CN210559766U - Wet vanadium recovery wastewater resource utilization system - Google Patents
Wet vanadium recovery wastewater resource utilization system Download PDFInfo
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Abstract
The utility model discloses a recycling system for vanadium recovery waste water by a wet method, which relates to the field of chemical equipment and comprises a pretreatment unit, an ammonia recovery unit and a sodium sulfate recovery unit; the preprocessing unit includes: a regulating tank, a dosing device, a dosing reaction tank, an inclined plate sedimentation tank, a sludge tank and a continuous automatic filtration system. By adopting the method, the effective treatment of the vanadium recovery wastewater of the wet method can be realized, and the treated wastewater can reach the primary standard of Integrated wastewater discharge Standard (GB 8978-1996). Meanwhile, by adopting the method, the by-products of ammonia water and sodium sulfate can be recovered, the concentration of the recovered ammonia water reaches 18% -25%, the recovered sodium sulfate meets the first-class I requirements in the Industrial anhydrous sodium sulfate (GB/T6009-2014), the reclamation of the wastewater is realized to a greater extent, and the method has great economic value. The novel multifunctional clothes hanger is ingenious in design, reasonable in design, convenient to use and simple to operate.
Description
Technical Field
The utility model relates to a chemical industry equipment field specifically is a wet process vanadium recovery waste water resource utilization system.
Background
A large amount of waste catalysts are generated in the acid making industry of China every year, and V-K-Si series catalysts for oxidation are general V2O5The content is 6.3% -8%, and the vanadium extraction and recovery treatment is carried out on the waste catalyst by adopting a wet process, so that the method has important environmental benefits and economic benefits. In the wet vanadium extraction recovery treatment process, a large amount of wastewater is generated, and the wastewater has the characteristics of high hardness, high salt content, high ammonia nitrogen content and the like. At present, the wastewater is directly recycled after the hardness in the wastewater is reduced through simple coagulating sedimentation, or the ammonia nitrogen in the wastewater is reduced by adopting a stripping, stripping or distilling method; when the wastewater is recycled to be supersaturated, evaporation and crystallization are carried out to obtain miscellaneous salt, transportation is carried out, and the condensate is continuously produced and recycled. The current treatment means cannot effectively treat the wastewater, and sodium salt in the wastewater is treated as solid waste. How to effectively treat the wastewater, reduce the operation cost and realize resource utilization to the maximum extent is the key point of the wastewater treatment research.
Therefore, the application provides a wet-process vanadium recycling wastewater resource utilization system to solve the problems.
SUMMERY OF THE UTILITY MODEL
The invention of the utility model aims to: the resource utilization system for the wet vanadium recovery wastewater is provided, aiming at the problems that the existing treatment equipment can not effectively treat the wet vanadium recovery wastewater, and the sodium salt in the wastewater is treated as solid waste to cause resource waste. By adopting the method, the effective treatment of the vanadium recovery wastewater of the wet method can be realized, and the treated wastewater can reach the primary standard of Integrated wastewater discharge Standard (GB 8978-1996). Meanwhile, by adopting the method, the by-products of ammonia water and sodium sulfate can be recovered, the concentration of the recovered ammonia water reaches 18% -25%, the recovered sodium sulfate meets the first-class I requirements in the Industrial anhydrous sodium sulfate (GB/T6009-2014), the reclamation of the wastewater is realized to a greater extent, and the method has great economic value. The application has the advantages of ingenious design, reasonable design, convenience in use and simplicity in operation, can meet the requirements of industrialization, large-scale production and application, and has high application value and good application prospect.
The utility model adopts the technical scheme as follows:
a wet vanadium recovery wastewater resource utilization system comprises a pretreatment unit, an ammonia recovery unit and a sodium sulfate recovery unit;
the preprocessing unit includes:
the wastewater can be homogenized and uniformly treated in the regulating tank;
the dosing device is connected with the dosing reaction tank and is used for adding an alkali solution into the dosing reaction tank to adjust the pH value to 10.0-10.5, adding a coagulant and adding a coagulant aid;
the dosing reaction tank is respectively connected with the regulating tank and the dosing device, and the wastewater is flocculated by regulating the pH value of the solution and adding a coagulant and a coagulant aid to react with the wastewater;
the inclined plate sedimentation tank is connected with the dosing reaction tank and is used for standing and precipitating substances in the dosing reaction tank to realize solid-liquid separation and respectively obtain supernatant and sludge;
the sludge tank is connected with the inclined plate sedimentation tank, and sludge generated by the inclined plate sedimentation tank can be sent into the sludge tank;
the continuous automatic filtration system is connected with the inclined plate sedimentation tank, and supernatant produced by the inclined plate sedimentation tank is added with alkali to adjust the pH value and then enters the continuous automatic filtration system to further reduce the SS of the wastewater;
the ammonia recovery unit includes:
the combined tank is used for recycling desorbed ammonia gas by utilizing the circulating injection of an ammonia water circulating injection pump and concentrating the ammonia gas;
the upper end of the negative-pressure sub-boiling alkali precipitation deamination tower is connected with a combined tank, waste water in the combined tank enters the negative-pressure sub-boiling alkali precipitation deamination tower through the upper part of the negative-pressure sub-boiling alkali precipitation deamination tower after being preheated by a waste heat recoverer, the waste water is uniformly distributed by a distributor in the negative-pressure sub-boiling alkali precipitation deamination tower and is subjected to mass transfer and heat transfer with hot steam flow rising from the bottom of the negative-pressure sub-boiling alkali precipitation deamination tower, and waste water at the bottom of the tower after ammonia desorption and ammonia;
the waste heat recoverer is respectively connected with the combined tank and the negative-pressure sub-boiling alkali-precipitation deamination tower, and the tower bottom waste water obtained by the negative-pressure sub-boiling alkali-precipitation deamination tower exchanges heat with the waste water entering the negative-pressure sub-boiling alkali-precipitation deamination tower through the waste heat recoverer and the combined tank;
the supergravity deamination separator is sequentially connected with a waste heat recoverer and a negative pressure sub-boiling alkali precipitation deamination tower, and the tower bottom wastewater after ammonia desorption is subjected to heat exchange by the waste heat recoverer and then is pumped into the supergravity deamination separator by a high-temperature pump to remove residual ammonia nitrogen;
the super ammonia absorber is respectively connected with the negative-pressure sub-boiling alkali separation deamination tower and the hypergravity deamination separator, and ammonia gas generated by the negative-pressure sub-boiling alkali separation deamination tower and the hypergravity deamination separator can enter the super ammonia absorber for absorption;
the ammonia water storage component is connected with the super ammonia absorber, and the ammonia gas absorbed in the super ammonia absorber can be sent into the ammonia water storage component to be prepared into ammonia water;
the sodium sulfate recovery unit includes:
the intermediate tank is connected with the hypergravity deamination separator, and the wastewater treated by the hypergravity deamination separator can be sent into the intermediate tank to be added with acid to adjust the pH value to 7-9;
the security filter is connected with the middle pool;
the nanofiltration equipment is connected with the security filter, the wastewater in the intermediate tank can enter the nanofiltration equipment for treatment after passing through the security filter, and the obtained clear liquid is recycled or discharged;
the freezing crystallization salt-forming system is connected with the nanofiltration equipment, and the solution treated by the nanofiltration equipment can enter the freezing crystallization salt-forming system for cooling and crystallization;
the centrifugal machine is connected with the freezing crystallization salt-forming system and can carry out centrifugal separation on the solid generated by crystallization of the freezing crystallization salt-forming system to respectively obtain crystalline sodium sulfate and mother liquor, and the mother liquor returns to the freezing crystallization salt-forming system;
and the dryer is connected with the centrifugal machine, and the crystalline sodium sulfate obtained by the separation of the centrifugal machine is dried by the dryer to obtain a finished product of sodium sulfate.
The pretreatment unit further comprises a filter press, the sludge tank is connected with the filter press, sludge in the sludge tank is subjected to filter pressing by the filter press to obtain second filtrate and sludge cakes, the filter press is connected with the regulating tank, and the second filtrate generated by the filter press can return to the regulating tank for recycling.
And carrying out sludge outward on the mud cakes generated by the filter press.
The ammonia water storage component is connected with the combined tank, and the ammonia gas absorbed in the super ammonia absorber can be sent into the ammonia water storage component to be prepared into ammonia water; when the concentration of the ammonia water is lower, part of the ammonia water returns to the combination tank for concentration again.
The ammonia water storage assembly comprises a first-level ammonia water tank, a second-level ammonia water tank and a tail gas absorption tower which are connected with the super ammonia absorber, the first-level ammonia water tank, the second-level ammonia water tank and the tail gas absorption tower are sequentially connected, and the first-level ammonia water tank is connected with the combined tank.
In view of the foregoing problems, the present application provides a wet vanadium recovery wastewater resource utilization system, which includes a pretreatment unit, an ammonia recovery unit, and a sodium sulfate recovery unit.
Wherein, the pretreatment unit is mainly used for reducing the total hardness, SS, heavy metal ions and the like in the wastewater. In the structure, wastewater firstly enters a regulating tank; and (3) homogenizing and homogenizing in the regulating reservoir, feeding the effluent of the regulating reservoir into a dosing reaction tank, adding alkali to regulate the pH value of the wastewater to 10-10.5, and adding a coagulant and a coagulant aid. Then, the mixture enters an inclined plate sedimentation tank for standing and sedimentation to realize solid-liquid separation. Sludge at the lower part of the inclined plate sedimentation tank enters a sludge tank, the sludge in the sludge tank is dehydrated through a filter press, filtrate generated by dehydration returns to the regulating tank, and the sludge is transported and disposed. And adding alkali into the supernatant obtained from the inclined plate sedimentation tank to adjust the pH value to 11.5-12, and then entering a continuous automatic filtration system to further reduce the SS in the wastewater.
The ammonia recovery unit is mainly used for reducing and recovering ammonia nitrogen in the wastewater.
The waste water at the outlet of the combined tank is preheated by the waste heat provided by the waste heat recoverer, then is pumped to a negative pressure sub-boiling alkali precipitation deamination tower, enters from the upper part of the tower, and is uniformly distributed by a waste water distributor to transfer heat with the hot steam flow mass transfer rising from the bottom of the tower. The bottom temperature and the top temperature of the negative pressure sub-boiling alkali precipitation deamination tower are controlled. And pumping the tower bottom wastewater after ammonia desorption into a supergravity ammonia-removing separator by a high-temperature pump, and further removing a small amount of residual ammonia nitrogen to reach the standard and then feeding the residual ammonia nitrogen into an intermediate tank.
The rising ammonia-containing gas in the supergravity deamination separator and the negative pressure sub-boiling alkali deamination tower is discharged from the upper part of the tower and sent into a super ammonia absorber for recycling. The primary ammonia water tank is circulating ammonia water, can be returned to the combination tank to recover moisture, simultaneously cleans partial filler on the combination tank to ensure the quality of the recovered ammonia water, and adopts common circulating water for cooling. The secondary ammonia water tank is the product ammonia water and is cooled by circulating water at the temperature of 5-10 ℃. A small amount of non-condensable gas in the ammonia tank carries ammonia gas, and the ammonia gas is purified by a tail gas absorption tower and then discharged to the outside.
The sodium sulfate recovery unit is mainly used for recovering sodium sulfate in the wastewater and enabling the wastewater to meet the requirements of recycling or discharging. And (3) conveying the wastewater treated by the supergravity deamination separator to an intermediate tank, adding sulfuric acid to adjust the pH value to 7-9, then feeding the wastewater into a security filter, and reducing SS (suspended solid) and the like in the wastewater by the security filter. The wastewater after security filtration enters a nanofiltration system, and the nanofiltration clear liquid is recycled or discharged to obtain the Na-containing wastewater2SO4The concentrated solution of (4). The obtained product mainly contains Na2SO4And (3) feeding the concentrated solution into a freezing crystallization salt-forming system, controlling the freezing temperature to be 1-3 ℃, then performing centrifugal separation, returning the mother solution to the freezing crystallization salt-forming system, and feeding the crystallized sodium sulfate into a dryer for drying to obtain a sodium sulfate product.
Through actual measurement, the wastewater treated by the system reaches the primary standard of Integrated wastewater discharge Standard (GB 8978-1996); meanwhile, the device can recover byproducts ammonia water and sodium sulfate, the concentration of the recovered ammonia water is 18% -25%, the recovered sodium sulfate meets the first-class I requirements in the Industrial anhydrous sodium sulfate (GB/T6009-2014), the wastewater recycling is realized to a greater extent, and the device has great economic value.
To sum up, owing to adopted above-mentioned technical scheme, the beneficial effects of the utility model are that:
(1) the continuous automatic filtering system is added, so that the removal effect of calcium, magnesium, SS and heavy metal ions is enhanced, the risk of scaling and blockage of equipment and pipelines is reduced, and the purity of a sodium sulfate product is improved;
(2) the ammonia water with the concentration of 18-25% can be prepared by matching a negative pressure sub-boiling alkali precipitation deamination tower, a super ammonia absorber and a two-stage ammonia water absorption tank; meanwhile, the waste heat recoverer is adopted, and the waste water at the bottom of the tower obtained by the negative-pressure sub-boiling alkali precipitation deamination tower exchanges heat with the waste water entering the negative-pressure sub-boiling alkali precipitation deamination tower from the combined tank, so that the energy consumption can be effectively reduced, and a better energy-saving effect is achieved;
(3) the method adopts nanofiltration to treat the deaminated wastewater, realizes the separation of monovalent salt and divalent salt, can reduce the load of a subsequent treatment unit, and can improve the purity of a sodium sulfate product;
(4) the sodium sulfate in the wastewater is recovered by adopting a freezing crystallization method, the solubility of the sodium sulfate at low temperature and the salt change such as sodium chloride are obviously utilized, the purity of the obtained sodium sulfate is high, and the energy consumption is reduced by more than 30% compared with the traditional triple effect evaporation;
(5) in the process of centrifugally separating the sodium sulfate, the low-temperature water is adopted for spraying, so that the purity of the sodium sulfate is further improved;
(6) the wastewater treated by the method can reach the first-class standard of Integrated wastewater discharge Standard (GB 8978-1996), byproducts ammonia water and sodium sulfate can be recovered, the concentration of the recovered ammonia water is 18% -25%, and the recovered sodium sulfate meets the first-class I requirements in Industrial anhydrous sodium sulfate (GB/T6009-2014), so that the wastewater recycling is realized to a greater extent, and the method has great economic value.
Drawings
FIG. 1 is a schematic view of a processing apparatus according to embodiment 1.
The labels in the figure are: 1. the device comprises a pretreatment unit, a 2 ammonia recovery unit, a 3 sodium sulfate recovery unit, a 10 regulating tank, a 11 dosing device, a 12 dosing reaction tank, a 13 inclined plate sedimentation tank, a 14 sludge tank, a 15 continuous automatic filtering system, a 16 filter press, a 20 combination tank, a 21 negative pressure sub-boiling alkali precipitation deamination tower, a 22 supergravity deamination separator, a 23 super ammonia absorber, a 24 primary ammonia tank, a 25 secondary ammonia tank, a 26 tail gas absorption tower, a 30 middle tank, a 31 safety filter, a 32 nanofiltration device, a 33 freezing crystallization salt formation system, a 34 centrifuge, a 35 and a dryer.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example 1
The wet vanadium recovery wastewater resource utilization system comprises a pretreatment unit, an ammonia recovery unit and a sodium sulfate recovery unit.
Wherein, the pretreatment unit comprises an adjusting tank, a dosing device, a dosing reaction tank, an inclined plate sedimentation tank, a sludge tank and a continuous automatic filtration system. In this structure, add the medicine reaction tank and link to each other with equalizing basin, charge device respectively, add the medicine reaction tank and link to each other with the inclined plate sedimentation tank, the inclined plate sedimentation tank links to each other with sludge tank, continuous automatic filtration system respectively.
The ammonia recovery unit comprises a combined tank, a negative pressure sub-boiling alkali precipitation deamination tower, a supergravity deamination separator, a superammonia absorber and an ammonia water storage component. Wherein, ammonia water is circularly sprayed by an ammonia water circulating injection pump to recover desorbed ammonia gas, and the ammonia gas is concentrated; the upper end of the negative pressure sub-boiling alkali precipitation deamination tower is connected with a combined tank, wastewater in the combined tank enters the negative pressure sub-boiling alkali precipitation deamination tower through the upper part of the negative pressure sub-boiling alkali precipitation deamination tower, the wastewater is uniformly distributed through a distributor in the negative pressure sub-boiling alkali precipitation deamination tower and is subjected to mass transfer and heat transfer with hot steam flow rising from the bottom of the tower, and ammonia gas is obtained from the tower bottom wastewater and the tower top after ammonia desorption at the tower bottom respectively; the hypergravity deamination separator is connected with the lower end of the negative pressure sub-boiling alkali precipitation deamination tower, and the tower bottom wastewater after ammonia desorption is pumped into the hypergravity deamination separator by a high temperature pump for residual ammonia nitrogen removal; the super ammonia absorber is respectively connected with the negative pressure sub-boiling alkali separating and deaminating tower and the hypergravity deamination separator, and ammonia gas generated by the negative pressure sub-boiling alkali separating and deaminating tower and the hypergravity deamination separator can enter the super ammonia absorber for absorption; the ammonia water storage component is respectively connected with the super ammonia absorber and the combined tank, ammonia gas absorbed in the super ammonia absorber can be sent into the ammonia water storage component to be prepared into ammonia water, and part of ammonia water can return to the combined tank. In this embodiment, the aqueous ammonia storage subassembly includes the one-level ammonia jar that links to each other with super ammonia absorber, second grade ammonia jar, tail gas absorption tower, and the one-level ammonia jar, second grade ammonia jar, tail gas absorption tower link to each other in proper order, and the one-level ammonia jar links to each other with the combination tank.
The sodium sulfate recovery unit comprises a middle tank, a security filter, a nanofiltration device, a freezing crystallization salt-forming system, a centrifugal machine and a dryer. Wherein, the hypergravity deamination separator, the middle pool, the security filter and the nanofiltration equipment are connected in sequence, the wastewater in the middle pool can enter the nanofiltration equipment for treatment after passing through the security filter, the obtained clear liquid is recycled or discharged, and simultaneously, the Na-containing material is obtained2SO4The concentrated solution of (4); the nanofiltration equipment is connected with the freezing crystallization salt-forming system, and the solution treated by the nanofiltration equipment can enter the freezing crystallization salt-forming system for cooling and crystallization; coldThe freezing crystallization salt forming system is connected with a centrifuge, the solid generated by the freezing crystallization salt forming system is centrifugally separated by the centrifuge to respectively obtain crystallized sodium sulfate and mother liquor, and the mother liquor returns to the freezing crystallization salt forming system; the centrifugal machine is connected with the dryer, and the crystallized sodium sulfate obtained by the separation of the centrifugal machine enters the dryer to be dried.
In this embodiment, the pretreatment unit further includes a filter press, the sludge tank is connected to the filter press, and the sludge in the sludge tank is subjected to filter pressing by the filter press to obtain a second filtrate and a sludge cake, the filter press is connected to the regulating reservoir, and the second filtrate generated by the filter press can be returned to the regulating reservoir for recycling, and the sludge cake generated by the filter press is transported to the outside.
In this embodiment, the ammonia recovery unit further includes a waste heat recovery unit, which is connected to the lower end of the negative pressure sub-boiling alkali precipitation deamination tower and the outlet of the combined tank, and the waste water treated by the negative pressure sub-boiling alkali precipitation deamination tower provides waste heat for the waste heat recovery unit, and the waste water is used for preheating the effluent of the combined tank and then enters the negative pressure sub-boiling alkali precipitation deamination tower.
And after the wet vanadium recovery wastewater enters an adjusting tank for homogenizing and equalizing, discharging water and entering a dosing reaction tank, adding alkali to adjust the pH value of the wastewater to 10.5, then adding PAC and PAM, then entering an inclined plate sedimentation tank for standing and sedimentation, allowing sludge at the lower part of the inclined plate sedimentation tank to enter a sludge tank, dehydrating by a filter press, returning filtrate to the adjusting tank, and transporting the sludge outside.
Adding alkali into the supernatant of the inclined plate sedimentation tank to adjust the pH value to 11.8, then feeding the supernatant into a continuous automatic filtration system, preheating the effluent by using waste heat provided by a waste heat recoverer, then feeding the effluent into a combined tank, circularly spraying by using an ammonia decomposition agent pump and an ammonia water circulating injection pump, then recovering the heat of the desorbed ammonia gas, and pumping the wastewater to a negative-pressure sub-boiling alkali precipitation deamination tower after passing through the combined tank. The temperature of the bottom of the tower and the temperature of the top of the tower of the negative pressure sub-boiling alkali precipitation deamination tower are controlled to be 115 ℃ and 95 ℃. And pumping the tower bottom wastewater after ammonia desorption into a supergravity deamination separator by a high-temperature pump for treatment, and then feeding into an intermediate tank.
The rising ammonia-containing gas in the supergravity deamination separator and the negative pressure sub-boiling alkali deamination tower is discharged from the upper part of the tower and sent into a super ammonia absorber for recycling. The primary ammonia water tank is circulating ammonia water, the secondary ammonia water tank is product ammonia water, the concentration of the ammonia water is 21.2%, and the circulating water at 5 ℃ is adopted for cooling.
Adding sulfuric acid into the intermediate tank to adjust the pH value to 8.6, then, entering security filtration, entering the nanofiltration system, and recycling or discharging the nanofiltration clear liquid. And (3) enabling the concentrated solution to enter a freezing crystallization salt-forming system, controlling the freezing temperature to be 2 ℃, then performing centrifugal separation, returning the mother solution to the freezing crystallization salt-forming system, enabling the crystallized sodium sulfate to enter a dryer, and drying to obtain a sodium sulfate product with the purity of 99.2%.
The results of measuring the quality of wastewater treated in this example are shown in Table 1 below.
TABLE 1 quality of wastewater
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (6)
1. A wet vanadium recovery wastewater resource utilization system is characterized by comprising a pretreatment unit, an ammonia recovery unit and a sodium sulfate recovery unit;
the preprocessing unit includes:
the wastewater can be homogenized and uniformly treated in the regulating tank;
the dosing device is connected with the dosing reaction tank and is used for adding an alkali solution into the dosing reaction tank to adjust the pH value to 10.0-10.5, adding a coagulant and adding a coagulant aid;
the dosing reaction tank is respectively connected with the regulating tank and the dosing device, and the wastewater is flocculated by regulating the pH value of the solution and adding a coagulant and a coagulant aid to react with the wastewater;
the inclined plate sedimentation tank is connected with the dosing reaction tank and is used for standing and precipitating substances in the dosing reaction tank to realize solid-liquid separation and respectively obtain supernatant and sludge;
the sludge tank is connected with the inclined plate sedimentation tank, and sludge generated by the inclined plate sedimentation tank can be sent into the sludge tank;
the continuous automatic filtration system is connected with the inclined plate sedimentation tank, and supernatant produced by the inclined plate sedimentation tank is added with alkali to adjust the pH value and then enters the continuous automatic filtration system to further reduce the SS of the wastewater;
the ammonia recovery unit includes:
the combined tank is used for recycling desorbed ammonia gas by utilizing the circulating injection of an ammonia water circulating injection pump and concentrating the ammonia gas;
the upper end of the negative-pressure sub-boiling alkali precipitation deamination tower is connected with a combined tank, waste water in the combined tank enters the negative-pressure sub-boiling alkali precipitation deamination tower through the upper part of the negative-pressure sub-boiling alkali precipitation deamination tower after being preheated by a waste heat recoverer, the waste water is uniformly distributed by a distributor in the negative-pressure sub-boiling alkali precipitation deamination tower and is subjected to mass transfer and heat transfer with hot steam flow rising from the bottom of the negative-pressure sub-boiling alkali precipitation deamination tower, and waste water at the bottom of the tower after ammonia desorption and ammonia;
the waste heat recoverer is respectively connected with the combined tank and the negative-pressure sub-boiling alkali-precipitation deamination tower, and the tower bottom waste water obtained by the negative-pressure sub-boiling alkali-precipitation deamination tower exchanges heat with the waste water entering the negative-pressure sub-boiling alkali-precipitation deamination tower through the waste heat recoverer and the combined tank;
the supergravity deamination separator is sequentially connected with a waste heat recoverer and a negative pressure sub-boiling alkali precipitation deamination tower, and the tower bottom wastewater after ammonia desorption is subjected to heat exchange by the waste heat recoverer and then is pumped into the supergravity deamination separator by a high-temperature pump to remove residual ammonia nitrogen;
the super ammonia absorber is respectively connected with the negative-pressure sub-boiling alkali separation deamination tower and the hypergravity deamination separator, and ammonia gas generated by the negative-pressure sub-boiling alkali separation deamination tower and the hypergravity deamination separator can enter the super ammonia absorber for absorption;
the ammonia water storage component is connected with the super ammonia absorber, and the ammonia gas absorbed in the super ammonia absorber can be sent into the ammonia water storage component to be prepared into ammonia water;
the sodium sulfate recovery unit includes:
the intermediate tank is connected with the hypergravity deamination separator, and the wastewater treated by the hypergravity deamination separator can be sent into the intermediate tank to be added with acid to adjust the pH value to 7-9;
the security filter is connected with the middle pool;
the nanofiltration equipment is connected with the security filter, the wastewater in the intermediate tank can enter the nanofiltration equipment for treatment after passing through the security filter, and the obtained clear liquid is recycled or discharged;
the freezing crystallization salt-forming system is connected with the nanofiltration equipment, and the solution treated by the nanofiltration equipment can enter the freezing crystallization salt-forming system for cooling and crystallization;
the centrifugal machine is connected with the freezing crystallization salt-forming system and can carry out centrifugal separation on the solid generated by crystallization of the freezing crystallization salt-forming system to respectively obtain crystalline sodium sulfate and mother liquor, and the mother liquor returns to the freezing crystallization salt-forming system;
and the dryer is connected with the centrifugal machine, and the crystalline sodium sulfate obtained by the separation of the centrifugal machine is dried by the dryer to obtain a finished product of sodium sulfate.
2. The wet-process vanadium recycling wastewater resource utilization system according to claim 1, wherein the pretreatment unit further comprises a filter press, the sludge tank is connected with the filter press, sludge in the sludge tank is subjected to filter pressing by the filter press to obtain a second filtrate and a sludge cake, the filter press is connected with the regulating reservoir, and the second filtrate generated by the filter press can be returned to the regulating reservoir for recycling.
3. The wet-process vanadium recovery wastewater resource utilization system according to claim 2, characterized in that the sludge cake produced by the filter press is transported outside.
4. The wet vanadium recovery wastewater resource utilization system according to claim 1, 2 or 3, wherein the ammonia water storage component is connected to the combination tank, and the ammonia gas absorbed in the super ammonia absorber can be sent to the ammonia water storage component to be made into ammonia water; when the concentration of the ammonia water is lower, part of the ammonia water returns to the combination tank for concentration again.
5. The wet vanadium recovery wastewater resource utilization system according to claim 1, 2 or 3, wherein the ammonia water storage assembly comprises a primary ammonia water tank, a secondary ammonia water tank and a tail gas absorption tower which are connected with the super ammonia absorber, the primary ammonia water tank, the secondary ammonia water tank and the tail gas absorption tower are sequentially connected, and the primary ammonia water tank is connected with the combination tank.
6. The wet-process vanadium recovery wastewater resource utilization system according to claim 4, wherein the ammonia water storage assembly comprises a primary ammonia water tank, a secondary ammonia water tank and a tail gas absorption tower which are connected with the super ammonia absorber, the primary ammonia water tank, the secondary ammonia water tank and the tail gas absorption tower are sequentially connected, and the primary ammonia water tank is connected with the combination tank.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113562743A (en) * | 2021-08-19 | 2021-10-29 | 上海大学(浙江·嘉兴)新兴产业研究院 | Ammonia gas concentration and recovery device, barium titanate production equipment and barium titanate production method |
| CN116462380A (en) * | 2023-06-20 | 2023-07-21 | 世韩(天津)节能环保科技有限公司 | Catalyst wastewater treatment system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113562743A (en) * | 2021-08-19 | 2021-10-29 | 上海大学(浙江·嘉兴)新兴产业研究院 | Ammonia gas concentration and recovery device, barium titanate production equipment and barium titanate production method |
| CN116462380A (en) * | 2023-06-20 | 2023-07-21 | 世韩(天津)节能环保科技有限公司 | Catalyst wastewater treatment system |
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