CN220364460U - System for be used for industrial waste water to remove silicon and dealkalize and soften - Google Patents
System for be used for industrial waste water to remove silicon and dealkalize and soften Download PDFInfo
- Publication number
- CN220364460U CN220364460U CN202321831864.9U CN202321831864U CN220364460U CN 220364460 U CN220364460 U CN 220364460U CN 202321831864 U CN202321831864 U CN 202321831864U CN 220364460 U CN220364460 U CN 220364460U
- Authority
- CN
- China
- Prior art keywords
- carbon dioxide
- wastewater
- exchange bed
- ion resin
- resin exchange
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000010842 industrial wastewater Substances 0.000 title claims abstract description 16
- 229910052710 silicon Inorganic materials 0.000 title description 8
- 239000010703 silicon Substances 0.000 title description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 104
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000002351 wastewater Substances 0.000 claims abstract description 63
- 239000011347 resin Substances 0.000 claims abstract description 58
- 229920005989 resin Polymers 0.000 claims abstract description 58
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 53
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 53
- 238000001471 micro-filtration Methods 0.000 claims abstract description 51
- 239000012528 membrane Substances 0.000 claims abstract description 49
- 239000011734 sodium Substances 0.000 claims abstract description 45
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 45
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 150000002500 ions Chemical class 0.000 claims abstract description 30
- 229910001415 sodium ion Inorganic materials 0.000 claims abstract description 29
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 21
- 238000002425 crystallisation Methods 0.000 claims abstract description 13
- 230000008025 crystallization Effects 0.000 claims abstract description 13
- 238000001704 evaporation Methods 0.000 claims abstract description 8
- 230000008020 evaporation Effects 0.000 claims abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 5
- 239000000945 filler Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 238000007664 blowing Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 24
- 235000012239 silicon dioxide Nutrition 0.000 abstract description 12
- 239000000377 silicon dioxide Substances 0.000 abstract description 12
- 238000000034 method Methods 0.000 description 11
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 7
- 239000010802 sludge Substances 0.000 description 6
- 239000003814 drug Substances 0.000 description 4
- 238000005189 flocculation Methods 0.000 description 4
- 230000016615 flocculation Effects 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The utility model provides a system for desilication and dealkalization softening of industrial wastewater, and relates to the technical field of water treatment. The utility model provides a system for desilication and dealkalization softening of industrial wastewater, which comprises: the device comprises a sodium metaaluminate dosing reaction concentration device, a tubular microfiltration membrane water producing tank, an H ion resin exchange bed, a Na ion resin exchange bed and a carbon dioxide removal device. After the wastewater is treated by the system, alkalinity, hardness and silicon dioxide can be removed at the same time, the silicon dioxide can be reduced to within 10mg/L, the hardness is hardly detected, the alkalinity can be reduced to within 20mg/L, and the effluent can directly enter a reverse osmosis and evaporation crystallization unit.
Description
Technical Field
The utility model relates to the technical field of water treatment, in particular to a system for desilication and dealkalization softening of industrial wastewater.
Background
In recent years, along with the improvement of environmental protection requirements, higher and deeper requirements are provided for the treatment of industrial wastewater, and the realization of high-multiple concentration and recycling of industrial wastewater and zero wastewater discharge become industry development trends. Reverse osmosis and evaporative crystallization processes are often adopted in the concentration and wastewater zero emission processes, but the alkalinity, hardness and silicon dioxide in the wastewater have serious influence on the normal operation of the system, and a pretreatment unit is required to be added to reduce the content of the wastewater. At present, an H ion resin exchange bed or a Na ion resin exchange bed is often adopted as a dealkalization softening pretreatment system; adopts magnesium agent or sodium metaaluminate agent, and cooperates with flocculation precipitation and filtration technology as pretreatment system for removing silicon dioxide. However, the combination of the H ion resin exchange bed and the decarbonizer can simultaneously remove alkalinity and hardness, but the pH of the wastewater can continuously fluctuate in the operation process, and the pH is regulated to be an operation difficulty; although the Na ion resin exchange bed has no pH fluctuation, the alkalinity in the wastewater cannot be removed at the same time in the operation process; the magnesium agent needs to be subjected to desilication in an alkaline environment with the pH value being more than 10.5, and the pH value needs to be adjusted back, so that the desilication effect is not obvious; although the pH of sodium metaaluminate can be smoothly carried out between 7 and 9 and the silicon dioxide can be reduced to be within 10mg/L, the sodium metaaluminate can enter a reverse osmosis and evaporation crystallization unit only by carrying out auxiliary treatment through a series of units such as flocculation, precipitation, filtration, ultrafiltration and the like.
In view of this, the present utility model has been made.
Disclosure of Invention
The utility model aims to provide a system for desilication and dealkalization softening of industrial wastewater, which aims to solve at least one of the problems.
In a first aspect, the present utility model provides a system for desilication and dealkalization softening of industrial wastewater, comprising: the device comprises a sodium metaaluminate dosing reaction concentration device 1, a tubular micro-filtration membrane device 2, a tubular micro-filtration membrane water production tank 3, an H ion resin exchange bed 4, a Na ion resin exchange bed 5 and a carbon dioxide removal device 7;
the sodium metaaluminate dosing reaction concentration device 1, the tubular micro-filtration membrane device 2 and the tubular micro-filtration membrane water production tank 3 are sequentially communicated;
the sodium metaaluminate dosing reaction concentration device 1 is used for the reaction of wastewater and sodium metaaluminate;
the tubular micro-filtration membrane device 2 is used for filtering the wastewater from the sodium metaaluminate dosing reaction concentration device 1;
the tubular micro-filtration membrane water producing tank 3 is used for collecting the wastewater filtered by the tubular micro-filtration membrane device 2;
the H ion resin exchange bed 4 and the Na ion resin exchange bed 5 are connected in parallel and are used for removing the alkalinity and hardness of the wastewater; the upstream of the H ion resin exchange bed 4 and the Na ion resin exchange bed 5 are communicated with a water outlet pipeline of the tubular microfiltration membrane water producing tank 3, and the downstream is communicated with a water inlet of the carbon dioxide removing device 7;
the carbon dioxide removal device 7 is used for removing free carbon dioxide in the wastewater.
As a further technical scheme, the sodium metaaluminate dosing reaction concentration device 1 is provided with a wastewater inlet 101 and a sodium metaaluminate dosing port 102.
As a further technical scheme, the tubular microfiltration membrane device 2 is provided with a concentrated water outlet for discharging concentrated muddy water.
As a further technical scheme, the device also comprises a pipeline mixer 6;
the pipe mixer 6 is located downstream of the H ion resin exchange bed 4 and Na ion resin exchange bed 5 and upstream of the carbon dioxide removal device 7, and is used for mixing the wastewater treated by the H ion resin exchange bed 4 and Na ion resin exchange bed 5.
As a further technical scheme, the carbon dioxide removal device 7 is filled with a filler; the top of the carbon dioxide removal device 7 is provided with a carbon dioxide outlet and a wastewater spraying device; the bottom of the carbon dioxide removal device 7 is provided with an air inlet for the blowing-in of air.
As a further technical scheme, the carbon dioxide removing device 7 is a carbon dioxide remover.
As a further technical scheme, the water collecting tank 8 is also included;
the water collection tank 8 is communicated with the carbon dioxide removal device 7 through a pipeline and is used for collecting the wastewater treated by the carbon dioxide removal device 7.
As a further technical scheme, the device also comprises a reverse osmosis device; the reverse osmosis device is communicated with the water collection tank 8 through a pipeline.
As a further technical scheme, the device also comprises an evaporation crystallization device; the evaporation crystallization device is communicated with a water concentration port pipeline of the reverse osmosis device.
Compared with the prior art, the utility model has the following beneficial effects:
the system for removing silicon and softening dealkalized industrial wastewater provided by the utility model adopts the tubular microfiltration membrane silicon removing device to replace the traditional flocculation, precipitation, multi-medium filtration and ultrafiltration silicon removing system, so that the treatment effect is obviously improved, and the system plays a positive role in shortening the process chain, reducing the occupied area and reducing the cost; the parallel connection process of the H ion resin exchange bed and the Na ion resin exchange bed replaces the traditional single resin bed dealkalization softening process, can simultaneously remove alkalinity and hardness, reduces the dosage of the regenerated and alkali-regulating medicament while dealkalizing and softening, and reduces the running cost of the system. After the wastewater is treated by the system, alkalinity, hardness and silicon dioxide can be removed at the same time, the silicon dioxide can be reduced to within 10mg/L, the hardness is hardly detected, the alkalinity can be reduced to within 20mg/L, and the effluent can directly enter a reverse osmosis and evaporation crystallization unit.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present utility model, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 is a system for desilication and dealkalization softening of industrial wastewater provided in example 1 of the present utility model.
Icon: 1-sodium metaaluminate dosing reaction concentration device; 101-a wastewater inlet; 102-a sodium metaaluminate dosing port; 103-a sludge discharge outlet; 2-tubular microfiltration membrane device; 3-a water producing tank of a tubular microfiltration membrane; a 4-H ion resin exchange bed; a 5-Na ion resin exchange bed; 6-pipe mixer; 7-a carbon dioxide removal device; 701-carbon dioxide outlet; 702-air inlet; 8-a water collecting tank.
Detailed Description
Embodiments of the present utility model will be described in detail below with reference to embodiments and examples, but it will be understood by those skilled in the art that the following embodiments and examples are only for illustrating the present utility model and should not be construed as limiting the scope of the present utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model. The specific conditions are not specified, and the process is carried out according to conventional conditions or conditions suggested by manufacturers. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
In a first aspect, the present utility model provides a system for desilication and dealkalization softening of industrial wastewater, comprising: the device comprises a sodium metaaluminate dosing reaction concentration device 1, a tubular micro-filtration membrane device 2, a tubular micro-filtration membrane water production tank 3, an H ion resin exchange bed 4, a Na ion resin exchange bed 5 and a carbon dioxide removal device 7;
the sodium metaaluminate dosing reaction concentration device 1, the tubular micro-filtration membrane device 2 and the tubular micro-filtration membrane water production tank 3 are sequentially communicated;
the sodium metaaluminate dosing reaction concentration device 1 is used for the reaction of wastewater and sodium metaaluminate;
the tubular micro-filtration membrane device 2 is used for filtering the wastewater from the sodium metaaluminate dosing reaction concentration device 1;
the tubular micro-filtration membrane water producing tank 3 is used for collecting the wastewater filtered by the tubular micro-filtration membrane device 2;
the H ion resin exchange bed 4 and the Na ion resin exchange bed 5 are connected in parallel and are used for removing the alkalinity and hardness of the wastewater; the upstream of the H ion resin exchange bed 4 and the Na ion resin exchange bed 5 are communicated with a water outlet pipeline of the tubular microfiltration membrane water producing tank 3, and the downstream is communicated with a water inlet of the carbon dioxide removing device 7;
the carbon dioxide removal device 7 is used for removing free carbon dioxide in the wastewater.
The harsh requirements of alkalinity, hardness and silicon dioxide are met according to reverse osmosis concentration recycling and zero emission of evaporative crystallization. The system for removing silicon and softening dealkalized industrial wastewater provided by the utility model adopts the tubular microfiltration membrane silicon removing device to replace the traditional flocculation, precipitation, multi-medium filtration and ultrafiltration silicon removing system, so that the treatment effect is obviously improved, and the system plays a positive role in shortening the process chain, reducing the occupied area and reducing the cost; the parallel connection process of the H ion resin exchange bed and the Na ion resin exchange bed replaces the traditional single resin bed dealkalization softening process, can simultaneously remove alkalinity and hardness, reduces the dosage of the regenerated and alkali-regulating medicament while dealkalizing and softening, and reduces the running cost of the system. After the wastewater is treated by the system, alkalinity, hardness and silicon dioxide can be removed at the same time, the silicon dioxide can be reduced to within 10mg/L, the hardness is hardly detected, the alkalinity can be reduced to within 20mg/L, and the effluent can directly enter a reverse osmosis and evaporation crystallization unit.
In this embodiment, the industrial wastewater may be, for example, coal gas wastewater.
In some preferred embodiments, the sodium metaaluminate dosing reaction concentration device 1 is provided with a wastewater inlet 101 and a sodium metaaluminate dosing port 102.
Wherein, the wastewater inlet 101 is used for introducing wastewater into the sodium metaaluminate dosing reaction concentration device 1; the sodium metaaluminate dosing port 102 is used for adding sodium metaaluminate into the sodium metaaluminate dosing reaction concentration device 1.
Only sodium metaaluminate medicament is added in the reaction process, so that the use of medicaments such as traditional PAC and PAM is reduced.
In some preferred embodiments, the pH of the reaction in the sodium metaaluminate dosing reaction concentration device 1 is 7-9, and the reaction time is 30-40min.
In some preferred embodiments, the tubular microfiltration membrane device 2 is provided with a concentrate discharge for the discharge of concentrated muddy water.
After the wastewater is treated by the tubular micro-filtration membrane device 2, the clear water on the water producing side of the tubular micro-filtration membrane flows into the water producing tank 3 of the tubular micro-filtration membrane, and the muddy water on the concentrated water side of the tubular micro-filtration membrane is discharged into a sludge treatment system after repeated circulating concentration.
In some preferred embodiments, a pump is further arranged downstream of the tubular microfiltration membrane water producing tank 3, and after the pump is lifted and split, one part of the water enters the H ion resin exchange bed, and the other part of the water enters the Na ion resin exchange bed.
Wherein the flow of wastewater in the tubular micro-filtration membrane water producing tank 3 is Q, and the flow of the H ion resin exchange bed is Q H Na ion resin exchange bed flow rate is Q Na 。
In the scheme, the flow distribution not only can realize manual control, but also can realize automatic control through a regulating valve, and the flow distribution entering the H ion resin exchange bed and the Na ion resin exchange bed is related to raw water quality and treatment requirements and can be generally calculated according to the following formula:
(1)
(2)
wherein: q: waste water flow, m 3 /h；
Q H : flow m into device D 3 /h；
Q Na : flow m into device E 3 /h；
[HCO 3 - ]: alkalinity in the wastewater, molar concentration of equivalent ions, mmol/L;
[SO 4 2- ]: SO in waste water 4 2- Equivalent ion molar concentration means mmol/L;
[CL - ]: CL in wastewater - Equivalent ion molar concentration means mmol/L;
A r : the residual alkalinity of the softened water after mixing is generally 0.2 to 0.5mmol/L.
In some preferred embodiments, further comprising a pipe mixer 6;
the pipe mixer 6 is located downstream of the H ion resin exchange bed 4 and Na ion resin exchange bed 5 and upstream of the carbon dioxide removal device 7, and is used for mixing the wastewater treated by the H ion resin exchange bed 4 and Na ion resin exchange bed 5.
In some preferred embodiments, the carbon dioxide removal device 7 is filled with a filler; the top of the carbon dioxide removal device 7 is provided with a carbon dioxide outlet and a wastewater spraying device; the bottom of the carbon dioxide removal device 7 is provided with an air inlet for the blowing-in of air.
In some preferred embodiments, the carbon dioxide removal device 7 is a carbon dioxide remover.
In some preferred embodiments, a water collection tank 8 is also included;
the water collection tank 8 is communicated with the carbon dioxide removal device 7 through a pipeline and is used for collecting the wastewater treated by the carbon dioxide removal device 7.
In some preferred embodiments, a reverse osmosis device is also included; the reverse osmosis device is communicated with the water collection tank 8 through a pipeline and is used for removing salt in the wastewater and concentrating the salt in the wastewater.
In some preferred embodiments, the apparatus further comprises an evaporative crystallization apparatus; the evaporation crystallization device is communicated with a water concentration port pipeline of the reverse osmosis device and is used for recycling salt crystals in concentrated wastewater obtained after treatment of the reverse osmosis device.
The utility model is further illustrated by the following specific examples and comparative examples, however, it should be understood that these examples are for the purpose of illustration only in greater detail and should not be construed as limiting the utility model in any way.
Example 1
A system for desilication and dealkalization softening of industrial wastewater is shown in figure 1, and comprises a sodium metaaluminate dosing reaction concentration device 1, a tubular microfiltration membrane device 2, a tubular microfiltration membrane water production tank 3, a parallel H ion resin exchange bed 4, a Na ion resin exchange bed 5, a pipeline mixer 6, a carbon dioxide removal device 7 and a water collecting tank 8 which are sequentially communicated through pipelines;
wherein, the sodium metaaluminate dosing reaction concentration device 1 is provided with a wastewater inlet 101, a sodium metaaluminate dosing port 102 and a sludge outlet 103; the tubular micro-filtration membrane device 2 is provided with a concentrated water outlet and a water producing port; the water inlet of the water producing tank 3 of the tubular micro-filtration membrane is communicated with a water producing port pipeline of the tubular micro-filtration membrane device 2; the carbon dioxide removal device 7 is a carbon dioxide remover, the carbon dioxide remover is filled with a filler, the top is provided with a carbon dioxide outlet 701 and a waste water spraying device, and the bottom is provided with an air inlet 702 for blowing air in.
The wastewater treatment flow of the device is as follows:
the wastewater enters a sodium metaaluminate dosing reaction concentration device 1 from a wastewater inlet 101, sodium metaaluminate is added into the sodium metaaluminate dosing reaction concentration device 1 from a sodium metaaluminate dosing port 102, so that the pH is controlled between 7 and 9, after the sodium metaaluminate and the wastewater effectively react for about 35 minutes in the sodium metaaluminate dosing reaction concentration device 1, a mud-water mixture is pumped into a tubular micro-filtration membrane device 2, the mud-water mixture circulates in a large flow rate in the tubular micro-filtration membrane device 2, clear water on the water production side of the tubular micro-filtration membrane device 2 flows into a tubular micro-filtration membrane water production tank 3, and muddy water on the concentrated water side of the tubular micro-filtration membrane device 2 is discharged into a sludge treatment system after repeated circulating concentration; the sludge in the sodium metaaluminate dosing reaction concentration device 1 is discharged from the sludge discharge outlet 103.
After the wastewater flowing out of the tubular microfiltration membrane water producing tank 3 is lifted and split by a pump, one part of the wastewater enters the H ion resin exchange bed 4, and the other part of the wastewater enters the Na ion resin exchange bed 5. The wastewater passes through the H ion resin exchange bed 4, the effluent is acidic, passes through the Na ion resin exchange bed 5, and is alkaline, and the two flows of water are mixed by the mixer 6 and then enter the carbon dioxide removal device 7.
In the carbon dioxide removal device 7, wastewater enters a top spraying device, is uniformly sprayed down, forms a water film layer when being filled, contacts with blast air at the lower part, discharges separated carbon dioxide gas from a carbon dioxide discharge outlet 701, and the produced water enters a water collection tank 8, wherein the water in the water collection tank 8 is used for subsequent reverse osmosis treatment or evaporative crystallization treatment.
Test example 1
The system provided in the embodiment 1 is applied to the treatment of wastewater before reverse osmosis in a concentration section of a certain coal gas wastewater salt separation zero emission project, and the water inlet and outlet indexes are as follows:
| sequence number | Project | Unit (B) | Water quality of inlet water | Effluent quality |
| 1 | SiO 2 | mg/L | ≤80 | ≤7 |
| 2 | Turbidity degree | NTU | ≤20 | ≤1 |
| 3 | Total alkalinity | mg/L | ≤120 | ≤20 |
| 4 | Total hardness of | mg/L | ≤350 | Can not be detected |
(1) After the sodium metaaluminate dosing reaction concentration device and the tubular micro-filtration mud-water separation, the silicon dioxide content is reduced to 7mg/L from 80mg/L or less of inlet water; the turbidity is reduced to 1mg/L from less than or equal to 20 mg/L.
(2) After passing through an H-Na ion resin exchange bed parallel system and a carbon dioxide removal device, the total hardness is reduced from less than or equal to 350mg/L of inlet water to no detection; the alkalinity is reduced to within 20mg/L from the inlet water of less than or equal to 120 mg/L.
(3) The effluent directly enters a reverse osmosis device of the concentration section.
Test example 2
The system provided in the embodiment 1 is applied to the treatment of wastewater before reverse osmosis in a concentration section of a comprehensive wastewater desalination zero emission project in coal chemical industry, and the water quality indexes of inlet and outlet are as follows:
| sequence number | Project | Unit (B) | Water quality of inlet water | Effluent quality |
| 1 | SiO 2 | mg/L | ≤120 | ≤10 |
| 2 | Turbidity degree | NTU | ≤15 | ≤1 |
| 3 | Total alkalinity | mg/L | ≤80 | ≤15 |
| 4 | Total hardness of | mg/L | ≤470 | Can not be detected |
(1) After the sodium metaaluminate dosing reaction concentration device and the tubular micro-filtration mud-water separation, the silicon dioxide content is reduced to within 10mg/L from the content of water which is less than or equal to 120 mg/L; the turbidity is reduced to 1mg/L from less than or equal to 15 mg/L.
(2) After passing through an H-Na ion resin exchange bed parallel system and a carbon dioxide removal device, the total hardness is reduced from 470mg/L or less of inlet water to no detection; the alkalinity is reduced to 15mg/L from 80mg/L or less of the inlet water.
(3) The effluent directly enters a reverse osmosis device of the concentration section.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (9)
1. A system for desilication and dealkalization softening of industrial wastewater, comprising: the device comprises a sodium metaaluminate dosing reaction concentration device (1), a tubular micro-filtration membrane device (2), a tubular micro-filtration membrane water production tank (3), an H ion resin exchange bed (4), a Na ion resin exchange bed (5) and a carbon dioxide removal device (7);
the sodium metaaluminate dosing reaction concentration device (1), the tubular micro-filtration membrane device (2) and the tubular micro-filtration membrane water production tank (3) are sequentially communicated;
the sodium metaaluminate dosing reaction concentration device (1) is used for reacting wastewater with sodium metaaluminate;
the tubular micro-filtration membrane device (2) is used for filtering the wastewater from the sodium metaaluminate dosing reaction concentration device (1);
the tubular microfiltration membrane water production tank (3) is used for collecting the wastewater filtered by the tubular microfiltration membrane device (2);
the H ion resin exchange bed (4) and the Na ion resin exchange bed (5) are connected in parallel and are used for removing the alkalinity and hardness of the wastewater; the upstream of the H ion resin exchange bed (4) and the Na ion resin exchange bed (5) are communicated with a water outlet pipeline of the tubular microfiltration membrane water production tank (3), and the downstream is communicated with a water inlet of the carbon dioxide removal device (7);
the carbon dioxide removal device (7) is used for removing free carbon dioxide in the wastewater.
2. The system according to claim 1, wherein the sodium metaaluminate dosing reaction concentration device (1) is provided with a wastewater inlet (101) and a sodium metaaluminate dosing port (102).
3. The system according to claim 1, characterized in that the tubular microfiltration membrane device (2) is provided with a concentrate outlet for the discharge of concentrated muddy water.
4. The system according to claim 1, further comprising a pipe mixer (6);
the pipeline mixer (6) is positioned at the downstream of the H ion resin exchange bed (4) and the Na ion resin exchange bed (5) and at the upstream of the carbon dioxide removing device (7) and is used for mixing the wastewater treated by the H ion resin exchange bed (4) and the Na ion resin exchange bed (5).
5. The system according to claim 1, characterized in that the carbon dioxide removal device (7) is filled with a filler; the top of the carbon dioxide removal device (7) is provided with a carbon dioxide outlet and a wastewater spraying device; the bottom of the carbon dioxide removal device (7) is provided with an air inlet for blowing air in.
6. The system according to claim 5, characterized in that the carbon dioxide removal device (7) is a carbon dioxide remover.
7. The system according to claim 1, further comprising a water collection tank (8);
the water collection tank (8) is communicated with the carbon dioxide removal device (7) through a pipeline and is used for collecting wastewater treated by the carbon dioxide removal device (7).
8. The system of claim 7, further comprising a reverse osmosis device; the reverse osmosis device is communicated with a water collecting tank (8) through a pipeline.
9. The system of claim 8, further comprising an evaporative crystallization device; the evaporation crystallization device is communicated with a water concentration port pipeline of the reverse osmosis device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321831864.9U CN220364460U (en) | 2023-07-12 | 2023-07-12 | System for be used for industrial waste water to remove silicon and dealkalize and soften |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321831864.9U CN220364460U (en) | 2023-07-12 | 2023-07-12 | System for be used for industrial waste water to remove silicon and dealkalize and soften |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220364460U true CN220364460U (en) | 2024-01-19 |
Family
ID=89516434
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321831864.9U Active CN220364460U (en) | 2023-07-12 | 2023-07-12 | System for be used for industrial waste water to remove silicon and dealkalize and soften |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220364460U (en) |
-
2023
- 2023-07-12 CN CN202321831864.9U patent/CN220364460U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112551787A (en) | Mine water deep treatment system and method for treating mine water | |
| CN109775939B (en) | Zero-discharge and salt-separation crystallization system and method for coal chemical industry sewage | |
| CN105384316A (en) | Electronic industrial fluoride, ammonia and nitrogen-containing wastewater treatment method | |
| CN108793642A (en) | A kind of dyeing waste water advanced treatment system and processing method | |
| CN109851139B (en) | High-salt wastewater softening and concentrating device and method | |
| CN105645663A (en) | A water treatment method combining flocculation, counter-current ozone air floatation and biofiltration in order and a device used in the method | |
| CN115231743A (en) | Low-cost desulfurization wastewater treatment method and system | |
| CN111153531A (en) | Liquid crystal display panel production plant fluorine-containing wastewater treatment device and process | |
| CN118026473A (en) | Sewage zero discharge treatment method and device for filter production line | |
| CN112573720A (en) | Thermal power plant desulfurization wastewater zero-discharge system and method | |
| CN220364460U (en) | System for be used for industrial waste water to remove silicon and dealkalize and soften | |
| CN208762364U (en) | Dyeing waste water advanced treatment system | |
| CN111115661A (en) | Nitric acid wastewater treatment system and method | |
| CN215559636U (en) | Wastewater treatment system | |
| CN215559437U (en) | Wastewater treatment system | |
| CN112575196B (en) | Method and equipment for extracting high-purity titanium liquid from olefin polymerization industrial waste acid sludge | |
| CN112678866B (en) | Recycling treatment method of olefin polymerization industrial waste acid residues | |
| CN211871651U (en) | Liquid crystal display panel manufacturing plant fluorine-containing wastewater treatment device | |
| CN113493279A (en) | Low-cost recycling cooperative treatment method and system for negative-hardness wastewater | |
| CN208279427U (en) | A kind of processing of desulfurization wastewater and chemical industry for making chlorine and alkali technique link processing system | |
| CN112939368A (en) | Circulating water sewage treatment and recycling method with high desalting rate | |
| CN205821040U (en) | Desulfurization wastewater advanced treating membrance separation is combined Zero discharging system by a kind of full embrane method | |
| CN113087197A (en) | Method for treating and recycling circulating water and sewage | |
| CN214829693U (en) | High-salt high-ammonia-nitrogen high-hardness wastewater treatment system | |
| CN214088122U (en) | Zero discharge system of desulfurization waste water of steam power plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |