CN215288069U - System for SRG washing wastewater catalytic desalination - Google Patents
System for SRG washing wastewater catalytic desalination Download PDFInfo
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Abstract
The utility model discloses a system for SRG washing wastewater catalysis desalination. The system comprises a wastewater conveying device, a carbon-liquid separation tank, a sedimentation adsorption tank, a catalytic disproportionation tank and a colloid destabilizing tank. And the wastewater conveying device is communicated with a feed inlet of the carbon-liquid separation tank. The carbon-liquid separation tank, the sedimentation adsorption tank, the catalytic disproportionation tank and the colloid destabilizing tank are sequentially connected in series. The utility model discloses simple structure, easy operation, when handling waste water, recoverable sulphur realizes the resourceful treatment of waste water, and no secondary pollution produces.
Description
Technical Field
The utility model relates to a SRG washing wastewater treatment technique, concretely relates to system of SRG washing wastewater catalysis desalination belongs to SRG flue gas washing wastewater treatment and sulphur resource recovery technical field.
Background
Sintering flue gas in the steel industry is subjected to a flue gas purification process by adopting an activated carbon method for desulfurization and denitrification, and sulfur dioxide gas collected by activated carbon is concentrated and released and then is sent to a sulfur resource workshop to produce sulfur resources. The flue gas enriched with sulfur dioxide gas is called sulfur-enriched gas (SRG flue gas) for short, and the gas can be processed by the procedures of purification, drying, conversion, absorption and the like to prepare sulfur resources meeting the national standard, and the resource recovery value is high. But the purification process in the process of producing sulfur resources can simultaneously wash impurities and harmful elements in the flue gas and enter the acidic washing wastewater, and meanwhile, part of sulfur dioxide gas in the flue gas can also be absorbed by water vapor and brought into the wastewater.
Generally, because the acidic material is greater than the alkaline material in the SRG gas, the SRG flue gas scrubbing wastewater tends to be acidic. When cyanide and derivatives thereof exist in the front-end flue gas, the cyanide and the derivatives thereof enter the SRG gas and are finally dissolved in the acidic washing wastewater, so that the alkalinity of the wastewater is increased (for example, cyanic acid is hydrolyzed to generate ammonia nitrogen), and the acidic washing wastewater is neutral. The acidic washing wastewater is neutral, SO a large amount of SO in SRG gas can be caused2The acid gas dissolves, causing a sharp increase in the hydrogen sulfite in the wastewater. The detection result shows that the concentration of the hydrogen sulfite in the acidic washing wastewater generated by the cyanide-free SRG gas washing is 2-5 g/L, and the concentration of the hydrogen sulfite in the acidic washing wastewater generated by the cyanide-containing SRG gas washing is 240-300 g/L. If the acidic washing wastewater containing bisulfite with high concentration enters a subsequent wastewater treatment system, the treatment difficulty is huge. One side ofThe alkali consumption is increased rapidly due to the surface, so that the liquid alkali is wasted and the waste water discharge amount is increased; in addition, during the process of adding alkali, sodium sulfite salt is formed and crystallized and precipitated, which causes system blockage and paralysis.
Sulfur is an oxygen group simple substance non-metallic solid, is an important chemical raw material, and is widely used for producing various chemical products, gunpowder, matches, pigments and medicinal products. Powdered sulfur is used agriculturally as an insecticide and fungicide. The sulfur is mainly extracted from natural sulfur ore deposit and recovered from natural gas, coal gas and industrial waste gas. With the expansion of sulfur demand, the recovery of sulfur from waste gases or waste water is becoming an increasingly important source of sulfur.
The liquid phase disproportionation process for preparing sulfur is characterized by that it utilizes the characteristic of sulfur element in bisulfite as intermediate valence state, and makes it produce disproportionation under the condition of high temp. and catalyst so as to implement recovery of elemental sulfur. Aiming at the defect that the blockage is caused by the crystallization of a wastewater system caused by directly adding alkali due to the higher concentration of the bisulfite in the wastewater. The use of "acid stripping" and "precipitation" methods has been reported earlier, but these methods have more or less drawbacks. The method specifically comprises the following steps:
an acidification stripping method: the bisulfite can be changed into sulfur dioxide to escape under the acidic condition, thereby realizing the reduction of the concentration of the bisulfite. The reactions involved are: HSO3 -+H+→H2SO3；H2SO3+ air → H2O+SO2×) @. However, this method requires the addition of an acid solution, which increases the total water content and increases the amount of acid solution added. In addition, the method utilizes strong acid to prepare weak acid, and the total salt content can be reduced by only 50% at most.
A precipitation method: the sulfate is removed by utilizing the property that the bisulfite and the metal cation form sulfate, such as calcium oxide, magnesium oxide, ferrous sulfate, ferric chloride, ferrous chloride, ferric nitrate and ferrous nitrate. The reactions involved are: SO (SO)3 2-+ precipitant M → MSO3↓. The process produces a large amount of solid slag and the metal salts are generally expensive.
A disproportionation method: as inNational patent documents 201210391355.9, 201210392392.1, 201711078170.1. Based on the property that bisulfite can disproportionate to elemental sulfur and sulfate, a reduction in 1/3 bisulfite is achieved without consuming added species. The reaction involved is: 3HSO3 -→S+2SO4 2-+H++H2And O. The temperature of the direct reaction is > 160 ℃. The addition of the catalyst can reduce the reaction temperature: if selenium is added, the reaction temperature can be reduced to 80-100 ℃; adding iodine and under the action of photocatalysis, the reaction can be carried out at normal temperature. But selenium and iodine are expensive and thus have no possibility of industrial application. Among the above methods, the disproportionation method has advantages of no additional consumption of substances, no increase in water amount, and the like. Disproportionation of the bisulfite by catalytic methods for sulfur recovery is a low cost process of operation. However, the process has not been widely popularized due to the high price of the catalyst. Therefore, the method for using the low-cost and high-efficiency bisulfite disproportionation catalyst for recycling the SRG washing wastewater is of great significance.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model provides a system for the catalytic desalination of SRG washing wastewater and a catalytic desalination method thereof. Active carbon powder contained in SRG washing wastewater is used as a carrier, thiosulfate ions contained in the SRG washing wastewater are used as a sulfur source, and sedimentation adsorption is carried out at normal temperature and normal pressure to obtain the sulfur-containing active carbon. Then sulfur-containing activated carbon is used as a catalyst, and the disproportionation reaction of high-concentration hydrogen sulfite ions can be realized at a lower temperature (about 50 ℃) to recover and obtain sulfur resources. On one hand, the content of salt in the SRG washing wastewater is reduced, and on the other hand, the purpose of recycling sulfur is realized; the liquid caustic soda consumption is greatly reduced, and through a comparison test, the liquid caustic soda consumption can be reduced by about 60%. The sulfur-containing activated carbon used by the utility model has the advantages of simple preparation process, easily obtained raw materials, low price, large-scale application prospect and recyclable prepared sulfur-containing activated carbon. Furthermore, the utility model discloses when handling waste water, recoverable sulphur realizes the resourceful treatment of waste water, and no secondary pollution produces. Therefore, the sulfur-containing activated carbon is used as a catalyst for the disproportionation and desulfurization reaction of the hydrogen sulfite ions in the SRG washing wastewater, and has wide market prospect and economic benefit.
In order to achieve the above object, the present invention adopts the following technical solutions:
according to a first embodiment of the present invention, a method for catalytic desalination of SRG washing wastewater is provided.
A system for catalytic desalting of SRG washing wastewater comprises a wastewater conveying device, a carbon-liquid separation tank, a sedimentation adsorption tank, a catalytic disproportionation tank and a colloid destabilization tank. And the wastewater conveying device is communicated with a feed inlet of the carbon-liquid separation tank. The carbon-liquid separation tank, the sedimentation adsorption tank, the catalytic disproportionation tank and the colloid destabilizing tank are sequentially connected in series.
Preferably, the system also comprises an acidification treatment tank which is positioned between the carbon liquid separation tank and the sedimentation adsorption tank. And the water outlet of the carbon-liquid separation tank is communicated with the water inlet of the acidification tank through a first pipeline. And the water outlet of the acidification treatment pool is communicated with the water inlet of the sedimentation adsorption pool through a second pipeline. An acid liquor conveying pipeline is connected to an acid inlet of the acidification tank.
Preferably, the system further comprises an activated carbon buffer bin. The active carbon buffer bin is positioned between the carbon-liquid separation tank and the sedimentation adsorption tank. And the discharge port of the carbon-liquid separation tank is communicated with the feed port of the activated carbon buffer bin through a first material conveying device. And the discharge port of the charcoal buffer bin is communicated with the feed inlet of the sedimentation adsorption tank through a second material conveying device.
Preferably, the system further comprises a liquid mixing tank. The liquid mixing tank is positioned between the sedimentation adsorption tank and the catalytic disproportionation tank. And the water outlet of the sedimentation adsorption tank is communicated with the water inlet of the liquid mixing tank through a third pipeline. The water outlet of the carbon-liquid separation tank is also communicated with the water inlet of the liquid mixing tank through a fourth pipeline. And the water outlet of the liquid mixing tank is communicated with the water inlet of the catalytic disproportionation tank through a fifth pipeline.
Preferably, the system also comprises a sulfur-containing activated carbon cache bin. The sulfur-containing activated carbon buffer bin is positioned between the sedimentation adsorption tank and the catalytic disproportionation tank. And the discharge port of the sedimentation adsorption tank is communicated with the feed inlet of the sulfur-containing activated carbon buffer bin through a third material conveying device. And the discharge port of the sulfur-containing activated carbon buffer bin is communicated with the feed inlet of the catalytic disproportionation pool through a fourth material conveying device.
Preferably, the discharge port of the sulfur-containing activated carbon buffer bin is communicated with the feed inlet of the sedimentation adsorption tank through a fifth material conveying device.
Preferably, the system further comprises a first solid liquid separation device. The first solid-liquid separation device is positioned between the catalytic disproportionation tank and the colloid destabilizing tank. And a discharge port of the catalytic disproportionation tank is connected with a feed port of the first solid-liquid separation device through a sixth material conveying device. And the water outlet of the first solid-liquid separation device is communicated with the water inlet of the colloid destabilizing tank through a sixth pipeline.
Preferably, the discharge port of the first solid-liquid separation device is also communicated with the feed port of the catalytic disproportionation pool through a seventh material conveying device.
Preferably, the system further comprises a second solid liquid separation device. And a feed inlet of the second solid-liquid separation device is communicated with a discharge outlet of the colloid destabilizing tank through an eighth material conveying device. And a discharge port of the second solid-liquid separation device is connected with a ninth material conveying device, and a water discharge port of the second solid-liquid separation device is connected with a seventh pipeline.
Preferably, the system further comprises a sulfur drying device. And a feed inlet of the sulfur drying device is communicated with a discharge outlet of the second solid-liquid separation device through a ninth material conveying device. And a protective gas conveying pipeline is connected to the gas inlet of the sulfur drying device.
Preferably, the system further comprises a wastewater post-treatment system. And a water inlet of the wastewater post-treatment system is communicated with a water outlet of the second solid-liquid separation device through a seventh pipeline.
Preferably, the system also comprises a sulfur storage bin. The sulfur storage bin is communicated with a discharge port of the sulfur drying device through a tenth material conveying device. According to a first embodiment of the present invention, a method for catalytic desalination of SRG washing wastewater is provided.
According to a second embodiment of the present invention, there is provided a method for catalytic desalination of SRG washing wastewater using the system of the first embodiment, comprising the steps of:
1) and (3) separating activated carbon powder from the SRG washing wastewater, adding acid into part of the SRG washing wastewater for acidification, mixing the activated carbon powder and the acidified part of the SRG washing wastewater, and performing sedimentation adsorption. Finally, carrying out solid-liquid separation to obtain the sulfur-containing activated carbon and the desulfurization wastewater.
2) Uniformly mixing the desulfurization wastewater and the residual SRG washing wastewater, and then adding sulfur-containing activated carbon to perform catalytic disproportionation reaction.
3) Continuously monitoring the pH value of the reaction system in the step 2) until the pH value is changed to a pH set value. Then carrying out solid-liquid separation to obtain filtrate.
4) And (3) continuously heating the filtrate obtained in the step 3) for reaction until precipitates are generated and a relatively clear supernatant appears, and filtering to obtain sulfur and desalted SRG washing wastewater.
Preferably, in step 1), the SRG washing wastewater is a cyanide-containing SRG washing wastewater.
Preferably, in step 1), the amount of the portion of the SRG washing wastewater used is such that the numerical ratio of the molar amount of thiosulfate (moL) in the portion of the SRG washing wastewater to the weight of activated carbon (g) is 0.05-0.5:1, preferably 0.1-0.3:1, more preferably 0.15-0.25: 1.
Preferably, in step 1), the acid is one or more of hydrochloric acid, sulfuric acid, nitric acid, nitrous acid, and phosphoric acid. Preferably sulfuric acid.
Preferably, in step 2), the disproportionation reaction is carried out at a temperature of 40 to 80 ℃, preferably 45 to 70 ℃, more preferably 50 to 60 ℃. The disproportionation reaction time is 0.3-10h, preferably 0.5-8h, more preferably 0.8-5 h.
Preferably, in step 3), the pH set point is < 3, preferably the pH set point is < 2.5, more preferably the pH set point is < 2.
Preferably, in step 4), the reaction temperature of the heating reaction is 50 to 120 ℃, preferably 60 to 110 ℃, and more preferably 70 to 100 ℃.
Preferably, step 1) is specifically: the activated carbon powder in the SRG washing wastewater is separated for standby, then part of the SRG washing wastewater is taken, and acid (such as sulfuric acid) is added into the part of the SRG washing wastewater to adjust the pH value to be less than 3 (preferably the pH value to be less than 2). Then adding the activated carbon powder into the acidified SRG wastewater for sedimentation adsorption (the adsorption time is 0.3-5h, preferably 0.5-3 h). And after adsorption, carrying out solid-liquid separation to obtain solid and filtrate, and drying the obtained solid to obtain the sulfur-containing activated carbon.
Generally, the sulfur-containing activated carbon has a sulfur loading of 1.6 to 16g, preferably 3.2 to 9.6g, and more preferably 4.8 to 8g per gram of activated carbon.
Preferably, the sulfur-containing activated carbon is activated carbon after multiple times of sedimentation adsorption, preferably 2 to 10 times, and more preferably 3 to 5 times. The SRG washing wastewater used for each settling adsorption is derived from the original SRG washing wastewater.
Preferably, step 2) is specifically: uniformly mixing the filtrate obtained after the solid-liquid separation in the step 1) with the residual SRG washing wastewater. Then adding sulfur-containing activated carbon, heating to 40-80 deg.C (preferably 50-60 deg.C), carrying out disproportionation reaction for 0.3-10h (preferably 0.5-8h), and carrying out step 3 after obtaining disproportionation reaction system.
Preferably, step 3) is specifically: continuously monitoring the pH value of the disproportionation reaction system in the step 2), and filtering when the pH value of the disproportionation reaction system is lower than 3 (preferably, the pH value is lower than 2), separating out sulfur-containing activated carbon and obtaining filtrate. Returning the sulfur-containing activated carbon to the step 2) to be continuously used as the catalyst, and performing the step 4) on the filtrate.
Preferably, the step 4) is specifically: heating the filtrate obtained in step 3) to 50-120 deg.C (preferably 70-100 deg.C) to react until sulfur precipitate and clear supernatant is obtained. Then separating out sulfur precipitate, drying to obtain elemental sulfur, and discharging the supernatant after the sulfur precipitate is separated out and treated by a wastewater post-treatment system.
In the prior art, because the acidic substances in the SRG gas are more than alkalineMass, and therefore, SRG flue gas scrubbing wastewater tends to be acidic. When cyanide and derivatives thereof exist in the front-end flue gas, the cyanide and the derivatives thereof enter the SRG gas and are finally dissolved in the acidic washing wastewater, so that the alkalinity of the wastewater is increased (for example, cyanic acid is hydrolyzed to generate ammonia nitrogen), and the acidic washing wastewater is neutral. The acidic washing wastewater is neutral, SO a large amount of SO in SRG gas can be caused2The acid gas dissolves, causing a sharp increase in the hydrogen sulfite in the wastewater. The detection result shows that the concentration of the hydrogen sulfite in the acidic washing wastewater generated by the cyanide-free SRG gas washing is 2-5 g/L, and the concentration of the hydrogen sulfite in the acidic washing wastewater generated by the cyanide-containing SRG gas washing is 240-300 g/L. If the acidic washing wastewater containing bisulfite with high concentration enters a subsequent wastewater treatment system, the treatment difficulty is huge. On one hand, the alkali consumption is increased sharply, the waste of liquid alkali is caused, and the discharge amount of waste water is increased; in addition, during the process of adding alkali, sodium sulfite salt is formed and crystallized and precipitated, which causes system blockage and paralysis. The existing acidification stripping method, precipitation method and disproportionation method have the problems of low treatment efficiency and high input cost, and are not beneficial to large-scale industrial popularization and application.
At present, the sulfur is mainly extracted from natural sulfur ore deposits and recovered from natural gas, coal gas and industrial waste gas. With the expansion of sulfur demand, the recovery of sulfur from waste gases or waste water is becoming an increasingly important source of sulfur. The liquid phase disproportionation process for preparing sulfur is characterized by that it utilizes the characteristic of sulfur element in bisulfite as intermediate valence state, and makes disproportionation take place under the condition of high temperature (for example, the temp. of bisulfite directly producing disproportionation reaction is greater than 160 deg.C) and catalyst so as to implement recovery of simple substance sulfur. However, the existing catalysts such as selenium and iodine are expensive, so that the catalyst is not suitable for industrial mass production and application at present.
The utility model discloses in, to the high characteristic of the bisulfite that contains of cyanogen SRG waste water, the utility model people of this application discovers through the research, when elementary substance sulphur and active carbon coexisted, can realize the disproportionation of high concentration bisulfite under the low temperature (about 50 ℃) condition. The sulfur-containing activated carbon is used as a catalyst, so that the disproportionation reaction of high-concentration hydrogen sulfite ions is realized, and the sulfur resource is obtained. On one hand, the content of salt in the SRG washing wastewater is reduced, and on the other hand, the purpose of recycling sulfur is realized; the liquid caustic soda consumption in the subsequent wastewater treatment process is greatly reduced, and the liquid caustic soda consumption can be reduced by about 60% through a contrast test. The sulfur-containing activated carbon used by the utility model has the advantages of simple preparation process, easily obtained raw materials, low price, large-scale application prospect and recyclable prepared sulfur-containing activated carbon.
In the utility model, under the catalytic action of the sulfur-containing active carbon, hydrogen ions and sulfite ions in the SRG washing wastewater are subjected to catalytic disproportionation reaction. Namely, the bisulfite can generate disproportionation reaction under the catalysis of sulfur-containing activated carbon at the temperature of 40-80 ℃ (preferably 50-60 ℃), and S (IV) is differentiated into S (0) and S (VI). The solution pH will decrease throughout the reaction. When the pH value of the solution is reduced to be less than 3 (preferably to be less than 2), the catalyst is filtered and separated (the separated sulfur-containing catalyst can be recycled after being dried, so that the investment cost of the catalyst is greatly reduced). The remaining solution is sulphur colloid and further heating (e.g. to 50-120 c, preferably to 70-100 c) is continued to destabilize the colloid and finally form sulphur particles. Separating out sulfur particle precipitate and drying to obtain the elemental sulfur. The utility model discloses when reducing washing waste water salinity content, recoverable sulphur realizes the utilization and the processing of waste water resource, and no secondary pollution produces. The reaction process of the disproportionation of S (IV) to S (0) and S (VI) is as follows: carrying out catalytic disproportionation by taking sulfur-containing activated carbon as a catalyst:
generally, the sulfur-containing activated carbon is prepared by using high-quality activated carbon as base carbon through a special process, and is mainly used for demercuration in a demercuration device for mercury-containing gases such as natural gas/coal gas and the like. The utility model discloses in, prepare through the adsorption method and obtain the active carbon that contains sulphur, specifically do: because SRG washing wastewater contains a large amount of thiosulfate which can be subjected to acidolysis under acidic condition to release colloidal sulfur, the SRG washing wastewater is collectedPart of SRG wastewater containing thiosulfate ions is used as a sulfur source after being acidified, and activated carbon contained in SRG washing wastewater is used as an adsorption carrier (or additionally added with activated carbon). The activated carbon is mixed with the SRG washing wastewater containing thiosulfate ions after acid hydrolysis (generally, the total amount of thiosulfate ions added is larger than the amount of activated carbon, for example, the numerical ratio of the molar amount (moL) of thiosulfate to the weight (g) of activated carbon is 0.05-0.5:1, preferably 0.1-0.3:1, more preferably 0.15-0.25:1), the acid for acidification is sulfuric acid, and when the thiosulfate ions meet the acid, colloidal sulfur is released. Meanwhile, in the acidolysis process, because the solution is mixed with the activated carbon powder or the activated carbon particles, the colloidal sulfur separated out by the acidolysis of thiosulfate ions can be adsorbed into the activated carbon powder or the activated carbon particles through the adsorption effect (the sedimentation adsorption process) of the activated carbon powder or the activated carbon particles, so as to form the sulfur-containing activated carbon. The specific reaction formula is as follows: acidolysis of thiosulfate ions under acidic conditions: s2O3 2-+H+→ S (Sulfur colloid) + HSO3 -。
In the utility model, the compound process of the sulfur-containing activated carbon is as follows: s + AC → S @ AC. (AC means activated carbon). The sulfur-containing activated carbon of the utility model has the advantages of simple preparation process, low price, wide source, easy separation and recovery and long service life.
The utility model discloses in, to contain the active carbon of sulphur to add in the waste water that contains the bisulfite to carry out the catalytic disproportionation to the bisulfite ion, its reaction temperature control is about 50 ℃, after reacting a period, becomes faint yellow when the solution. And (3) filtering to separate out sulfur-containing activated carbon, and continuing to react the residual filtrate at 70-100 ℃ until sulfur precipitates are generated and clear supernatant is obtained, namely, finishing the reaction (the residual filtrate is sulfur colloid, and continuing to perform heating reaction to destabilize the colloid and form sulfur particles).
The utility model discloses in, during SRG washing waste water carried the charcoal liquid separation pond through waste water conveyor, after the charcoal liquid separation pond subsided that stews, the active carbon powder in the SRG waste water was separated out. Meanwhile, extracting part of supernatant of the carbon liquid separation tank into an acidification treatment tank, adding acid (sulfuric acid) to adjust the pH value of the wastewater in the acidification treatment tank to be less than 3 (preferably less than 2), and adding activated carbon powder (additionally adding new activated carbon powder according to working condition requirements) separated from the SRG wastewater before for sedimentation and adsorption. Separating sulfur-containing activated carbon after adsorption for later use. And the wastewater from which the sulfur-containing activated carbon is separated is conveyed to a liquid mixing tank to be mixed with the original SRG wastewater.
In the utility model, the sulfur-containing activated carbon after the adsorption through sedimentation can be directly used for catalyzing the disproportionation reaction of the bisulfite in the SRG washing wastewater. Generally, in order to make the catalytic effect of the sulfur-containing activated carbon better, the sulfur-containing activated carbon generally needs to be subjected to multiple sedimentation adsorption treatments. Namely the utility model discloses in can be provided with a plurality of sedimentation adsorption tanks simultaneously, then will contain sulphur activated carbon one by one and adsorb the processing in each sedimentation adsorption tank. The wastewater of each sedimentation adsorption tank is from original SRG washing wastewater, and the wastewater after sedimentation adsorption is also conveyed to the liquid mixing tank to be mixed with the rest SRG washing wastewater. (the remaining portion of the SRG wash wastewater refers to the original SRG wash wastewater after removal of all SRG wastewater required for settling adsorption).
The utility model discloses in, the liquid mixing pond is for carrying out intensive mixing with remaining SRG waste water with SRG waste water after subsiding the absorption, is on the one hand for concentrating the catalytic disproportionation that realizes the bisulfite in the two waste water, and on the other hand is also for adjusting the acid of the waste water after mixing unanimously with the concentration phase equilibrium of contained bisulfite ion. And then the wastewater after uniform mixing is conveyed to a catalytic disproportionation pool for catalytic disproportionation reaction.
The utility model discloses in, put into the catalytic disproportionation pond simultaneously SRG washing waste water that contains the bisulfite ion and content active carbon, then heat to 40-80 ℃ (preferably 50-60 ℃) and carry out disproportionation for the bisulfite ion in the waste water takes place disproportionation under the catalytic action who contains sulfur activated carbon. Thereby realizing the purpose of reducing the bisulfite content of the SRG washing wastewater. The SRG wastewater with the bisulfite content reduced is discharged into a wastewater post-treatment system for subsequent purification treatment.
The utility model discloses in, the sulphur colloid that the disproportionation reaction of hydrogen sulfite radical ion generated in the catalytic disproportionation pond is retrieved and is carried out further heating (for example heating to 50-120 ℃, preferably heating to 70-100 ℃) destabilizing reaction in the colloid destabilizing pond, and then the preparation obtains the sulphur simple substance that has economic value and carries out recycle.
The utility model discloses in, what waste water conveyor was waste water pipeline. The caliber is 0.1-100m, preferably 0.3-80m, more preferably 0..8-50m, and still more preferably 1-30 m.
In the utility model, the number of the wastewater conveying device, the carbon-liquid separation tank, the sedimentation adsorption tank, the catalytic disproportionation tank and the colloid destabilizing tank is 1-100, preferably 2-80, preferably 3-50, and more preferably 5-30 respectively.
In the utility model, the volumes of the carbon-liquid separation tank, the sedimentation adsorption tank, the catalytic disproportionation tank and the colloid destabilizing tank are respectively and independently 1-100000000m3Preferably 2-50000000m3More preferably 3 to 10000000m3More preferably 5 to 1000000m3More preferably 10 to 500000m3。
In the present invention, the sulfur loading per gram of activated carbon is the sulfur content per unit mass of activated carbon in the sulfur-containing activated carbon after the embodiment provided by the present invention. I.e., the mass ratio of sulfur to activated carbon in the sulfur-containing activated carbon.
Compared with the prior art, the utility model discloses a beneficial technological effect as follows:
1. the utility model discloses can utilize the active carbon that SRG waste water itself contains as the adsorption carrier to and release colloidal sulfur as the sulphur source after the acidolysis of the thiosulfate radical ion in the utilization waste water, have stronger adsorption through active carbon powder or active carbon granule. So that the colloidal sulfur separated out by the acidolysis of thiosulfate ions enters the activated carbon powder or the activated carbon particles to form the sulfur-containing activated carbon. The sulfur-containing activated carbon with excellent catalytic performance is prepared by changing waste into valuable under normal temperature and normal pressure through simple process conditions.
2. The utility model discloses a special structural design, ingenious utilization contain the catalytic disproportionation of sulphur active carbon and be used for containing bisulfite in cyanogen SRG washing wastewater, realize its low temperature catalytic disproportionation. The salt content of the washing wastewater is reduced, and simultaneously, the sulfur can be recovered, so that the resource utilization and treatment of the wastewater are realized, and no secondary pollution is generated.
3. The utility model discloses based on the nature of bisulfite disproportionation sulphur production, through the new technology of the disproportionation method desalination sulphur removal that proposes of structural optimization novelty, salt content reduces and the recovery of sulphur resource in the realization waste water, very big reduction follow-up waste water treatment in-process liquid caustic soda's consumption (through contrast test, can reduce about 60%). Provides a new way for the treatment and resource utilization of SRG washing wastewater.
Drawings
FIG. 1 is a schematic diagram of the system for catalytic desalination of SRG washing wastewater.
FIG. 2 is an overall structure diagram of the system for catalytic desalination of SRG washing wastewater.
FIG. 3 is a comparison graph of the later alkali consumption of the wastewater after the system treatment and the later alkali consumption of the wastewater in the prior art.
Reference numerals: 1: a wastewater delivery device; 2: a carbon-liquid separation tank; 3: a sedimentation adsorption tank; 4: a catalytic disproportionation tank; 5: a colloid destabilizing tank; 6: an acidification treatment tank; 601: an acid liquor conveying pipeline; 7: an active carbon cache bin; 8: a liquid mixing tank; 9: a sulfur-containing activated carbon cache; 10: a first solid-liquid separation device; 11: a second solid-liquid separation device; 12: a sulfur drying device; 1201: a shielding gas delivery conduit; 13: a wastewater post-treatment system; 14: a sulfur storage bin; l1: a first conduit; l2: a second conduit; l3: a third pipeline; l4: a fourth conduit; l5: a fifth pipeline; l6: a sixth pipeline; l7: a seventh pipe; s1: a first material conveying device; s2: a second material conveying device; s3: a third material conveying device; s4: a fourth material conveying device; s5: a fifth material conveying device; s6: a sixth material conveying device; s7: a seventh material conveying device; s8: an eighth material conveying device; s9: a ninth material conveying device; s10: a tenth material conveying device.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed invention includes but is not limited to the following embodiments.
A system for the catalytic desalination of SRG washing wastewater or a system for the catalytic desalination of SRG washing wastewater used in the method of the first embodiment comprises a wastewater conveying device 1, a carbon-liquid separation tank 2, a sedimentation adsorption tank 3, a catalytic disproportionation tank 4 and a colloid destabilizing tank 5. The waste water conveying device 1 is communicated with a feed inlet of the carbon-liquid separation tank 2. The carbon-liquid separation tank 2, the sedimentation adsorption tank 3, the catalytic disproportionation tank 4 and the colloid destabilizing tank 5 are sequentially connected in series. The volume of the carbon liquid separation tank 2 is 3-10000000m3Preferably 5 to 1000000m3More preferably 10 to 500000m3。
Preferably, the system also comprises an acidification treatment tank 6, and the acidification treatment tank 6 is positioned between the carbon liquid separation tank 2 and the sedimentation adsorption tank 3. The water outlet of the carbon-liquid separation tank 2 is communicated with the water inlet of the acidification tank 6 through a first pipeline L1. The water outlet of the acidification treatment pool 6 is communicated with the water inlet of the sedimentation adsorption pool 3 through a second pipeline L2. An acid liquor conveying pipeline 601 is connected to an acid inlet of the acidification tank 6.
Preferably, the system further comprises an activated carbon buffer bin 7. The activated carbon buffer storage bin 7 is positioned between the carbon liquid separation tank 2 and the sedimentation adsorption tank 3. The discharge port of the carbon-liquid separation tank 2 is communicated with the feed port of the activated carbon buffer storage bin 7 through a first material conveying device S1. The discharge port of the charcoal buffer storage bin 7 is communicated with the feed inlet of the sedimentation adsorption tank 3 through a second material conveying device S2.
Preferably, the system further comprises a liquid mixing tank 8. The liquid mixing tank 8 is positioned between the sedimentation adsorption tank 3 and the catalytic disproportionation tank 4. The water outlet of the sedimentation adsorption tank 3 is communicated with the water inlet of the liquid mixing tank 8 through a third pipeline L3. The water outlet of the carbon-liquid separation tank 2 is also communicated with the water inlet of the liquid mixing tank 8 through a fourth pipeline L4. The water outlet of the liquid mixing tank 8 is communicated with the water inlet of the catalytic disproportionation tank 4 through a fifth pipeline L5.
Preferably, the system also comprises a sulfur-containing activated carbon buffer bin 9. The sulfur-containing activated carbon buffer bin 9 is positioned between the sedimentation adsorption tank 3 and the catalytic disproportionation tank 4. And the discharge port of the sedimentation adsorption tank 3 is communicated with the feed inlet of the sulfur-containing activated carbon buffer storage bin 9 through a third material conveying device S3. The discharge port of the sulfur-containing activated carbon buffer bin 9 is communicated with the feed inlet of the catalytic disproportionation pool 4 through a fourth material conveying device S4.
Preferably, the discharge port of the sulfur-containing activated carbon buffer bin 9 is also communicated with the feed port of the sedimentation adsorption tank 3 through a fifth material conveying device S5.
Preferably, the system further comprises a first solid liquid separation device 10. The first solid-liquid separation device 10 is positioned between the catalytic disproportionation tank 4 and the colloid destabilizing tank 5. The discharge port of the catalytic disproportionation tank 4 is connected with the feed port of the first solid-liquid separation device 10 through a sixth material conveying device S6. The water outlet of the first solid-liquid separation device 10 is communicated with the water inlet of the colloid destabilizing pool 5 through a sixth pipeline L6.
Preferably, the discharge port of the first solid-liquid separation device 10 is also communicated with the feed port of the catalytic disproportionation tank 4 through a seventh material conveying device S7.
Preferably, the system further comprises a second solid liquid separation device 11. And the feed inlet of the second solid-liquid separation device 11 is communicated with the discharge outlet of the colloid destabilizing tank 5 through an eighth material conveying device S8. A discharge port of the second solid-liquid separation device 11 is connected with a ninth material conveying device S9, and a water discharge port of the second solid-liquid separation device 11 is connected with a seventh pipeline L7.
Preferably, the system further comprises a sulphur drying apparatus 12. The feed inlet of the sulfur drying device 12 is communicated with the discharge outlet of the second solid-liquid separation device 11 through a ninth material conveying device S9. And a protective gas conveying pipeline 1201 is connected to the gas inlet of the sulfur drying device 12.
Preferably, the system also includes a wastewater aftertreatment system 13. The water inlet of the wastewater post-treatment system 13 is communicated with the water outlet of the second solid-liquid separation device 11 through a seventh pipeline L7.
Preferably, the system further comprises a sulphur storage silo 14. The sulfur storage bin 14 is communicated with a discharge port of the sulfur drying device 12 through a tenth material conveying device S10.
Example 1
As shown in figure 2, the system for the catalytic desalination of the SRG washing wastewater comprises a wastewater conveying device 1, a carbon-liquid separation tank 2, a sedimentation adsorption tank 3, a catalytic disproportionation tank 4 and a colloid destabilizing tank 5. The waste water conveying device 1 is communicated with a feed inlet of the carbon-liquid separation tank 2. The carbon-liquid separation tank 2, the sedimentation adsorption tank 3, the catalytic disproportionation tank 4 and the colloid destabilizing tank 5 are sequentially connected in series. The volume of the carbon-liquid separation tank 2 is 300000m3。
Example 2
Example 1 was repeated as shown in fig. 3, except that the system further included an acidification treatment tank 6, and the acidification treatment tank 6 was located between the carbon-liquid separation tank 2 and the settling adsorption tank 3. The water outlet of the carbon-liquid separation tank 2 is communicated with the water inlet of the acidification tank 6 through a first pipeline L1. The water outlet of the acidification treatment pool 6 is communicated with the water inlet of the sedimentation adsorption pool 3 through a second pipeline L2. An acid liquor conveying pipeline 601 is connected to an acid inlet of the acidification tank 6.
Example 3
Example 2 is repeated except that the system further comprises a charcoal buffer bin 7. The activated carbon buffer storage bin 7 is positioned between the carbon liquid separation tank 2 and the sedimentation adsorption tank 3. The discharge port of the carbon-liquid separation tank 2 is communicated with the feed port of the activated carbon buffer storage bin 7 through a first material conveying device S1. The discharge port of the charcoal buffer storage bin 7 is communicated with the feed inlet of the sedimentation adsorption tank 3 through a second material conveying device S2.
Example 4
Example 3 was repeated except that the system further included a mixing tank 8. The liquid mixing tank 8 is positioned between the sedimentation adsorption tank 3 and the catalytic disproportionation tank 4. The water outlet of the sedimentation adsorption tank 3 is communicated with the water inlet of the liquid mixing tank 8 through a third pipeline L3. The water outlet of the carbon-liquid separation tank 2 is also communicated with the water inlet of the liquid mixing tank 8 through a fourth pipeline L4. The water outlet of the liquid mixing tank 8 is communicated with the water inlet of the catalytic disproportionation tank 4 through a fifth pipeline L5.
Example 5
Example 4 was repeated except that the system further included a sulfur-containing activated carbon buffer bin 9. The sulfur-containing activated carbon buffer bin 9 is positioned between the sedimentation adsorption tank 3 and the catalytic disproportionation tank 4. And the discharge port of the sedimentation adsorption tank 3 is communicated with the feed inlet of the sulfur-containing activated carbon buffer storage bin 9 through a third material conveying device S3. The discharge port of the sulfur-containing activated carbon buffer bin 9 is communicated with the feed inlet of the catalytic disproportionation pool 4 through a fourth material conveying device S4.
Example 6
Example 5 is repeated, except that the discharge port of the sulfur-containing activated carbon buffer bin 9 is also communicated with the feed port of the sedimentation adsorption tank 3 through a fifth material conveying device S5.
Example 7
Example 6 is repeated except that the system further comprises a first solid liquid separation device 10. The first solid-liquid separation device 10 is positioned between the catalytic disproportionation tank 4 and the colloid destabilizing tank 5. The discharge port of the catalytic disproportionation tank 4 is connected with the feed port of the first solid-liquid separation device 10 through a sixth material conveying device S6. The water outlet of the first solid-liquid separation device 10 is communicated with the water inlet of the colloid destabilizing pool 5 through a sixth pipeline L6.
Example 8
Example 7 was repeated except that the discharge port of the first solid-liquid separating device 10 was also communicated with the feed port of the catalytic disproportionation tank 4 through a seventh material transport device S7.
Example 9
Example 8 is repeated except that the system further comprises a second solid liquid separation device 11. And the feed inlet of the second solid-liquid separation device 11 is communicated with the discharge outlet of the colloid destabilizing tank 5 through an eighth material conveying device S8. A discharge port of the second solid-liquid separation device 11 is connected with a ninth material conveying device S9, and a water discharge port of the second solid-liquid separation device 11 is connected with a seventh pipeline L7.
Example 10
Example 9 is repeated except that the system further comprises a sulphur drying apparatus 12. The feed inlet of the sulfur drying device 12 is communicated with the discharge outlet of the second solid-liquid separation device 11 through a ninth material conveying device S9. And a protective gas conveying pipeline 1201 is connected to the gas inlet of the sulfur drying device 12.
Example 11
Example 10 was repeated except that the system further included a wastewater aftertreatment system 13. The water inlet of the wastewater post-treatment system 13 is communicated with the water outlet of the second solid-liquid separation device 11 through a seventh pipeline L7.
Example 12
Example 11 is repeated except that the system further comprises a sulphur storage silo 14. The sulfur storage bin 14 is communicated with a discharge port of the sulfur drying device 12 through a tenth material conveying device S10.
Example 13
Example 1 was repeated, except that the volume of the carbon-liquid separation tank 2 was 100000m3。
Example 14
Example 1 was repeated, except that the volume of the carbon-liquid separation tank 2 was 50000m3。
Application example 1
5.0m of cyanogen-containing SRG wastewater is taken3And detecting that the content of sulfate ions in the wastewater is 911mg/L and the content of the active carbon is 82 mg/L.
Firstly, separating the active carbon powder in the cyanide-containing SRG washing wastewater, and then taking 2.0m3The cyanogen-containing SRG washes the waste water, and sulfuric acid is added into the part of the waste water to adjust the pH value to be less than 3. Then adding activated carbon powder into the acidified cyanide-containing SRG wastewater at normal temperature and pressure for sedimentation and adsorption for 2 hours. And after adsorption, carrying out solid-liquid separation to obtain a solid I and a filtrate I, and drying the obtained solid I at 80 ℃ for 1h to obtain the sulfur-containing activated carbon I.
Application example 2
5.0m of cyanogen-containing SRG wastewater is taken3And detecting that the content of sulfate ions in the wastewater is 1209mg/L and the content of the activated carbon is 71 mg/L.
Firstly, separating the active carbon powder in the cyanide-containing SRG washing wastewater, and then taking 2.5m3Washing waste water of SRG containing cyanogen, and adding the waste waterAdding sulfuric acid to regulate pH value to less than 2. Then adding activated carbon powder into the acidified cyanide-containing SRG wastewater at normal temperature and pressure for sedimentation and adsorption for 2 hours. And after adsorption, carrying out solid-liquid separation to obtain a solid II and a filtrate II, and drying the obtained solid II at 70 ℃ for 2h to obtain the sulfur-containing activated carbon II.
Application example 3
Example 1 was repeated, except that 1.0m was again taken3The cyanogen-containing SRG washes the waste water, and sulfuric acid is added into the part of the waste water to adjust the pH value to be less than 2. Then adding sulfur-containing activated carbon I into the acidified cyanide-containing SRG wastewater at normal temperature and normal pressure for settling and adsorbing for 1 h. And after adsorption, carrying out solid-liquid separation to obtain solid III and filtrate III, and drying the obtained solid III at 70 ℃ for 2h to obtain the sulfur-containing activated carbon III.
Application example 4
Application example 1 was repeated except that filtrate I and the remaining 3.0m3The cyanogen-containing SRG washing wastewater is uniformly mixed, and the concentration of bisulfite ions in the mixed washing wastewater is detected to be 64.67 g/L. Then adding sulfur-containing activated carbon I, and heating to 55 ℃ for disproportionation reaction; and continuously monitoring the pH value of the reaction system, filtering when the pH value of the reaction system is lower than 2, separating sulfur-containing activated carbon and obtaining filtrate. The filtrate was heated to 90 ℃ and the reaction was continued until sulfur precipitate was formed and a clear supernatant was obtained. The sulphur precipitate was then separated and dried at 80 ℃ for 2h under nitrogen protection to yield 39.01kg of elemental sulphur. The content of the bisulfate ion in the wastewater after catalytic desulfurization is detected to be 0.56 g/L.
Application example 5
Application example 2 was repeated except that filtrate II and the remaining 2.5m3The cyanogen-containing SRG washing wastewater is uniformly mixed, and the concentration of bisulfite ions in the mixed washing wastewater is detected to be 60.94 g/L. Then adding sulfur-containing activated carbon I, and heating to 55 ℃ for disproportionation reaction; and continuously monitoring the pH value of the reaction system, filtering when the pH value of the reaction system is lower than 2, separating sulfur-containing activated carbon and obtaining filtrate. The filtrate was heated to 90 ℃ and the reaction was continued until sulfur precipitate was formed and a clear supernatant was obtained. The sulphur precipitate is then separated off and kept under nitrogen at 8Drying at 0 ℃ for 2h to obtain 36.88kg of elemental sulfur. The content of the bisulfate ion in the wastewater after catalytic desulfurization is detected to be 0.80 g/L.
Application example 6
Application example 3 was repeated except that filtrate I, filtrate III and the remaining 2.0m3The cyanogen-containing SRG washing wastewater is uniformly mixed, and the concentration of bisulfite ions in the mixed washing wastewater is detected to be 62.73 g/L. Then adding sulfur-containing activated carbon III, and heating to 55 ℃ for disproportionation reaction; and continuously monitoring the pH value of the reaction system, filtering when the pH value of the reaction system is lower than 2, separating sulfur-containing activated carbon and obtaining filtrate. The filtrate was heated to 90 ℃ and the reaction was continued until sulfur precipitate was formed and a clear supernatant was obtained. The sulphur precipitate was then separated and dried at 80 ℃ for 2h under nitrogen protection to obtain 37.25kg of elemental sulphur. The content of the bisulfate ion in the wastewater after catalytic desulfurization was detected to be 0.42 g/L.
Claims (25)
1. The system for the catalytic desalination of the SRG washing wastewater is characterized in that: the system comprises a wastewater conveying device (1), a carbon-liquid separation tank (2), a sedimentation adsorption tank (3), a catalytic disproportionation tank (4) and a colloid destabilizing tank (5); the waste water conveying device (1) is communicated with a feed inlet of the carbon-liquid separation tank (2); the carbon-liquid separation tank (2), the sedimentation adsorption tank (3), the catalytic disproportionation tank (4) and the colloid destabilizing tank (5) are sequentially connected in series; the volume of the carbon liquid separation tank (2) is 3-10000000m3。
2. The system of claim 1, wherein: the volume of the carbon-liquid separation tank (2) is 5-1000000m3。
3. The system of claim 2, wherein: the volume of the carbon-liquid separation tank (2) is 10-500000m3。
4. The system according to any one of claims 1-3, wherein: the system also comprises an acidification treatment pool (6), wherein the acidification treatment pool (6) is positioned between the carbon-liquid separation pool (2) and the sedimentation adsorption pool (3); the water outlet of the carbon-liquid separation tank (2) is communicated with the water inlet of the acidification tank (6) through a first pipeline (L1); the water outlet of the acidification treatment pool (6) is communicated with the water inlet of the sedimentation adsorption pool (3) through a second pipeline (L2); an acid liquor conveying pipeline (601) is connected to an acid inlet of the acidification tank (6).
5. The system of claim 4, wherein: the system also comprises an active carbon buffer bin (7); the activated carbon buffer bin (7) is positioned between the carbon-liquid separation tank (2) and the sedimentation adsorption tank (3); the discharge port of the carbon-liquid separation tank (2) is communicated with the feed port of the activated carbon buffer bin (7) through a first material conveying device (S1); the discharge port of the charcoal buffer bin (7) is communicated with the feed inlet of the sedimentation adsorption tank (3) through a second material conveying device (S2).
6. The system according to any one of claims 1-3, 5, wherein: the system also comprises a liquid mixing tank (8); the liquid mixing tank (8) is positioned between the sedimentation adsorption tank (3) and the catalytic disproportionation tank (4); the water outlet of the sedimentation adsorption tank (3) is communicated with the water inlet of the liquid mixing tank (8) through a third pipeline (L3); the water outlet of the carbon-liquid separation tank (2) is also communicated with the water inlet of the liquid mixing tank (8) through a fourth pipeline (L4); the water outlet of the liquid mixing pool (8) is communicated with the water inlet of the catalytic disproportionation pool (4) through a fifth pipeline (L5).
7. The system of claim 4, wherein: the system also comprises a liquid mixing tank (8); the liquid mixing tank (8) is positioned between the sedimentation adsorption tank (3) and the catalytic disproportionation tank (4); the water outlet of the sedimentation adsorption tank (3) is communicated with the water inlet of the liquid mixing tank (8) through a third pipeline (L3); the water outlet of the carbon-liquid separation tank (2) is also communicated with the water inlet of the liquid mixing tank (8) through a fourth pipeline (L4); the water outlet of the liquid mixing pool (8) is communicated with the water inlet of the catalytic disproportionation pool (4) through a fifth pipeline (L5).
8. The system of any one of claims 1-3, 5, 7, wherein: the system also comprises a sulfur-containing activated carbon buffer bin (9); the sulfur-containing activated carbon buffer bin (9) is positioned between the sedimentation adsorption tank (3) and the catalytic disproportionation tank (4); the discharge port of the sedimentation adsorption tank (3) is communicated with the feed port of the sulfur-containing activated carbon buffer bin (9) through a third material conveying device (S3); the discharge port of the sulfur-containing activated carbon buffer bin (9) is communicated with the feed inlet of the catalytic disproportionation pool (4) through a fourth material conveying device (S4).
9. The system of claim 4, wherein: the system also comprises a sulfur-containing activated carbon buffer bin (9); the sulfur-containing activated carbon buffer bin (9) is positioned between the sedimentation adsorption tank (3) and the catalytic disproportionation tank (4); the discharge port of the sedimentation adsorption tank (3) is communicated with the feed port of the sulfur-containing activated carbon buffer bin (9) through a third material conveying device (S3); the discharge port of the sulfur-containing activated carbon buffer bin (9) is communicated with the feed inlet of the catalytic disproportionation pool (4) through a fourth material conveying device (S4).
10. The system of claim 6, wherein: the system also comprises a sulfur-containing activated carbon buffer bin (9); the sulfur-containing activated carbon buffer bin (9) is positioned between the sedimentation adsorption tank (3) and the catalytic disproportionation tank (4); the discharge port of the sedimentation adsorption tank (3) is communicated with the feed port of the sulfur-containing activated carbon buffer bin (9) through a third material conveying device (S3); the discharge port of the sulfur-containing activated carbon buffer bin (9) is communicated with the feed inlet of the catalytic disproportionation pool (4) through a fourth material conveying device (S4).
11. The system of claim 8, wherein: the discharge hole of the sulfur-containing activated carbon buffer bin (9) is also communicated with the feed inlet of the sedimentation adsorption tank (3) through a fifth material conveying device (S5).
12. The system according to claim 9 or 10, characterized in that: the discharge hole of the sulfur-containing activated carbon buffer bin (9) is also communicated with the feed inlet of the sedimentation adsorption tank (3) through a fifth material conveying device (S5).
13. The system of any one of claims 1-3, 5, 7, 9-11, wherein: the system further comprises a first solid-liquid separation device (10); the first solid-liquid separation device (10) is positioned between the catalytic disproportionation tank (4) and the colloid destabilizing tank (5); the discharge port of the catalytic disproportionation tank (4) is connected with the feed port of the first solid-liquid separation device (10) through a sixth material conveying device (S6); the water outlet of the first solid-liquid separation device (10) is communicated with the water inlet of the colloid destabilizing pool (5) through a sixth pipeline (L6).
14. The system of claim 4, wherein: the system further comprises a first solid-liquid separation device (10); the first solid-liquid separation device (10) is positioned between the catalytic disproportionation tank (4) and the colloid destabilizing tank (5); the discharge port of the catalytic disproportionation tank (4) is connected with the feed port of the first solid-liquid separation device (10) through a sixth material conveying device (S6); the water outlet of the first solid-liquid separation device (10) is communicated with the water inlet of the colloid destabilizing pool (5) through a sixth pipeline (L6).
15. The system of claim 6, wherein: the system further comprises a first solid-liquid separation device (10); the first solid-liquid separation device (10) is positioned between the catalytic disproportionation tank (4) and the colloid destabilizing tank (5); the discharge port of the catalytic disproportionation tank (4) is connected with the feed port of the first solid-liquid separation device (10) through a sixth material conveying device (S6); the water outlet of the first solid-liquid separation device (10) is communicated with the water inlet of the colloid destabilizing pool (5) through a sixth pipeline (L6).
16. The system of claim 13, wherein: the discharge port of the first solid-liquid separation device (10) is also communicated with the feed port of the catalytic disproportionation pool (4) through a seventh material conveying device (S7).
17. The system according to claim 14 or 15, wherein: the discharge port of the first solid-liquid separation device (10) is also communicated with the feed port of the catalytic disproportionation pool (4) through a seventh material conveying device (S7).
18. The system of any one of claims 1-3, 5, 7, 9-11, 14-16, wherein: the system further comprises a second solid-liquid separation device (11); the feed inlet of the second solid-liquid separation device (11) is communicated with the discharge outlet of the colloid destabilizing tank (5) through an eighth material conveying device (S8); a discharge port of the second solid-liquid separation device (11) is connected with a ninth material conveying device (S9), and a water discharge port of the second solid-liquid separation device (11) is connected with a seventh pipeline (L7).
19. The system of claim 4, wherein: the system further comprises a second solid-liquid separation device (11); the feed inlet of the second solid-liquid separation device (11) is communicated with the discharge outlet of the colloid destabilizing tank (5) through an eighth material conveying device (S8); a discharge port of the second solid-liquid separation device (11) is connected with a ninth material conveying device (S9), and a water discharge port of the second solid-liquid separation device (11) is connected with a seventh pipeline (L7).
20. The system of claim 6, wherein: the system further comprises a second solid-liquid separation device (11); the feed inlet of the second solid-liquid separation device (11) is communicated with the discharge outlet of the colloid destabilizing tank (5) through an eighth material conveying device (S8); a discharge port of the second solid-liquid separation device (11) is connected with a ninth material conveying device (S9), and a water discharge port of the second solid-liquid separation device (11) is connected with a seventh pipeline (L7).
21. The system of claim 18, wherein: the system also comprises a sulfur drying device (12); the feed inlet of the sulfur drying device (12) is communicated with the discharge outlet of the second solid-liquid separation device (11) through a ninth material conveying device (S9); and a protective gas conveying pipeline (1201) is connected to the gas inlet of the sulfur drying device (12).
22. The system according to claim 19 or 20, wherein: the system also comprises a sulfur drying device (12); the feed inlet of the sulfur drying device (12) is communicated with the discharge outlet of the second solid-liquid separation device (11) through a ninth material conveying device (S9); and a protective gas conveying pipeline (1201) is connected to the gas inlet of the sulfur drying device (12).
23. The system of claim 21, wherein: the system also comprises a waste water post-treatment system (13); the water inlet of the wastewater post-treatment system (13) is communicated with the water outlet of the second solid-liquid separation device (11) through a seventh pipeline (L7).
24. The system of claim 22, wherein: the system also comprises a waste water post-treatment system (13); the water inlet of the wastewater post-treatment system (13) is communicated with the water outlet of the second solid-liquid separation device (11) through a seventh pipeline (L7).
25. The system according to claim 23 or 24, wherein: the system also comprises a sulfur storage bin (14); the sulfur storage bin (14) is communicated with a discharge port of the sulfur drying device (12) through a tenth material conveying device (S10).
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