CN211198889U - Strong brine deep purification device - Google Patents
Strong brine deep purification device Download PDFInfo
- Publication number
- CN211198889U CN211198889U CN201921731384.9U CN201921731384U CN211198889U CN 211198889 U CN211198889 U CN 211198889U CN 201921731384 U CN201921731384 U CN 201921731384U CN 211198889 U CN211198889 U CN 211198889U
- Authority
- CN
- China
- Prior art keywords
- water
- tank
- cod
- solid
- liquid separation
- 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
- 239000012267 brine Substances 0.000 title claims abstract description 63
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 63
- 238000000746 purification Methods 0.000 title claims abstract description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 232
- 238000000926 separation method Methods 0.000 claims abstract description 52
- 229910052710 silicon Inorganic materials 0.000 claims abstract description 42
- 239000010703 silicon Substances 0.000 claims abstract description 42
- 239000012528 membrane Substances 0.000 claims abstract description 13
- 238000001471 micro-filtration Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims description 72
- 239000007788 liquid Substances 0.000 claims description 60
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 40
- 239000010802 sludge Substances 0.000 claims description 29
- 230000003647 oxidation Effects 0.000 claims description 28
- 238000007254 oxidation reaction Methods 0.000 claims description 28
- 239000003814 drug Substances 0.000 claims description 23
- 238000001514 detection method Methods 0.000 claims description 17
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 5
- 229910044991 metal oxide Inorganic materials 0.000 claims description 4
- 150000004706 metal oxides Chemical class 0.000 claims description 4
- 239000002033 PVDF binder Substances 0.000 claims description 3
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 abstract description 27
- 238000005516 engineering process Methods 0.000 abstract description 5
- 239000000203 mixture Substances 0.000 abstract description 2
- 210000005056 cell body Anatomy 0.000 abstract 1
- 238000000034 method Methods 0.000 description 19
- 230000008569 process Effects 0.000 description 19
- 238000005345 coagulation Methods 0.000 description 11
- 230000015271 coagulation Effects 0.000 description 11
- 239000000126 substance Substances 0.000 description 11
- 238000001179 sorption measurement Methods 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 239000002920 hazardous waste Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000011403 purification operation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
Images
Landscapes
- Water Treatment By Sorption (AREA)
Abstract
The application provides a strong brine degree of depth purifier, this purifier looks into the composition difference of the strong brine of application occasion, carry out different purification operational mode, it has solved the strong brine softening and has removed silicon, remove COD inefficiency, the problem of the unsatisfied follow-up technology index of intaking of product water quality, simultaneously with whole processing technology flow device ization, abandon traditional big cell body and deposit, the filter separation, change formula microfiltration membrane separation into to, deep purification, and then improve total hardness, the clearance of soluble silicon and COD, strong brine degree of depth purification to the different salt content of different trades has the universal applicability, this strong brine degree of depth purifier operates stably, and convenient management, high treatment efficiency has important using value.
Description
Technical Field
The utility model relates to a contain salt waste water resource utilization field, in particular to high concentration contains purifier of salt and organic matter separation in salt waste water.
Background
The near zero emission work of high-salt-content wastewater in the industries of coal chemical industry, steel, petrochemical industry, paper making and the like is comprehensively developed. However, the harmless treatment of the mixed salt is a difficult problem, the traditional high-salt wastewater zero discharge process usually converts the mixed salt into mixed salt, the mixed salt is dissociated in the category of mixed salt hazardous wastes, if the treatment is carried out according to the treatment requirement of the hazardous wastes, each ton of the mixed salt needs more than 3000 yuan, the places for treating the hazardous wastes are very few, and the heavy metal and organic pollutants doped in the mixed salt are easy to dissolve and seep out when meeting water, so that the hidden danger of secondary pollution exists. Therefore, the requirement on high-precision material separation of the strong brine is higher and higher, excessive miscellaneous salt hazardous waste is avoided, and the strong brine is required to be refined in the softening silicon removal pretreatment process.
At present, the treatment process for separating materials of concentrated brine and recycling byproduct salt is mature, two newly released group standards of coal chemical industry byproduct sodium sulfate, namely coal chemical industry byproduct sodium chloride, have high standard requirements on crystalline salt, and the advanced purification treatment of the wastewater is also required by the high standard at the same time.
SUMMERY OF THE UTILITY MODEL
In view of this, to the problem that current device exists, this application provides a strong brine degree of depth purifier and processing technology, and this processing technology depends on the composition difference of the strong brine of application occasion, carries out different purification operation modes, and it has solved the strong brine softening and has removed silicon, removes COD inefficiency, and the product water quality of water can not satisfy the problem of follow-up technology index of intaking.
In order to achieve the above-mentioned purpose, the present application adopts the following scheme,
the embodiment of the application also provides a deep brine purification device which is characterized by comprising a COD removal device, a softening silicon removal device and a COD deep treatment device, wherein the softening silicon removal device is connected with the COD removal device and the COD deep treatment device through a pipeline and a liquid pump,
the COD removing device comprises a first reaction tank and a first concentration tank connected with the first reaction tank,
the first reaction tank is provided with a feeding port for feeding medicine,
a first water inlet for flowing in the strong brine to be treated,
a first water outlet through which the water treated by the first reaction tank flows to a first concentration tank,
the mixed liquid treated by the first concentration tank flows into a water inlet of a first solid-liquid separation device, the first produced water is separated by the first solid-liquid separation device and flows to a first intermediate water tank through a water outlet of the first intermediate water tank,
the softening desiliconization device comprises a second reaction tank, a second concentration tank connected with the second reaction tank, and a second solid-liquid separation device connected with the second concentration tank;
the second reaction tank is internally provided with a first pH detection device for detecting the pH value of water in the second reaction tank, a water outlet of the first reaction tank is connected with a water inlet of a second concentration tank through a pipeline and a pump, a water outlet of the second concentration tank is connected with a water inlet of a second solid-liquid separation device through a pipeline and a pump, a sludge outlet of the second concentration tank is connected with a sludge dewatering device through a pipeline and a sludge pump, the water treated by the second solid-liquid separation device is connected with a water inlet of a second middle water tank through a pipeline through a water production port of the second solid-liquid separation device, and a concentrated water port is connected with the second concentration tank through a pipeline;
the COD advanced purification device comprises: and the water inlet of the electrocatalytic oxidation device is connected with the second middle water tank, the water outlet of the electrocatalytic oxidation device is connected with the water inlet of the water producing pool, and the water produced by the electrocatalytic oxidation device flows into the water producing pool.
Preferably, the first solid-liquid separation device or the second solid-liquid separation device comprises a roll type microfiltration membrane, the membrane material is PVDF, the recovery rate is 95% -99%, the maximum water inlet pressure is 0.8Mpa, the maximum pressure drop is 0.12Mpa, the pH value is 2-10 during operation, and the solid content of the separated concentrated water is 1% -5%.
Preferably, the pH value of the reaction formula of the second reaction tank is between 10.5 and 11.5.
Preferably, the electrocatalytic oxidation device comprises a two-dimensional electrode or a three-dimensional electrode, wherein a layer of micron or submicron metal oxide is deposited on the surface of an electrode plate, and the COD removal rate is more than 90%.
Preferably, the water producing pond is provided with a second pH detection device.
Preferably, the dosing module of the deep brine purification device is electrically connected with the second pH detection device, and doses a medicament into the water producing tank based on information fed back by the second detection device so as to adjust water in the water producing tank to reclaimed water.
Preferably, the salt content of the concentrated brine is 6-25%, COD is more than or equal to 100 mg/L, the soluble silicon content is 80-200 mg/L (calculated by SiO 2), and the total hardness is more than 120 mg/L (calculated by CaCO 3).
The embodiment of the application provides a deep brine purification device which is characterized by comprising a COD removal device, a COD deep treatment device connected with the COD removal device through a pipeline and a liquid pump,
the COD removing device comprises a first reaction tank and a first concentration tank connected with the first reaction tank,
the first reaction tank is provided with a feeding port for feeding medicine,
a first water inlet for flowing in the strong brine to be treated,
a first water outlet through which the water treated by the first reaction tank flows to a first concentration tank,
the mixed liquid treated by the first concentration tank flows into a water inlet of a first solid-liquid separation device, the first produced water is separated by the first solid-liquid separation device and flows to a first intermediate water tank through a water outlet of the first intermediate water tank,
the COD advanced purification device comprises: the water inlet of the electrocatalytic oxidation device is connected with the first middle water tank, the water outlet of the electrocatalytic oxidation device is connected with the water inlet of the water producing pool, the produced water treated by the electrocatalytic oxidation device flows into the water producing pool, and the salt content of the strong brine is 6% -25%.
Preferably, the electrocatalytic oxidation device comprises a two-dimensional electrode or a three-dimensional electrode, wherein a layer of micron or submicron metal oxide is deposited on the surface of an electrode plate, and the COD removal rate is more than 90%.
The embodiment of the application provides a strong brine deep purification device, which is characterized in that the salt content of the strong brine is 6% -25%, the device comprises a softening and desiliconizing device, the device is provided with a second reaction tank and a water producing tank, wherein a water inlet of the second reaction tank is connected to a water outlet of an adjusting tank through a pipeline and a lift pump, a water outlet of the second reaction tank is connected to the water producing tank through a pipeline and a pump,
and a second pH detection device is arranged in the second reaction tank and used for detecting the pH value of water in the second reaction tank.
Advantageous effects
Compared with the prior art, the embodiment of the application has the following advantages:
1) solves the problems that the efficiency of softening and removing silicon and COD of strong brine is low, and the water quality of produced water can not meet the water inlet index of the subsequent process,
2) the whole process flow is in device arrangement, the traditional large tank body is abandoned, the rolled microfiltration membrane is used for separation and deep purification, the total hardness and the removal rate of soluble silicon and COD are improved, compared with the conventional treatment process for softening and removing silicon and COD by strong brine,
3) the device is simple to operate, small in occupied area and short in hydraulic retention time, has universal applicability to deep purification of strong brine with different salt contents in different industries, is stable in operation, convenient to manage and high in treatment efficiency, and has important application value.
Drawings
Other features and aspects of the present invention will become apparent from the following detailed description of exemplary embodiments, which proceeds with reference to the accompanying drawings.
The accompanying drawings, which are incorporated in and constitute a part of the specification, illustrate exemplary embodiments, features, and aspects of the present invention and, together with the description, serve to explain the principles of the invention.
FIG. 1 is a schematic flow diagram of a treatment process according to an embodiment of the present application;
fig. 2 is a schematic structural diagram of a purification apparatus according to an embodiment of the present application.
Description of numbering: the device comprises a regulating tank 101, a first reaction tank 102, a first concentration tank 103, a first scroll type microfiltration membrane solid-liquid separation device 104, a first intermediate water tank 105, a sludge dewatering device 106, a first chemical adding device 107, a regulating tank lift pump 108, a concentration tank water inlet pump 109, a first solid-liquid separation device water inlet pump 110, a second reaction tank water inlet pump 111, a first chemical adding pump 112, a second reaction tank 201, a second concentration tank 202, a second scroll type microfiltration membrane solid-liquid separation device 203, a second intermediate water tank 204, an electrocatalytic oxidation device 205, a water production tank 206, a second chemical adding device 207, a first softening desiliconization reaction pH detection device 208, a second concentration tank water inlet pump 209, a second scroll type microfiltration membrane solid-liquid separation device water inlet pump 210, an electrocatalytic oxidation device water inlet pump 211, a water production tank second pH detection device 212, a sludge conveying pump 213 and a second chemical adding pump 214.
Detailed Description
Various exemplary embodiments, features and aspects of the present invention will be described in detail below with reference to the accompanying drawings. In the drawings, like reference numbers can indicate functionally identical or similar elements. While the various aspects of the embodiments are presented in drawings, the drawings are not necessarily drawn to scale unless specifically indicated. By definition, in this embodiment reference will be made to tds (total dissolved solids), which refers to the total dissolved solids, also known as total salt content, including both inorganic and organic content. COD (chemical Oxygen demand) means that the chemical Oxygen demand is the amount of reducing substances to be oxidized in a water sample measured chemically.
The embodiment of the application provides a process for deeply purifying concentrated brine, which can be applied to different water qualities of the concentrated brine, and mainly comprises a stage of removing COD by adsorption coagulation and a stage of deeply purifying COD for treating the concentrated brine with high COD and low hardness, a stage of softening and removing silicon for treating the concentrated brine with low COD and high hardness, and a stage of removing silicon for treating the concentrated brine with low COD and high hardness, wherein the stage of removing COD by adsorption coagulation, a stage of softening and removing silicon for treating the concentrated brine with low COD and the stage of deeply purifying COD are included in the process of treating the concentrated brine, the treated produced water is returned to reclaimed water and then discharged, and the mechanism of returning to reclaimed water is adopted, and the pH value of the finally produced water is increased due to the fact that the pH value of the softening and removing silicon process in a second reaction tank is 10.5-11.5 (alkaline is returned to a reclaimed water environment), and the pH value of the finally produced water is adjusted to be neutral, namely, the pH value is equal to 7, in the embodiment of the application, the concentrated brine has the salt content of 6-25%, the total hardness of 100-L-500 mg/L (calculated by CaCO 80-3982), the total hardness of 100-3970 mg/2 and the soluble SiO.
In one embodiment, the first product water after the concentrated brine is subjected to COD removal treatment is subjected to softening and silicon removal treatment, slaked lime and sodium carbonate or sodium hydroxide and sodium carbonate are added to remove hardness in the concentrated brine, magnesium salt or aluminum salt is added to remove SiO2 in the concentrated brine, the pH range of the softening and silicon removal reaction is 10.5-11.5, and the total hardness and the removal rate of soluble silicon are 70-90%.
The embodiments presented in this application are described below with reference to examples.
Fig. 1 is a schematic flow chart of a treatment process according to an embodiment of the present invention, which comprises 3 stages, namely a coagulation COD removal stage S100, a softening silicon removal stage S200, and a COD deep purification stage S300.
Wherein the stage of adding coagulation and removing COD comprises,
s1, allowing strong brine to be treated to flow into a first reaction tank, and adding a medicament into the first reaction tank to perform adsorption coagulation COD removal treatment;
s2, carrying out solid-liquid separation on the mixed liquid obtained by removing the COD based on the first solid-liquid separation device, and conveying the separated first produced water to a first intermediate water tank.
The softening and silicon-removing stage S200 comprises,
s3, guiding the water in the first intermediate water tank to a second reaction tank, adding a silicon removal agent into the second reaction tank to remove the total hardness and soluble silicon in the water,
s4, conveying the mixed liquor obtained by the treatment of the second reaction tank to a second concentration tank;
s5, guiding the mixed liquid in the second concentration tank to a second solid-liquid separation device for solid-liquid separation, and conveying the obtained first produced water to a second intermediate water tank;
a COD deep purification stage S300 comprising
And S6, conveying the water in the second middle water tank to an electrocatalytic oxidation device to remove residual COD, and conveying the produced water treated by the electrocatalytic oxidation device to a water producing pool (also called a water producing tank).
In other embodiments, depending on the water quality of the water to be treated, one or a combination of the coagulation and COD removal stage S100, the softening and silicon removal stage S200, and the COD deep purification stage S300 may be selected to meet the treatment requirements of different water qualities, and the purification treatment process for different water qualities will be described with reference to the following embodiments.
In one embodiment, the concentrated brine concentrated by a zero emission project in coal chemical industry has a water quality (high COD and high hardness) of 10% salt content and a total hardness of 400 mg/L (CaCO)3Calculated), soluble silicon 100 mg/L (in SiO)2Meter), COD is 1000 mg/L, after the concentrated salt water deep purification device and the process treatment of the utility model, the total hardness of the effluent is less than 80 mg/L (using CaCO)3Calculated), soluble silicon < 20 mg/L (in SiO)2Metering), COD is less than 60 mg/L, the treatment process comprises the steps of a COD adsorption and coagulation removing stage, a softening and silicon removing stage and a COD deep purification stage;
the processing steps are as follows:
1. COD removing stage by adsorption coagulation
S11, homogenizing and homogenizing the strong brine in a regulating tank (101), conveying the uniform concentrated brine to a first reaction tank (102), carrying out a special-effect compound reagent reaction to remove COD, conveying the mixed liquor to a first concentration tank (103), and conveying the reaction sludge to a sludge dewatering device (106);
s12, conveying the mixed liquor treated in the step S11 to a first solid-liquid separation device (104) for solid-liquid separation, and conveying the obtained first produced waterThe COD of the effluent from the first middle water tank (105) is 600 mg/L, and the total hardness is 562.5 mg/L (as CaCO)3Calculated), soluble silicon 75 mg/L (in SiO)2A meter); the first concentration tank is mainly used for returning concentrated water of the first solid-liquid separation device to the concentration tank, and finally reacting concentrated sludge and conveying the concentrated sludge to the sludge dewatering device.
2. Softening and desiliconizing stage
S13, conveying the first produced water treated in the step S12 to a second reaction tank (201), performing enhanced softening silicon removal medicament reaction to remove total hardness and soluble silicon, conveying the mixed solution to a second concentration tank 202, and conveying the reaction sludge to a sludge dewatering device (106);
s14, conveying the mixed liquid treated in the step S13 to a second solid-liquid separation device (203) for solid-liquid separation, conveying the obtained second produced water to a second intermediate water tank (204), and conveying the effluent water with the total hardness of 77 mg/L (as CaCO)3Calculated), soluble silicon 15 mg/L (in terms of SiO)2A meter);
3. COD deep purification stage
S15, conveying the second produced water treated in the step S14 to an electrocatalytic oxidation device (205) to further remove residual COD (namely, deep removal of COD), and conveying the produced water to a water production pool (206), wherein the COD of the effluent is 56 mg/L.
As shown in fig. 2, the connection diagram of the deep purification device of the embodiment is shown, and the device includes: a COD removing device, a softening silicon removing device and a COD advanced treatment device which are connected by pipelines and liquid pumps,
the COD removing device is as follows: the water outlet of a strong brine adjusting tank (101) is connected with the water inlet of a first reaction tank (102) through a pipeline and an adjusting tank lifting pump (108), a medicine adding hole of the first reaction tank (102) is connected with a first medicine adding device (107) through a pipeline and a medicine adding pump (112), the water outlet of the first reaction tank (102) is connected with the water inlet of a first concentration tank (103) through a pipeline and a pump (109), the water outlet of the first concentration tank (103) is connected with a first solid-liquid separation device (104) through a pipeline and a pump (110), the mud outlet of the first concentration tank (103) is connected with a sludge dewatering device (106) through a pipeline and a sludge pump (213), the water producing port of the first solid-liquid separation device (104) is connected with the water inlet of a first intermediate water tank (105) through a pipeline, the water outlet of the first intermediate water tank (105) is connected with the first concentration tank (103) through a pipeline, and the water outlet of the first intermediate water tank (105) is connected with the water inlet of a second reaction tank (201) through;
the softening and silicon-removing device comprises: a medicine adding hole of a second reaction tank (201) is connected with a second medicine adding device (207) through a pipeline and a medicine adding pump (214), a first reaction pH detection device (208) is arranged in the second reaction tank, a water outlet of the second reaction tank (201) is connected with a water inlet of a second concentration tank (202) through a pipeline and a pump (209), a water outlet of the second concentration tank (202) is connected with a water inlet of a second solid-liquid separation device (203) through a pipeline and a pump (210), a sludge outlet of the second concentration tank (202) is connected with a sludge dewatering device (106) through a pipeline and a sludge pump (213), a water producing port of the second solid-liquid separation device (203) is connected with a water inlet of a second intermediate water tank (204) through a pipeline, and a concentrated water port is connected with the second concentration tank (202) through a pipeline;
the COD deep purification device is: the water outlet of the second middle water pool (204) is connected with the water inlet of the electrocatalytic oxidation device (205) through a pipeline and a lift pump (211), the water outlet of the electrocatalytic oxidation device (205) is connected with the water inlet of the water producing pool (206) through a pipeline, and the water producing pool (206) is provided with a second pH detection device (212). The medicine adding module is electrically connected with the second pH detection device, and adds a medicine into the water producing tank based on information fed back by the second detection device so as to adjust water in the water producing tank to reclaimed water (pH is 7).
In one embodiment, the water after the hardness removal pretreatment in a certain petrochemical zero-emission project is concentrated brine with high COD and low hardness, and the quality of the concentrated brine (in the case of high COD and low hardness water quality), the salt content is 21 percent, and the total hardness is 50 mg/L (as CaCO)3Calculated), soluble silicon 7.5 mg/L (in SiO)2Calculated), COD is 1881 mg/L, after the deep purification device and the process treatment of the concentrated salt water of the utility model, the total hardness of the effluent is less than 50 mg/L (using CaCO)3Calculated) soluble silicon < 7.5 mg/L (in SiO)2Calculated), COD is less than 80 mg/L, and the treatment process comprises a COD adsorption coagulation removal stage and a COD deep purification stage.
The specific processing steps in this example are as follows:
1. COD removing stage by adsorption coagulation
S21, homogenizing and homogenizing the strong brine in an adjusting tank (101), conveying the uniform concentrated brine to a first reaction tank (102), carrying out a special-effect compound reagent reaction to remove COD, conveying the mixed liquor to a first concentration tank (103), and conveying the reaction sludge to a sludge dewatering device (106);
s22, conveying the mixed liquor treated in the step S21 to a first solid-liquid separation device (104) for solid-liquid separation, conveying the obtained first produced water to a first intermediate water tank (105), wherein the COD of the effluent is 940.5 mg/L, and the total hardness is 45 mg/L (using CaCO)3Calculated), soluble silicon 5.1 mg/L (in SiO)2A meter);
2. COD deep purification stage
S23, conveying the first produced water treated in the step S22 to an electrocatalytic oxidation device (205) to remove residual COD, and conveying the produced water to a water producing pool (206), wherein the COD of the effluent is 75 mg/L.
To facilitate description of some of the devices and corresponding numbering described along with fig. 2, the device includes: COD remove device, COD advanced treatment unit, each device is connected through pipeline and liquid pump, and COD remove device is: a water outlet of a strong brine adjusting tank (101) is connected with a water inlet of a first reaction tank (102) through a pipeline and an adjusting tank lifting pump (108), a medicine adding hole of the first reaction tank (102) is connected with a first medicine adding device (107) through a pipeline and a medicine adding pump (112), a water outlet of the first reaction tank (102) is connected with a water inlet of a first concentration tank (103) through a pipeline and a pump (109), a water outlet of the first concentration tank (103) is connected with a first solid-liquid separation device (104) through a pipeline and a pump (110), a sludge outlet of the first concentration tank (103) is connected with a sludge dewatering device (106) through a pipeline and a sludge pump (213), a water producing port of the first solid-liquid separation device (104) is connected with a water inlet of a first intermediate water tank (105) through a pipeline, and a water outlet is connected with the first concentration tank (103) through a pipeline;
the COD deep purification stage comprises: the water outlet of the first middle water pool (105) is connected with the water inlet of the electrocatalytic oxidation device (205) through a pipeline and a first middle water pool lift pump (111), and the water outlet of the electrocatalytic oxidation device (205) is connected with the water producing pool (206) through a pipeline.
In one embodiment, the water after the high-grade oxidation treatment in the zero discharge project of the coking wastewater generated in a steel plant is concentrated brine with low COD and high hardness, wherein the concentrated brine has 13% salt content and 510 mg/L (CaCO) total hardness in the case of water with low COD and high hardness3Calculated), 77.5mg of soluble silicon/L (in SiO)2Meter), COD is 65 mg/L, after the concentrated salt water deep purification device and the process treatment of the utility model, the total hardness of the effluent is less than 80 mg/L (using CaCO)3Calculated) soluble silicon < 15 mg/L (in SiO)2Calculated), COD is 68 mg/L, the treatment process mainly comprises softening and silicon removal, and the treatment steps are as follows:
s31, homogenizing and homogenizing the strong brine in a regulating tank (101), conveying the homogenized strong brine to a second reaction tank (201), performing enhanced softening silicon removal medicament reaction to remove total hardness and soluble silicon, conveying the mixed solution to a second concentration tank (202), and conveying the reaction sludge to a sludge dewatering device (106);
s32, conveying the mixed liquor treated in the step S31 to a second solid-liquid separation device (203) for solid-liquid separation, conveying the obtained second produced water to a water production pool (206), wherein the total hardness of the produced water is 78 mg/L (as CaCO)3Calculated), soluble silicon is 13 mg/L (calculated as SiO)2Calculated), the COD was 68 mg/L.
To facilitate description of some devices and corresponding numbers along the description of fig. 2, in this embodiment, the processing equipment mainly includes a softening and silicon-removing device: the water outlet of the concentrated brine adjusting tank (101) is connected with the water inlet of a second reaction tank (201) through a pipeline meter lifting pump (108), the medicine adding hole of the second reaction tank (201) is connected with a second medicine adding device (207) through a pipeline and a medicine adding pump (214), a first reaction pH detection device (208) is arranged in the second reaction tank, the water outlet of the second reaction tank (201) is connected with the water inlet of a second concentration tank (202) through a pipeline and a pump (209), the water outlet of the second concentration tank (202) is connected with the water inlet of a second solid-liquid separation device (203) through a pipeline and a pump (210), the mud outlet of the second concentration tank (202) is connected with a sludge dewatering device (106) through a pipeline and a sludge pump (213), the water outlet of the second solid-liquid separation device (203) is connected with the water inlet of a water producing tank (206) through a pipeline, the concentrated water outlet is connected with the second concentration tank (202) through a pipeline, and the water producing tank (206) is internally provided with a second pH detection device.
In the deep purification process of the strong brine, the COD removal section of the adsorption coagulation, the softening silicon removal section and the COD deep purification section are combined according to different water qualities of the strong brine (the salt content is 6-25 percent) in application occasions. Not every process may include all of the features described above. Preferably, such as:
(1) on the occasion of high COD and high hardness water, COD is more than or equal to 100 mg/L, the total hardness is more than 120 mg/L (calculated by CaCO 3), and the water is purified by adopting a mode of 'COD removing section + softening silicon removing section + COD deep purification section';
(2) under the condition of high COD and low hardness water quality, the COD is more than or equal to 100 mg/L, the total hardness is less than or equal to 120 mg/L (calculated by CaCO 3), and the water is purified by adopting a mode of a COD removal section and a COD deep purification section;
(3) the water quality with low COD and high hardness is that COD is less than 100 mg/L, total hardness is more than 120 mg/L (calculated by CaCO 3), and the water is purified by adopting a softening and desiliconization mode.
In the deep purification device for the concentrated brine, the first solid-liquid separation device and the second solid-liquid separation device are provided with the spiral microfiltration membranes, so that the deep purification device for the concentrated brine has excellent membrane flux and interception performance in a wide molecular weight range and high pollution resistance. The membrane material is PVDF, the recovery rate is 95-99%, the solid content of concentrated water is 1-5%, the maximum water inlet pressure is 0.8Mpa, the maximum pressure drop is 0.12Mpa, and the operating pH value range is 2-10.
The electrocatalytic oxidation device adopts a two-dimensional electrode/a three-dimensional electrode, a layer of micron or submicron metal oxide is deposited on the surface of the electrode plate, the stability of the electrode is improved, and the removal rate of COD is more than 90%.
The above embodiments are only for illustrating the technical concept and features of the present invention, and the purpose of the embodiments is to enable those skilled in the art to understand the contents of the present invention and to implement the present invention, which cannot limit the protection scope of the present invention. All modifications made according to the spirit of the main technical scheme of the present invention shall be covered within the protection scope of the present invention.
Claims (6)
1. A strong brine deep purification device is characterized by comprising a COD removal device, a softening silicon removal device and a COD deep treatment device, wherein the softening silicon removal device is connected with the COD removal device and the COD deep treatment device through a pipeline and a liquid pump,
the COD removing device comprises a first reaction tank and a first concentration tank connected with the first reaction tank,
the first reaction tank is provided with a feeding port for feeding medicine,
a first water inlet for flowing in the strong brine to be treated,
a first water outlet through which the water treated by the first reaction tank flows to a first concentration tank,
the mixed liquid treated by the first concentration tank flows into a water inlet of a first solid-liquid separation device, the first produced water is separated by the first solid-liquid separation device and flows to a first intermediate water tank through a water outlet of the first intermediate water tank,
the softening desiliconization device comprises a second reaction tank, a second concentration tank connected with the second reaction tank, and a second solid-liquid separation device connected with the second concentration tank;
the second reaction tank is internally provided with a first pH detection device for detecting the pH value of water in the second reaction tank, a water outlet of the first reaction tank is connected with a water inlet of a second concentration tank through a pipeline and a pump, a water outlet of the second concentration tank is connected with a water inlet of a second solid-liquid separation device through a pipeline and a pump, a sludge outlet of the second concentration tank is connected with a sludge dewatering device through a pipeline and a sludge pump, the water treated by the second solid-liquid separation device is connected with a water inlet of a second middle water tank through a pipeline through a water production port of the second solid-liquid separation device, and a concentrated water port is connected with the second concentration tank through a pipeline;
the COD advanced purification device comprises: and the water inlet of the electrocatalytic oxidation device is connected with the second middle water tank, the water outlet of the electrocatalytic oxidation device is connected with the water inlet of the water producing pool, and the water produced by the electrocatalytic oxidation device flows into the water producing pool.
2. The concentrated brine deep purification device as claimed in claim 1, wherein the first solid-liquid separation device or the second solid-liquid separation device comprises a roll type microfiltration membrane, and the membrane material of the roll type microfiltration membrane is PVDF.
3. The concentrated brine deep purification device according to claim 1, wherein the electrocatalytic oxidation device comprises a two-dimensional electrode or a three-dimensional electrode, and a layer of micron or submicron metal oxide is deposited on the surface of an electrode plate of the electrocatalytic oxidation device.
4. The brine deep purification device as claimed in claim 1, wherein the water production tank is provided with a second pH detection device.
5. The concentrated brine deep purification device of claim 4, wherein the dosing module is electrically connected to the second pH detection device, and doses a medicament into the water producing tank based on information fed back by the second detection device to adjust water in the water producing tank to reclaimed water.
6. A strong brine deep purification device is characterized by comprising a COD removal device which is connected with a COD deep treatment device through a pipeline and a liquid pump,
the COD removing device comprises a first reaction tank and a first concentration tank connected with the first reaction tank,
the first reaction tank is provided with a feeding port for feeding medicine,
a first water inlet for flowing in the strong brine to be treated,
a first water outlet through which the water treated by the first reaction tank flows to a first concentration tank,
the mixed liquid treated by the first concentration tank flows into a water inlet of a first solid-liquid separation device, the first produced water is separated by the first solid-liquid separation device and flows to a first intermediate water tank through a water outlet of the first intermediate water tank,
the COD advanced purification device comprises: the water inlet of the electrocatalytic oxidation device is connected with the first intermediate water tank, the water outlet of the electrocatalytic oxidation device is connected with the water inlet of the water producing pool, and the water produced by the electrocatalytic oxidation device flows into the water producing pool.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921731384.9U CN211198889U (en) | 2019-10-13 | 2019-10-13 | Strong brine deep purification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921731384.9U CN211198889U (en) | 2019-10-13 | 2019-10-13 | Strong brine deep purification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211198889U true CN211198889U (en) | 2020-08-07 |
Family
ID=71879426
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921731384.9U Active CN211198889U (en) | 2019-10-13 | 2019-10-13 | Strong brine deep purification device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211198889U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110734170A (en) * | 2019-10-13 | 2020-01-31 | 麦王环境技术股份有限公司 | deep purification device and treatment process for concentrated salt water |
| WO2022083071A1 (en) * | 2020-10-22 | 2022-04-28 | 麦王环境技术股份有限公司 | Deep purification device and process for non-degradable organic wastewater |
-
2019
- 2019-10-13 CN CN201921731384.9U patent/CN211198889U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110734170A (en) * | 2019-10-13 | 2020-01-31 | 麦王环境技术股份有限公司 | deep purification device and treatment process for concentrated salt water |
| WO2022083071A1 (en) * | 2020-10-22 | 2022-04-28 | 麦王环境技术股份有限公司 | Deep purification device and process for non-degradable organic wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101337750B (en) | Reclamation and comprehensive treatment method for paper-making waste water | |
| CN100465110C (en) | Coking waste water reuse treatment method | |
| CN104176857B (en) | The treatment process of Mn-bearing waste water in wet method electrolysis manganese production process | |
| CN105540947A (en) | Method and system for processing drilling wastewater | |
| CN103214153B (en) | Regenerative cycle and utilization method for papermaking deep-treatment wastewater | |
| CN105906149A (en) | Chlor-alkali plant strong brine zero-discharge treatment system and treatment method | |
| CN211198889U (en) | Strong brine deep purification device | |
| CN102583817A (en) | Printing and dyeing tail water deep treatment and reuse process | |
| CN107522327A (en) | The oxidation integrated papermaking wastewater treatment device of electric flocculation precipitate high grade | |
| CN217809018U (en) | HPPO waste water and hydrogen peroxide solution waste water combined treatment system | |
| CN101723551B (en) | Method for treating recycling of coking wastewater | |
| CN112624446A (en) | Organic wastewater zero-discharge treatment process | |
| CN102887611A (en) | Membrane-process integrated technique for implementing comprehensive wastewater zero discharge or low discharge of large-scale steel plant | |
| CN110734170A (en) | deep purification device and treatment process for concentrated salt water | |
| CN101343129B (en) | Pretreatment technique for decolorization of wastewater at middle plate of paper-making pulping | |
| CN106495355A (en) | A kind of electroplating wastewater treatment reclaiming technique and combinations thereof device | |
| CN109110967B (en) | Bauxite beneficiation wastewater recycling system and method based on membrane chemical reactor | |
| CN101723550B (en) | System for treating recycling of coking wastewater | |
| CN111484149A (en) | High-efficiency hardness removing device and method for high-concentration industrial waste liquid treatment | |
| CN212102493U (en) | Advanced treatment system for supplementing water by using urban reclaimed water as circulating water of power plant | |
| CN109205944A (en) | A kind of pharmacy waste water divides salt processing method | |
| CN115259507A (en) | Processing device for flowback liquid | |
| CN112374636A (en) | Deep purification device and process for refractory organic wastewater | |
| CN112321074A (en) | Coal chemical wastewater treatment process | |
| CN220334988U (en) | High-concentration metal cutting waste liquid treatment device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: Floor 4, block a, Oriental fisherman's Wharf, 1088 Yangshupu Road, Yangpu District, Shanghai 200082 Patentee after: Mai Wang Environmental Technology Co.,Ltd. Country or region after: China Address before: Floor 4, block a, Oriental fisherman's Wharf, 1088 Yangshupu Road, Yangpu District, Shanghai 200082 Patentee before: MCWONG ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Country or region before: China |
|
| CP03 | Change of name, title or address |