tons; the chlor-alkali industry and the metal pickling industry can also generate a large amount of waste hydrochloric acid. The current common treatment mode for the waste acid is neutralization and precipitation treatment, the pH of the acid liquor is neutralized to 6-9 by using alkaline substances, and the precipitate is discharged in the form of sludge. The method not only needs to add extra alkaline substances, but also causes secondary pollution due to improper treatment of sludge and the like.
Therefore, it is particularly critical to develop a method and a device for treating solid wastes with high efficiency and recycling the solid wastes.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a retrieve different concentration SO from the waste liquid 2 The device can efficiently treat hazardous waste, does not need to additionally input alkaline substances in the treatment of waste sodium sulfite and waste acid, and does not cause secondary pollution in the treatment of sludge and the like; meanwhile, the method can treat waste sodium sulfite and waste acid, can recycle the waste sodium sulfite and the waste acid, and can generate SO with different concentrations 2 A gas.
In order to solve the technical problem, the utility model discloses a technical scheme is: the method can recover SO with different concentrations from waste liquid 2 The device for the gas comprises a plurality of aeration tanks, a sulfur dioxide stripping tower and an external circulation device, wherein the sulfur dioxide stripping tower comprises a stripping tower tank body, and the lower part of the stripping tower tank body is provided with a nitrogen inlet; the top of the stripping tower tank body is provided with a Venturi reactor, the aeration tank is connected with the sulfur dioxide stripping tower through the Venturi reactor, and the outer side of the sulfur dioxide stripping tower is connected with an external circulation device.
By usingAbove-mentioned technical scheme, the main raw materials that use are strong acid or medium-strong acid such as industry waste sodium sulfite and waste sulfuric acid, respectively in sodium sulfite aeration tank and the abundant aeration of sulfuric acid aeration tank before the use, detach the dissolved gas who smugglies secretly in the solution, guarantee product sulfur dioxide's purity, carry out abundant aeration back through the aeration tank, rethread sulfur dioxide blows off the tower and reacts, rethread external circulation device sprays the circulating fluid to sulfur dioxide in the tower that blows off, nitrogen inlet of rethread sulfur dioxide blows off the lower part of tower blows in to the inside of the tower that blows in nitrogen gas with the dissolved SO of solution in the tower jar body 2 Blowing out, and simultaneously controlling the concentration of sulfur dioxide by adjusting the flow of nitrogen SO as to obtain SO with different concentrations 2 A gas. Wherein the concentration of the waste sodium sulfate is required to be more than 4 percent, and the waste acid can be waste sulfuric acid or other strong acid or medium strong acid; the SO with different concentrations is recovered from the waste liquid 2 The gas device can fully mix the reaction liquid and react to release SO with different concentrations 2 A gas.
As the utility model discloses a preferred technical scheme, blow off the internal first layer of packing and the second floor of being equipped with down from last of tower tank, the first layer pack with parallel arrangement about the second floor packs, blow off the tower tank body and pack through the first layer and divide into the upper portion jar body, the middle part jar body and the lower part jar body with the second floor, the outside of the tower tank body that blows off is equipped with the second grade reaction circulating pump, the import of second grade reaction circulating pump with the lower part jar body is connected, just the export of second grade reaction circulating pump with the middle part jar body is connected, makes the second grade reaction circulating pump is followed blow off the bottom of the tower tank body to pump income solution is used for spraying in the middle part jar body, simultaneously the second grade reaction circulating pump still is connected with the outer pipeline of sodium sulfate solution, the nitrogen gas entry is established the side of the lower part jar body. The first layer of filler and the second layer of filler are both non-metallic fillers; a nitrogen inlet is arranged at the lower part of the tank body and is used for introducing nitrogen into the stripping tower to dissolve SO in the solution 2 Blowing out, and simultaneously controlling the concentration of sulfur dioxide by adjusting the flow of nitrogen.
As the utility model discloses a preferred technical scheme, the aeration tank includes sodium sulfite aeration tank and sulphuric acid aeration tank, sodium sulfite aeration tank and sulphuric acid aeration tank respectively with the upper portion of venturi reactor is connected, just the top of sodium sulfite aeration tank and sulphuric acid aeration tank all is equipped with waste liquid entry and impurity gas export, the bottom of sodium sulfite aeration tank and sulphuric acid aeration tank all is equipped with gas inlet.
As an optimal technical scheme of the utility model, outer circulating device includes one-level reaction circulation jar and one-level reaction circulating pump, the middle part jar of body with the entry of one-level reaction circulation jar is connected, the outside of one-level reaction circulation jar is equipped with one-level reaction circulating pump, between the export of one-level reaction circulating pump with the lower part jar of body is connected.
As the utility model discloses an optimized technical scheme, between the export of one-level reaction circulating pump through the heat exchanger with the upper portion jar body is connected, utilizes the heat exchanger takes away the reaction heat, makes and should retrieve different concentration SO from the waste liquid 2 The gas device is kept at a constant temperature, namely the reaction temperature is kept between 35 and 45 ℃. The reaction effect is best when the reaction temperature is between 35 and 45 ℃. The heat exchanger type may be a plate heat exchanger or a tube and tube heat exchanger.
As the preferred technical proposal of the utility model, a liquid collector is arranged in the middle tank body, so that the primary circulating liquid flows back to the primary reaction circulating tank from the middle tank body; and a nitrogen inlet is formed in the lower tank body. The liquid collector is arranged in the stripping tower tank body and aims to enable the primary circulating liquid to flow back to the primary reaction circulating tank.
As the utility model discloses an optimized technical scheme, the top of the stripping tower jar body still is equipped with the third layer and packs, the SO after the processing 2 Gas passes through the third layer of filler and then passes through SO 2 And discharging from an outlet. The third layer of filler is non-metallic filler.
As an optimized technical scheme of the utility model, SO 2 The outlet is connected with a cooling and drying machine. Making the discharged SO after the reaction 2 The gas is further cooled by the cooling dryer, and the temperature is reduced to about 0-10 ℃, so that the purposes of dehydration and purification are achieved. Blow-offThe outlet of the tower is provided with a cooling and drying machine which can be used for cooling SO 2 Cooling, dehumidifying and purifying.
As the preferred technical scheme of the utility model, the molar ratio of the waste sodium sulfite to the waste sulfuric acid is 1.1-1; and the ratio of the solution circulation amount of the first-stage reaction circulating pump to the sum of the addition amounts of the waste sodium sulfite and the waste sulfuric acid is 50 to 1; the ratio of the solution circulation volume of the second-stage reaction circulating pump to the solution circulation volume of the first-stage reaction circulating pump is 1.
The technical problem to be solved by the utility model is to provide a method for recovering SO with different concentrations from waste liquid 2 Method of gas recovery from waste streams of different concentrations of SO 2 The gas method can efficiently treat the hazardous waste, and no alkaline substance is additionally added in the treatment of the waste sodium sulfite and the waste acid, so that secondary pollution can not be caused by the treatment of sludge and the like; meanwhile, the method not only can treat the waste sodium sulfite and the waste acid, but also can utilize the waste sodium sulfite and the waste acid as resources to generate SO with different concentrations 2 A gas.
In order to solve the technical problem, the utility model discloses a technical scheme is: the SO with different concentrations is recovered from the waste liquid 2 The gas preparation method specifically comprises the following steps:
s1: respectively fully aerating waste sodium sulfite gas in a sodium sulfite aeration tank and waste sulfuric acid in a sulfuric acid aeration tank, and then mixing the waste sodium sulfite gas and the waste sulfuric acid in a Venturi reactor;
s2: the mixed waste sodium sulfite gas and waste sulfuric acid enter a stripping tower tank body, a sodium sulfate solution generated by the reaction of the waste sodium sulfite and the waste sulfuric acid is used as a reaction medium, and the sodium sulfate solution is respectively sprayed on a first layer of filler and a second layer of filler by a first-stage reaction circulating pump and a second-stage reaction circulating pump;
s3: blowing nitrogen into the interior of the blow-off tower tank body to dissolve SO in the solution 2 And blowing off, discharging from the top of the upper tank body, and controlling the concentration of sulfur dioxide by adjusting the flow of nitrogen.
Compared with the prior art, the utility model has the following advantage: the method can recover SO with different concentrations from waste liquid 2 Complete use of waste sulfurous acid in gas deviceSodium and waste acid, in the process of treating hazardous waste, sulfur dioxide gas with different concentrations can be prepared; the sulfur dioxide stripping tower of the utility model can strip sulfur dioxide from the solution, thereby improving the yield of sulfur dioxide; the whole preparation method does not need additional raw materials, has simple and convenient method, and recovers SO with different concentrations from waste liquid 2 The gas device has the characteristics of low cost and small investment. The method and the device have the absolute advantages of waste recycling, high input-output ratio and capability of producing sulfur dioxide with different concentrations.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings and examples.
FIG. 1 shows the recovery of SO of different concentrations from waste liquid 2 A structure diagram of a gas device;
wherein, the 1-sodium sulfite aeration tank; 2-sulfuric acid aeration tank; 3-a sulfur dioxide stripping tower; 301-secondary reaction circulation pump; 3021 — first layer of filler; 3022-second layer of filler; 3023-third layer of filler; 303-a liquid trap; 304-a venturi reactor; 305-a stripping tower tank body; 4-first-stage reaction circulating tank; 401-first order reaction circulation pump; 5-a heat exchanger; 6-a cold dryer.
Detailed Description
In order to deepen the understanding of the present invention, the present invention will be described in further detail with reference to the accompanying drawings and embodiments, which are only used for explaining the present invention and are not limited to the protection scope of the present invention.
Example (b): the SO with different concentrations is recovered from the waste liquid 2 The gas device comprises a plurality of aeration tanks, a sulfur dioxide stripping tower 3 and an external circulation device, wherein the sulfur dioxide stripping tower 3 comprises a stripping tower tank body 305, and the lower part of the stripping tower tank body 305 is provided with a nitrogen inlet; a venturi reactor 304 is arranged at the top of the stripping tower tank body 305, the aeration tank is connected with the sulfur dioxide stripping tower 3 through the venturi reactor 304, and an external circulating device is connected to the outer side of the sulfur dioxide stripping tower 3; the inside of the stripping tower tank body 305 is provided with a material from top to bottomA first layer of filler 3021 and a second layer of filler 3022, wherein the first layer of filler 3021 and the second layer of filler 3022 are arranged in parallel from top to bottom, the blowdown tower tank body 305 is divided into an upper tank body, a middle tank body and a lower tank body by the first layer of filler 3021 and the second layer of filler 3022, a second-stage reaction circulating pump 301 is arranged outside the blowdown tower tank body 305, an inlet of the second-stage reaction circulating pump 301 is connected to the lower tank body, and an outlet of the second-stage reaction circulating pump 301 is connected to the middle tank body, so that the second-stage reaction circulating pump 301 pumps a solution from the bottom of the blowdown tower tank body 305 into the middle tank body for spraying, meanwhile, the second-stage reaction circulating pump 301 is further connected to a sodium sulfate solution discharge pipeline, and a nitrogen inlet is arranged on the side surface of the lower tank body; the first layer of filler 3021 and the second layer of filler 3022 are both non-metallic fillers; the aeration tank comprises a sodium sulfite aeration tank 1 and a sulfuric acid aeration tank 2, the sodium sulfite aeration tank 1 and the sulfuric acid aeration tank 2 are respectively connected with the upper part of the venturi reactor 304, and the tops of the sodium sulfite aeration tank 1 and the sulfuric acid aeration tank 2 are both provided with a waste liquid inlet and an impurity gas outlet, namely the top of the sodium sulfite aeration tank 1 is provided with a waste sodium sulfite inlet and an impurity gas outlet, and the top of the sulfuric acid aeration tank 2 is provided with a waste sulfuric acid inlet and an impurity gas outlet; gas inlets are formed in the bottoms of the sodium sulfite aeration tank 1 and the sulfuric acid aeration tank 2, namely nitrogen is introduced into the bottom of the sodium sulfite aeration tank 1 through the gas inlets, and air or nitrogen is introduced into the bottom of the sulfuric acid aeration tank 2 through the gas inlets; the external circulation device comprises a first-stage reaction circulation tank 4 and a first-stage reaction circulation pump 401, the middle tank body is connected with an inlet of the first-stage reaction circulation tank 4, the first-stage reaction circulation pump 401 is arranged on the outer side of the first-stage reaction circulation tank 4, and an outlet of the first-stage reaction circulation pump 401 is connected with the lower tank body; the outlet of the first-stage reaction circulating pump 401 is connected with the upper tank body through a heat exchanger 5, and reaction heat is taken away by the heat exchanger 5, SO that SO with different concentrations is recovered from waste liquid 2 The gas device keeps constant temperature, namely keeps the reaction temperature between 35 and 45 ℃; the reaction effect is best when the reaction temperature is between 35 and 45 DEG C(ii) a The heat exchanger 5 may be of the plate heat exchanger or tube and tube heat exchanger type; a liquid collector 303 is arranged in the middle tank body, so that the primary circulating liquid flows back to the primary reaction circulating tank 4 from the middle tank body; a nitrogen inlet is formed in the lower tank body; the liquid collector 303 is arranged inside the tank body 305 of the stripping tower, and aims to enable the primary circulating liquid to flow back to the primary reaction circulating tank 4; the top of the blow-off tower body 305 is also provided with a third layer of filler 3023, and the treated SO 2 The gas passes through the third layer of packing 3023 and then passes through SO 2 Discharging through an outlet; the third layer of filler 3023 is a non-metallic filler; the SO 2 The outlet is connected with a cooling drier 6, SO that the discharged SO after the reaction 2 The gas is further cooled by the cooling dryer 6, and the temperature is reduced to about 0-10 ℃, so that the aim of dehydration and purification is fulfilled; the outlet of the sulfur dioxide stripping tower 3 is provided with a cooling and drying machine 6 which can cool SO 2 Cooling, dehumidifying and purifying; the molar ratio of the waste sodium sulfite to the waste sulfuric acid is 1.1-1; and the ratio of the solution circulation amount of the first-stage reaction circulating pump 401 to the sum of the addition amounts of the waste sodium sulfite and the waste sulfuric acid is 50 to 1; the ratio of the solution circulation volume of the secondary reaction circulation pump 301 to the solution circulation volume of the primary reaction circulation pump is 1.
The method can recover SO with different concentrations from waste liquid 2 The gas preparation method specifically comprises the following steps:
s1: after fully aerating the waste sodium sulfite gas in a sodium sulfite aeration tank 1 and the waste sulfuric acid in a sulfuric acid aeration tank 2, respectively, the waste sodium sulfite gas and the waste sulfuric acid enter a Venturi reactor 304 to be mixed;
s2: the mixed waste sodium sulfite gas and waste sulfuric acid enter a stripping tower tank body 305, sodium sulfate solution generated by the reaction of the waste sodium sulfite and the waste sulfuric acid is taken as a reaction medium, and the sodium sulfate solution is respectively sprayed on a first layer of filler 3021 and a second layer of filler 3022 through a first-stage reaction circulating pump 401 and a second-stage reaction circulating pump 301;
s3: the SO dissolved in the solution is then removed by blowing nitrogen into the interior of the blow-off column tank 305 2 And blowing off, discharging from the top of the upper tank body, and controlling the concentration of sulfur dioxide by adjusting the flow of nitrogen.
The specific embodiment is as follows: recovery of SO of different concentrations from waste liquor using the above-described examples 2 The gas device and the method use 17% sodium sulfite solution, the solution also contains 1-sodium naphthalene sulfonate, 2-sodium naphthalene sulfonate, 1-naphthol and 2-naphthol, and other impurities, belonging to high salt, high COD and high chroma chemical wastewater. The waste acid is sulfuric acid pickling waste liquor in the steel industry, the content of sulfuric acid is 14%, and ferrous sulfate and heavy metal ions such as nickel, cadmium and the like are also contained in the waste acid. Respectively filling the waste sodium sulfite solution and the waste sulfuric acid solution into a sodium sulfite aeration tank 1 and a sulfuric acid aeration tank 2, and removing volatile components in the waste sodium sulfite solution and the waste sulfuric acid solution after full aeration by using nitrogen; the mixture is injected into a venturi reactor 304 according to the volume ratio of 1.3, a solution with enough liquid level is supplemented in advance in a stripping tower 3 and a primary reaction circulating tank 4, a primary reaction circulating pump 401 and a secondary reaction circulating pump 301 are started, and the pump flow rates are respectively 150m 3 H and 200m 3 The reaction liquid is sprayed on the first layer of filler 3021 (non-metallic filler), the temperature of the reaction liquid in the system is controlled between 35 ℃ and 40 ℃ through the heat exchanger 5, and the SO removed by blowing 2 The temperature of the gas is reduced to 5-8 ℃ through a cold dryer 6, the concentration of the obtained sulfur dioxide is 45%, and the rest components are nitrogen.
For those skilled in the art, the specific embodiments are only exemplary descriptions of the present invention, and it is obvious that the present invention is not limited to the above-mentioned embodiments, and various insubstantial modifications can be made without modification to the method concept and technical solution of the present invention, and the present invention is also within the scope of the present invention.
Claims (8)
1. Recovering SO with different concentrations from waste liquid 2 The device for the gas is characterized by comprising a plurality of aeration tanks, a sulfur dioxide stripping tower and an external circulation device, wherein the sulfur dioxide stripping tower comprises a stripping tower tank body, and the lower part of the stripping tower tank body is provided with a nitrogen inlet; the top of the stripping tower tank body is provided with a Venturi reactor, the aeration tank is connected with the sulfur dioxide stripping tower through the Venturi reactor,and the outer side of the sulfur dioxide stripping tower is connected with an external circulating device.
2. Recovery of different concentrations of SO from waste streams as claimed in claim 1 2 The device for the gas is characterized in that a first layer of filler and a second layer of filler are arranged in a stripping tower tank body from top to bottom, the first layer of filler and the second layer of filler are arranged in parallel up and down, the stripping tower tank body is divided into an upper tank body, a middle tank body and a lower tank body through the first layer of filler and the second layer of filler, a secondary reaction circulating pump is arranged outside the stripping tower tank body, an inlet of the secondary reaction circulating pump is connected with the lower tank body, an outlet of the secondary reaction circulating pump is connected with the middle tank body, so that the secondary reaction circulating pump pumps the solution from the bottom of the stripping tower tank body into the middle tank body for spraying, and meanwhile, the secondary reaction circulating pump is also connected with a sodium sulfate solution discharge pipeline; the nitrogen inlet is formed in the side face of the lower tank body.
3. Recovery of SO of different concentrations from waste streams according to claim 1 2 Gaseous device, its characterized in that, the aeration tank includes sodium sulfite aeration tank and sulphuric acid aeration tank, sodium sulfite aeration tank and sulphuric acid aeration tank respectively with the upper portion of venturi reactor is connected, just the top of sodium sulfite aeration tank and sulphuric acid aeration tank all is equipped with waste liquid entry and foreign gas export, the bottom of sodium sulfite aeration tank and sulphuric acid aeration tank all is equipped with gas inlet.
4. Recovery of SO of different concentrations from waste liquors as claimed in claim 2 2 The gas device is characterized in that the outer circulating device comprises a first-stage reaction circulating tank and a first-stage reaction circulating pump, the middle tank body is connected with an inlet of the first-stage reaction circulating tank, the first-stage reaction circulating pump is arranged on the outer side of the first-stage reaction circulating tank, and an outlet of the first-stage reaction circulating pump is connected with the lower tank body.
5. Recovery of SO of different concentrations from waste streams according to claim 4 2 The gas device is characterized in that the outlet of the primary reaction circulating pump is connected with the upper tank body through a heat exchanger.
6. Recovery of SO of different concentrations from waste streams according to claim 4 2 The gas device is characterized in that a liquid collector is arranged in the middle tank body, so that primary circulating liquid flows back to the primary reaction circulating tank from the middle tank body.
7. Recovery of SO of varying concentration from waste streams as claimed in claim 3 2 The gas device is characterized in that the top of the blow-off tower tank body is also provided with a third layer of filler, and the treated SO 2 Gas passes through the third layer of filler and then passes through SO 2 And discharging from an outlet.
8. Recovery of SO of different concentrations from waste streams according to claim 7 2 Apparatus for gases, characterized in that said SO 2 The outlet is connected with a cooling and drying machine.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115159469A (en) * | 2022-06-29 | 2022-10-11 | 江苏德义通环保科技有限公司 | Recovering SO with different concentrations from waste liquid 2 Apparatus and method for gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115159469A (en) * | 2022-06-29 | 2022-10-11 | 江苏德义通环保科技有限公司 | Recovering SO with different concentrations from waste liquid 2 Apparatus and method for gas |
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