CN115947500A - Treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese - Google Patents
Treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese Download PDFInfo
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Abstract
The invention relates to a treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese, belonging to the technical field of wastewater treatment and metal smelting. The invention relates to a treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese, which comprises the following specific steps: (1) Mixing the treated C272 manganese raffinate P507 cobalt raffinate P507 nickel raffinate, filtering and deoiling for later use; (2) Performing ion exchange on the mixed solution obtained in the step (1) to obtain sodium sulfate wastewater and saturated resin; (3) Concentrating the sodium sulfate wastewater in the step (2) through a reverse osmosis membrane to obtain concentrated sodium sulfate and fresh water; (4) Evaporating the concentrated sodium sulfate solution in the step (3) by an MVR evaporator to obtain sodium sulfate crystallized salt solution and condensed water; (5) Separating the sodium sulfate crystallized salt solution obtained in the step (4) by a centrifuge to obtain sodium sulfate; (6) Regenerating the saturated resin in the step (2) to obtain concentrated nickel sulfate; (7) And (6) precipitating and filtering concentrated nickel sulfate step by step to obtain cobalt salt, nickel salt and manganese salt respectively.
Description
The invention relates to a treatment and recycling process of sodium sulfate wastewater containing heavy metals, in particular to a treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese, belonging to the technical field of wastewater treatment and metal smelting. Background art when ternary battery waste is used as a raw material to produce cobalt series products and ternary precursors of lithium battery anode materials, a leaching working section post-processes C272 manganese extraction, P507 cobalt extraction, P507 nickel extraction and other working procedures generate a large amount of raffinate waste water, the three kinds of raffinate waste water mainly contain valuable metals such as heavy metals of nickel (50-200 mg/L), cobalt (1-50 mg/L), manganese (100-500 mg/L) and sodium sulfate (30000-50000 mg/L), and the three kinds of raffinate waste water belong to high-salt inorganic waste water, and if the three kinds of raffinate waste water are directly discharged, serious pollution of surface water, underground water and even soil is caused, and the waste of limited resources is also caused; the traditional process for treating the heavy metal-containing wastewater generally carries out classification treatment or filtration after fractional precipitation under different pH conditions, and because the concentrations of high-valence metal nickel and cobalt in the feed liquid are relatively low and the feed liquid contains other impurities, the feed liquid has no direct recovery value, the metal ions and the total salt content of the treated wastewater cannot meet the current national and industrial water pollutant discharge standard, and the nickel-containing filter residue belongs to a class of pollutants (hazardous waste), the treatment cost is high.
Disclosure of Invention
The invention aims to provide a process for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese, so as to solve the problems in the background technology. The specific scheme of the invention is as follows:
a treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese comprises the following steps:
(1) Mixing the pretreated C272 manganese raffinate, P507 cobalt raffinate and P507 nickel raffinate, and further finely filtering and deoiling the mixed solution for later use.
(2) 3, using a 8% sulfuric acid solution with 2BV resin volume to carry out thin film distillation at the flow rate of 15 m/h and in a mode of middle-to-middle discharge after the thin film distillation, and discharging concentrated sulfuric acid nickel regeneration liquid with the pH value of the discharged liquid being more than or equal to 2 into a concentrated sulfuric acid nickel tank; and discharging the dilute nickel sulfate with the pH value less than 2 into a dilute nickel sulfate tank for later use. After regeneration is finished, washing the resin with pure water until the pH value is more than 6, wherein the resin is H-shaped; then passing through a resin column in a mode of feeding in and discharging out below 2.15BV of 4% sodium hydroxide solution of resin volume, and discharging transformation liquid with the PH value less than or equal to 11 into a concentrated sulfuric acid nickel tank; and discharging the dilute alkali liquor with the pH value of more than 11 into an alkali washing water tank for later use. After the transformation is finished, washing the solution by pure water until the pH value is less than 10, and finishing the regeneration and transformation and then using the ion exchanger for standby.
(3) Carrying out ion exchange adsorption on the mixed feed liquid obtained in the step (1) through the ion exchange resin regenerated and transformed in the step (2), allowing the sodium sulfate wastewater obtained after adsorption to enter an ion exchange rear liquid tank, detecting the adsorbed solution by a total manganese online analyzer in the adsorption process, and when Mn is contained 2+ The content is more than 0.5mg/L, the resin is adsorbed and saturated at the moment, the switching feed liquid enters a standby ion exchanger to operate, and the resin with saturated adsorption is obtained.
(4) And (4) further concentrating and desalting the sodium sulfate wastewater generated in the step (3) through an RO reverse osmosis device, concentrating to obtain a concentrated sodium sulfate solution, and simultaneously obtaining reverse osmosis fresh water and conveying the reverse osmosis fresh water to a pure water station for utilization as raw water.
(5) And (4) circularly evaporating the concentrated sodium sulfate solution concentrated in the step (4) through an MVR evaporator until the sodium sulfate solution is saturated and separated out to obtain sodium sulfate crystalline salt solution, and conveying the high-temperature condensate generated by evaporation to a pure water station to be used as raw water after the waste heat of the high-temperature condensate is utilized by an MVR preheater.
(6) And (5) centrifuging the saturated sodium sulfate crystallized salt solution obtained in the step (5) through a centrifugal machine to obtain sodium sulfate.
(7) And (3) regenerating and transforming the saturated resin obtained in the step (3) through the step (2).
(8) And (7) performing regeneration and transformation to obtain concentrated sulfuric acid nickel solution, and performing fractional precipitation and filtration to obtain cobalt salt, nickel salt and manganese salt.
Drawings
FIG. 1 is a schematic process flow diagram of a treatment and recycling process of sodium sulfate wastewater containing nickel, cobalt and manganese.
Detailed Description
To better illustrate the objects and technical solutions of the present invention, the present invention will be further described with reference to specific examples. It should be understood by those skilled in the art that the following specific examples are illustrative only and are not intended to limit the present invention.
Example 1: treatment and recycling process of sodium sulfate wastewater containing nickel, cobalt and manganese
(1) Collecting the pretreated C272 manganese raffinate, P507 cobalt raffinate and P507 nickel raffinate into a pre-ion exchange liquid tank, further fine filtering and deoiling the mixed liquid for later use to obtain a mixed liquid component (Ni) 2+ ：96mg/L，Co 2+ ：28mg/L，Mn 2+ ：352mg/L，Na + ：32750mg/L）
(2) 3, using one ion exchanger for dual purposes, namely respectively using 8% sulfuric acid solution with the volume amount of 2BV resin to pass through the resin at the flow rate of 15 m/h and in a mode of proceeding and discharging below, and discharging concentrated sulfuric acid nickel regeneration liquid with the pH value of discharge liquid being more than or equal to 2 into a concentrated sulfuric acid nickel groove; when the PH value of the discharged regeneration liquid is less than 2, discharging the dilute nickel sulfate regeneration liquid into a dilute nickel sulfate tank for later use in the following feeding and discharging mode. After regeneration is finished, washing the resin with pure water until the pH value is more than 6, wherein the resin is H-shaped; then, the H-type resin was converted into the Na-type resin by using a sodium hydroxide solution of 4% by volume based on 2.15BV of the resin, and the regenerated and washed ion exchange column was converted in a bottom-in-top-out manner. Discharging the transformation liquid with the PH value less than or equal to 11 discharged from the front section of the transformation process into a concentrated sulfuric acid nickel tank; and (4) discharging the dilute alkali liquor with the pH value of more than 11 into an alkali washing water tank for later use. After the transformation is finished, washing the solution by pure water until the pH value is less than 10, and finishing the regeneration and transformation and then using the ion exchanger for standby.
(3) Carrying out ion exchange adsorption on the mixed material liquid obtained in the step (1) through the ion exchange resin regenerated and transformed in the step (2), and obtaining sodium sulfate wastewater (Na) after adsorption + :31480 mg/L) into a liquid tank after ion exchange, detecting the solution after adsorption by an on-line analyzer of total manganese in the adsorption process, and when Mn is generated 2+ The content is more than 0.5mg/L, the resin is adsorbed and saturated at the moment, the switching feed liquid enters a standby ion exchanger to operate, and the resin with saturated adsorption is obtained.
(4) Sodium sulfate wastewater generated in the step (3)Further concentrating and desalting by RO reverse osmosis device to obtain concentrated sodium sulfate solution (Na) + :77650 mg/L) and reverse osmosis fresh water (Na) is obtained + :1283 mg/L) is conveyed to a pure water station to be used as raw water.
(5) Circularly evaporating the concentrated sodium sulfate solution in the step (4) through an MVR evaporator until the sodium sulfate solution is saturated and separated out to obtain sodium sulfate crystal salt solution, and conveying the high-temperature condensate generated by evaporation to a pure water station through an MVR preheater after utilizing waste heat to be used as raw water for utilization.
(6) And (5) centrifuging the saturated sodium sulfate crystallized salt solution obtained in the step (5) through a centrifugal machine to obtain sodium sulfate.
(7) And (3) regenerating and transforming the saturated resin obtained in the step (3) through the step (2).
(8) And (4) performing fractional precipitation and filtration on the concentrated nickel sulfate solution obtained by regeneration and transformation in the step (7) to obtain cobalt salt, nickel salt and manganese salt.
Test results 1:
| composition test sample | pH (dimensionless) | Ni 2+ (mg/L) | Co 2+ (mg/L) | Mn 2+ (mg/L) | Na + (mg/L) |
| Before ion exchange | 4.8 | 96 | 28 | 352 | 32750 |
| After ion exchange | 5.2 | 0.03 | 0.04 | 0.07 | 31480 |
| Concentrated nickel sulfate solution | 3.6 | 12775 | 3286 | 14342 | 10610 |
| RO concentrated solution | 5.9 | 0.10 | 0.12 | 0.16 | 77650 |
| Composition test sample | pH (dimensionless) | Ni 2+ (mg/L) | Co 2+ (mg/L) | Mn 2+ (mg/L) | Na + (mg/L) |
| RO fresh water | 5.0 | - | - | - | 1283 |
| MVR condensed water | 7.1 | - | - | - | 10 |
| Composition test sample | Water content (%) | Ni 2+ （g/kg） | Co 2+ （g/kg） | Mn 2+ （g/kg） | Na + （g/kg） |
| Sodium sulfate salt | 4.7 | 0.00053 | 0.00031 | 0.00076 | 386 |
Example 2: treatment and recycling process of sodium sulfate wastewater containing nickel, cobalt and manganese
(1) Collecting the pretreated C272 manganese raffinate, P507 cobalt raffinate and P507 nickel raffinate into a pre-ion exchange liquid tank, further fine filtering and deoiling the mixed liquid for later use to obtain a mixed liquid component (Ni) 2+ ：148mg/L，Co 2+ ：36mg/L，Mn 2+ ：412mg/L，Na + ：40961mg/L）
(2) 3, using one ion exchanger for dual purposes, namely respectively using 8% sulfuric acid solution with the volume amount of 2BV resin to pass through the resin at the flow rate of 15 m/h and in a mode of proceeding and discharging below, and discharging concentrated sulfuric acid nickel regeneration liquid with the pH value of discharge liquid being more than or equal to 2 into a concentrated sulfuric acid nickel groove; when the PH value of the discharged regeneration liquid is less than 2, discharging the dilute nickel sulfate regeneration liquid into a dilute nickel sulfate tank for later use in the following feeding and discharging mode.
After regeneration is finished, washing the resin with pure water until the pH value is more than 6, wherein the resin is H-shaped; then, the H-type resin was converted into the Na-type resin by using a sodium hydroxide solution of 4% by volume based on 2.15BV of the resin, and the regenerated and washed ion exchange column was converted in a bottom-in-top-out manner. Discharging the transformation liquid with the PH value less than or equal to 11 discharged from the front section of the transformation process into a concentrated sulfuric acid nickel tank; and discharging the dilute alkali liquor with the pH value of more than 11 into an alkali washing water tank for later use. After the transformation is finished, washing the solution by pure water until the pH value is less than 10, and finishing the regeneration and transformation and then using the ion exchanger for standby.
(3) Carrying out ion exchange adsorption on the mixed material liquid obtained in the step (1) through the ion exchange resin regenerated and transformed in the step (2), and obtaining sodium sulfate wastewater (Na) after adsorption + :36274 mg/L) enters an ion exchange rear liquid tank, and a total manganese on-line analyzer detects the solution after adsorption in the adsorption process, when Mn is in the solution 2+ The content is more than 0.5mg/L, the resin is adsorbed and saturated at the moment, the switching feed liquid enters a standby ion exchanger to operate, and the resin with saturated adsorption is obtained.
(4) Further concentrating and desalting the sodium sulfate wastewater generated in the step (3) by an RO reverse osmosis device to obtain concentrated sodium sulfate solution (Na) + :89730 mg/L) and simultaneously obtaining reverse osmosis fresh water (Na) + :1579 mg/L) is sent to a pure water station to be used as raw water.
(5) And (4) circularly evaporating the concentrated sodium sulfate solution in the step (4) through an MVR evaporator until the sodium sulfate solution is saturated and separated out to obtain sodium sulfate crystalline salt solution, and conveying the high-temperature condensate generated by evaporation to a pure water station to be used as raw water after waste heat of the high-temperature condensate is utilized by an MVR preheater.
(6) And (5) centrifuging the saturated sodium sulfate crystallized salt solution obtained in the step (5) through a centrifugal machine to obtain sodium sulfate.
(7) And (4) regenerating and transforming the saturated resin obtained in the step (3) through the step (2).
(8) And (7) regenerating and transforming to obtain concentrated nickel sulfate solution, and performing fractional precipitation and filtration to obtain cobalt salt, nickel salt and manganese salt.
Test results 2:
| composition test sample | pH (dimensionless) | Ni 2+ (mg/L) | Co 2+ (mg/L) | Mn 2+ (mg/L) | Na + (mg/L) |
| Before ion exchange | 4.4 | 148 | 36 | 412 | 40961 |
| After ion exchange | 4.8 | 0.04 | 0.03 | 0.06 | 36274 |
| Concentrated sulfuric acid nickel liquid | 3.5 | 13066 | 2710 | 13870 | 11860 |
| RO concentrated solution | 5.6 | 0.11 | 0.13 | 0.14 | 89730 |
| Composition test sample | pH (dimensionless) | Ni 2+ (mg/L) | Co 2+ (mg/L) | Mn 2+ (mg/L) | Na + (mg/L) |
| RO fresh water | 4.9 | - | - | - | 1579 |
| MVR condensed water | 7.1 | - | - | - | 10 |
| Composition test sample | Water content (%) | Ni 2+ （g/kg） | Co 2+ （g/kg） | Mn 2+ （g/kg） | Na + （g/kg） |
| Sodium sulfate salt | 4.6 | 0.00064 | 0.00038 | 0.00079 | 402 |
Example 3: treatment and recycling process of sodium sulfate wastewater containing nickel, cobalt and manganese
(1) Mixing the pretreated C272 manganese raffinate, P507 cobalt raffinate and P507 nickel raffinate into a pre-ion exchange liquid tank, fine filtering and deoiling the mixed liquid to obtain mixed liquid component (Ni) 2+ ：125mg/L，Co 2+ ：41mg/L，Mn 2+ ：457mg/L，Na + ：36890mg/L）
(2) 3, using one ion exchanger for dual purposes, namely respectively using 8% sulfuric acid solution with the volume amount of 2BV resin to pass through the resin at the flow rate of 15 m/h and in a mode of proceeding and discharging below, and discharging concentrated sulfuric acid nickel regeneration liquid with the pH value of discharge liquid being more than or equal to 2 into a concentrated sulfuric acid nickel groove; when the PH value of the discharged regeneration liquid is less than 2, discharging the dilute nickel sulfate regeneration liquid into a dilute nickel sulfate tank for later use in the following feeding and discharging mode. After regeneration is finished, washing the resin with pure water until the pH value is more than 6, wherein the resin is H-shaped; then the H type resin is converted into Na type by using sodium hydroxide solution with 4 percent of the volume amount of 2.15BV resin, and the regenerated and washed ion exchange column is converted by adopting a mode of feeding in and feeding out from the bottom. Discharging the transformation liquid with the PH value less than or equal to 11 discharged from the front section of the transformation process into a concentrated sulfuric acid nickel tank; and discharging the dilute alkali liquor with the pH value of more than 11 into an alkali washing water tank for later use. After the transformation is finished, washing the solution by pure water until the pH value is less than 10, and finishing the regeneration and transformation and then using the ion exchanger for standby.
(3) Carrying out ion exchange adsorption on the mixed material liquid obtained in the step (1) through the ion exchange resin regenerated and transformed in the step (2), and obtaining sodium sulfate wastewater (Na) after adsorption + :32560 mg/L) into ion exchange liquid tank, detecting the adsorbed solution with total manganese on-line analyzer during adsorption process, and detecting when Mn is present 2+ The content is more than 0.5mg/L, the resin is adsorbed and saturated at the moment, the switching feed liquid enters a standby ion exchanger to operate, and the resin with saturated adsorption is obtained.
(4) Further concentrating and desalting the sodium sulfate wastewater generated in the step (3) by an RO reverse osmosis device to obtain concentrated sodium sulfate solution (Na) + :79622 mg/L) and simultaneously obtaining reverse osmosis fresh water (Na) + :1369 mg/L) to a pure water station for use as raw water.
(5) And (4) circularly evaporating the concentrated sodium sulfate solution in the step (4) through an MVR evaporator until the sodium sulfate solution is saturated and separated out to obtain sodium sulfate crystalline salt solution, and conveying the high-temperature condensate generated by evaporation to a pure water station to be used as raw water after waste heat of the high-temperature condensate is utilized by an MVR preheater.
(6) And (5) centrifuging the saturated sodium sulfate crystallized salt solution obtained in the step (5) through a centrifugal machine to obtain sodium sulfate.
(7) And (3) regenerating and transforming the saturated resin obtained in the step (3) through the step (2).
(8) And (7) regenerating and transforming to obtain concentrated nickel sulfate solution, and performing fractional precipitation and filtration to obtain cobalt salt, nickel salt and manganese salt.
Test results 3:
| composition test sample | pH (dimensionless) | Ni 2+ (mg/L) | Co 2+ (mg/L) | Mn 2+ (mg/L) | Na + (mg/L) |
| Before ion exchange | 4.7 | 125 | 41 | 457 | 36890 |
| After ion exchange | 4.9 | 0.03 | 0.02 | 0.05 | 32560 |
| Concentrated nickel sulfate solution | 3.6 | 13828 | 3143 | 14382 | 12775 |
| RO concentrated solution | 0.10 | 0.12 | 0.13 | 79622 | |
| Composition test sample | pH (dimensionless) | Ni 2+ (mg/L) | Co 2+ (mg/L) | Mn 2+ (mg/L) | Na + (mg/L) |
| RO fresh water | 4.9 | - | - | - | 1369 |
| MVR condensed water | 7.0 | - | - | - | 18 |
| Composition test sample | Water content (%) | Ni 2+ （g/kg） | Co 2+ （g/kg） | Mn 2+ （g/kg） | Na + （g/kg） |
| Sodium sulfate salt | 4.7 | 0.00073 | 0.00044 | 0.00085 | 389 |
Claims (10)
1. A treatment and recovery process of sodium sulfate wastewater containing nickel, cobalt and manganese is characterized by comprising the following specific steps:
(1) Mixing the pretreated C272 manganese raffinate, P507 cobalt raffinate and P507 nickel raffinate, and further finely filtering and deoiling the mixed liquor for later use;
(2) 3, using a 8% sulfuric acid solution with 2BV resin volume to carry out thin film distillation at the flow rate of 15 m/h and in a mode of middle-to-middle discharge after the thin film distillation, and discharging concentrated sulfuric acid nickel regeneration liquid with the pH value of the discharged liquid being more than or equal to 2 into a concentrated sulfuric acid nickel tank; discharging the dilute nickel sulfate with the pH value less than 2 into a dilute nickel sulfate tank for later use, and after regeneration is finished, washing the dilute nickel sulfate with pure water until the pH value is more than 6, wherein the resin is H-shaped; then passing through a resin column in a mode of feeding in and discharging out below 4% sodium hydroxide solution with the volume amount of 2.15BV resin, and discharging transformation liquid with the PH value less than or equal to 11 into a concentrated sulfuric acid nickel tank; discharging dilute alkali liquor with the pH value of more than 11 into an alkali washing water tank for later use, washing the dilute alkali liquor with pure water after transformation is finished until the pH value is less than 10, and finishing the regeneration and transformation and then using an ion exchanger for later use;
(3) Carrying out ion exchange adsorption on the mixed feed liquid obtained in the step (1) through the ion exchange resin regenerated and transformed in the step (2), allowing the sodium sulfate wastewater obtained after adsorption to enter an ion exchange rear liquid tank, detecting the adsorbed solution by a total manganese online analyzer in the adsorption process, and when Mn is contained 2+ The content is more than 0.5mg/L, the resin is adsorbed and saturated at the moment, the switching feed liquid enters a standby ion exchanger to operate, and the resin with saturated adsorption is obtained;
(4) Further concentrating and desalting the sodium sulfate wastewater generated in the step (3) through an RO reverse osmosis device to obtain a concentrated sodium sulfate solution, and simultaneously obtaining reverse osmosis fresh water and conveying the reverse osmosis fresh water to a pure water station for use as raw water;
(5) Circularly evaporating the concentrated sodium sulfate solution concentrated in the step (4) through an MVR evaporator until the sodium sulfate solution is saturated and separated out to obtain sodium sulfate crystalline salt solution, and conveying the high-temperature condensate generated by evaporation to a pure water station to be used as raw water after waste heat of the high-temperature condensate is utilized by an MVR preheater;
(6) Centrifuging the saturated sodium sulfate crystallized salt solution obtained in the step (5) by a centrifugal machine to obtain sodium sulfate;
(7) Regenerating and transforming the saturated resin obtained in the step (3) through the step (2);
(8) And (7) obtaining concentrated sulfuric acid nickel liquid through regeneration and transformation, and obtaining cobalt salt, nickel salt and manganese salt through step-by-step precipitation and filtration.
2. The process of claim 1 for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese, which comprises the following steps: the fine filtration in the step (1) adopts a disc type self-cleaning filter, and the oil removal adopts a resin ZGSO107 oil removal filter.
3. The process for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese according to claim 1, wherein: and (3) adding the mixed liquor in the step (1) with the dilute nickel sulfate or alkali washing water collected in the step (2) to adjust the pH value to be more than or equal to 4.2, and then entering an ion exchanger.
4. The process for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese according to claim 1, wherein: the ion exchange resin in the step (2) is D851 macroporous styrene structure chelating resin.
5. The process of claim 1 for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese, which comprises the following steps: in the step (2), the regeneration and transformation wastewater of the ion exchanger is divided into concentrated nickel sulfate, dilute nickel sulfate and alkali washing water through a pH first limit value '2' and a pH second limit value '11'.
6. The process of claim 1 for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese, which comprises the following steps: part of the dilute nickel sulfate in the step (2) is used for preparing 8% sulfuric acid, and the rest is used for adjusting the pH value of the mixed solution in the step (1) to be more than or equal to 4.2; and (3) preparing 4% sodium hydroxide by using a part of the alkali washing water, and adjusting the pH value of the mixed solution obtained in the step (1) to be more than or equal to 4.2 by using the rest of the alkali washing water.
7. The process of claim 1 for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese, which comprises the following steps: in the step (3), in order to avoid leakage of the target heavy metal, mn is passed through the water outlet end of the ion exchanger 2+ Mn monitored by an on-line analyzer 2+ Judging that the resin is saturated when the content is more than 0.5mg/L, and switching the feed liquid to enter a standby ion exchanger for operation, wherein the principle is that the exchange selectivity of the ion exchange resin to target heavy metal ions is Ni < 2+ > Co < 2+ > Mn < 2+ > according to claim 4.
8. The process for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese according to claim 1, wherein: and (5) the RO device in the step (4) is a high-pressure reverse osmosis device with energy recovery.
9. The process for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese according to claim 1, wherein: in the step (5), the evaporation temperature of the MVR evaporator is 90 ℃, and the vacuum degree at the evaporation temperature is-0.03 MPa.
10. The process of claim 1 for treating and recovering sodium sulfate wastewater containing nickel, cobalt and manganese, which comprises the following steps: and (4) the centrifuge in the step (6) is an LWL type horizontal screw centrifuge.
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| CN116477805A (en) * | 2023-05-10 | 2023-07-25 | 苏州登峰环境工程有限公司 | Cobalt sulfamate electroless plating cleaning wastewater zero-emission treatment process |
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| CN116477805A (en) * | 2023-05-10 | 2023-07-25 | 苏州登峰环境工程有限公司 | Cobalt sulfamate electroless plating cleaning wastewater zero-emission treatment process |
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