CN116621387B - Concentrated solution full-quantification treatment system and method - Google Patents
Concentrated solution full-quantification treatment system and method Download PDFInfo
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- CN116621387B CN116621387B CN202310802174.9A CN202310802174A CN116621387B CN 116621387 B CN116621387 B CN 116621387B CN 202310802174 A CN202310802174 A CN 202310802174A CN 116621387 B CN116621387 B CN 116621387B
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- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000011002 quantification Methods 0.000 title claims abstract description 21
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 98
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- 238000001704 evaporation Methods 0.000 claims abstract description 51
- 230000008020 evaporation Effects 0.000 claims abstract description 51
- 238000003860 storage Methods 0.000 claims abstract description 50
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 229910010271 silicon carbide Inorganic materials 0.000 claims abstract description 41
- 239000003513 alkali Substances 0.000 claims abstract description 40
- 239000012528 membrane Substances 0.000 claims abstract description 37
- 238000001035 drying Methods 0.000 claims abstract description 30
- 239000002253 acid Substances 0.000 claims abstract description 28
- 239000013049 sediment Substances 0.000 claims description 37
- 239000006228 supernatant Substances 0.000 claims description 28
- 239000012452 mother liquor Substances 0.000 claims description 27
- 239000012141 concentrate Substances 0.000 claims description 14
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- 230000035484 reaction time Effects 0.000 claims description 4
- NBBQQQJUOYRZCA-UHFFFAOYSA-N diethoxymethylsilane Chemical compound CCOC([SiH3])OCC NBBQQQJUOYRZCA-UHFFFAOYSA-N 0.000 claims description 3
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- 230000006872 improvement Effects 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
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- 229910052791 calcium Inorganic materials 0.000 description 3
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- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The application discloses a concentrated solution full-quantification treatment system and a concentrated solution full-quantification treatment method, and belongs to the technical field of concentrated solution treatment. The concentrated solution full-quantification treatment system comprises a raw liquid pool, a primary flocculation reaction tank, a primary flocculation sedimentation tank, an intermediate water tank, an alkali reaction tank, a sedimentation tank, a silicon carbide membrane unit, an acid reaction tank, a first sludge storage tank, a second sludge storage tank and a filter press. The method is applied to the aspect of full quantification treatment of concentrated solution, solves the problems of unstable operation and large mother solution yield of the existing evaporation process, has good organic matter removal effect, can effectively relieve the problems of evaporator scaling, drying system foaming and the like, increases the stable operation period of the evaporation system, improves the treatment capacity, reduces the mother solution yield and can realize the full quantification treatment target.
Description
Technical Field
The application belongs to the technical field of concentrated solution treatment, and particularly relates to a concentrated solution full-quantification treatment system and method.
Background
The existing leachate treatment process is mainly a membrane process based on membrane advanced treatment, wherein the membrane advanced treatment comprises NF, RO and DTRO which are mainly processes, and the membrane process can generate 10% -40% of concentrated solution. The concentrated solution has the characteristics of high salt content, complex pollution components, high organic pollutant content, easy scaling and the like, is difficult to treat in the industry, and the general thinking about the concentrated solution treatment at the present stage is control in a system, so that the concentrated solution is reduced, and finally, the concentrated solution is reasonably treated as far as possible.
At present, the treatment modes of the inner membrane concentrate in the industry mainly can be divided into three categories, namely recharging treatment, namely recharging the membrane concentrate to a landfill for treatment, however, most of the membrane concentrate is forbidden under the current environmental protection requirement; secondly, the reduction treatment, namely, the absolute content of the membrane concentrate is reduced by physical, chemical and other means, and the treatment technology comprises reverse osmosis, nanofiltration, evaporation and the like, but concentrate or mother liquor can be generated and needs further treatment; thirdly, innocent treatment is carried out, the treatment technology comprises advanced oxidation, coagulation electric flocculation, adsorption, back spraying incineration and the like, however, the advanced oxidation technology depends on the medicament and the operation condition, the pollutant is not thoroughly removed, the back spraying incineration of the concentrated solution has corrosion problems on a hearth and related equipment, and the back spraying amount is limited. Therefore, the evaporation process is the main stream direction of the current concentrate treatment.
However, the existing evaporation process still has the problems of unstable operation and large mother liquor yield, and specifically:
1) The equipment of the evaporation system is frequently cleaned and has poor continuous operation stability
After improvement, the concentrated solution is disposed to 500m 3 The treatment capacity of/d is affected by the fast scaling speed of the evaporator, the treatment capacity decays fast, and finally, the equipment is frequently shut down and cleaned, the system cannot continuously run, and in addition, inorganic scale and organic matters are attached to the surface of the heat exchanger to affect the heat exchange effect, so that the yield of the evaporated mother liquor is high;
2) The scale layer of the equipment is complex, and the tube bundle is damaged due to manual cleaning
The components of the scale layer of the evaporator are mainly calcium sulfate scale and organic compound scale, calcium sulfate cannot be dissolved in acid and alkali cleaning agents, the manual cleaning effect is poor, the single cleaning time is long, the surface of an evaporation tube bundle is irreversibly damaged by strong mechanical cleaning operation, the tube bundle scale is aggravated, vicious circulation is formed, and even the evaporation tube bundle is damaged, so that the following effects are caused: (1) The pressure of the pipe box is reduced, saturated steam cannot be formed, and distilled water cannot be produced after heat exchange; (2) The concentrated solution enters the tube bundle to form a scale body, and the evaporation performance is affected by blocking the tube bundle; (3) The concentrated solution enters the tube bundle without forming scale, and is mixed into distilled water to influence the effluent quality of the MVR evaporator.
In addition, when the MVR evaporation mother liquor is treated by the drying process, the problems of foaming during operation and incapability of realizing mother liquor decrement exist, and the method is specific:
when the MVR evaporation mother liquor is treated by adopting a drying process, after the drying and concentration are carried out to a certain extent, the foaming phenomenon of the upper space of the steam-water separation chamber is serious, the generated foam is easily pumped away and enters a high-speed rotating steam compressor, so that the dynamic balance of the compressor is invalid, the compressor is subjected to phenomena of surge, vibration, overrun of displacement and the like, even the compressor is damaged, the treatment performance of the evaporation mother liquor is severely limited, salt cannot be separated out, and the analysis is mainly because organic matters in water obstruct the nucleation of the salt, so that crystalline salt cannot be separated out; because the operation of the drying system is serious in foaming, after the technical improvement, in order to ensure the processing capacity of the concentrated solution system, the drying equipment and the evaporation equipment are operated in parallel and used for processing the concentrated solution, and the mother solution decrement cannot be realized.
Disclosure of Invention
Aiming at the defects existing in the prior art, the application aims to solve the technical problems of unstable operation and large mother liquor yield of the existing evaporation process, and provides the concentrated solution full-quantification treatment system and method which have the advantages of good organic matter removal effect, capability of effectively relieving the problems of evaporator scaling, drying system foaming and the like, increase of the stable operation period of the evaporation system, improvement of the treatment capacity and reduction of the mother liquor yield, and capability of realizing the full-quantification treatment target.
In order to solve the technical problems, the application adopts the following technical scheme:
the application provides a concentrated solution full-quantification treatment system, which comprises a raw liquid pool, a primary flocculation reaction tank, a primary flocculation sedimentation tank, an intermediate water tank, an alkali reaction tank, a sedimentation tank, a silicon carbide membrane unit, an acid reaction tank, a first sludge storage tank, a second sludge storage tank and a filter press; the outlet of the raw liquid pool is connected with the inlet of the primary flocculation reaction tank; the outlet of the primary flocculation reaction tank is connected with the inlet of the primary flocculation sedimentation tank; the supernatant outlet of the primary flocculation sedimentation tank is connected with the inlet of the intermediate water tank; the outlet of the intermediate water tank is connected with the inlet of the alkali reaction tank; the outlet of the alkali reaction tank is connected with the inlet of the sedimentation tank; the supernatant outlet of the sedimentation tank is connected with the inlet of the silicon carbide membrane unit; the supernatant outlet of the silicon carbide film unit is connected with the inlet of the acid reaction tank;
further comprises: a pump for conveying the sediment in the primary flocculation sedimentation tank to the first sludge storage tank, and conveying the sediment filtered by the silicon carbide membrane unit and the sediment in the sedimentation tank to the second sludge storage tank; and a high-pressure pump for delivering the sediment in the first sludge storage tank and the second sludge storage tank to the filter press for dehydration; the liquid outlet of the filter press is connected with the inlet of the alkali reaction tank and/or the inlet of the acid reaction tank;
the primary flocculation sedimentation tank adopts a central diversion cylinder type water distribution;
the maximum transmembrane pressure difference of the silicon carbide film in the silicon carbide film unit is 0.4Mpa, and the film flux is 0.3m 3 /m 2 ·h。
Preferably, the device also comprises an intermediate water tank, an evaporation unit, a primary mother liquor tank, a drying unit and a secondary mother liquor tank; the inlet of the intermediate water tank is connected with the outlet of the acid reaction tank, and the supernatant outlet of the intermediate water tank is connected with the inlet of the evaporation unit; the outlet of the evaporation unit is connected with the inlet of the primary mother liquid pool; the outlet of the primary mother liquor pool is connected with the inlet of the drying unit; and the outlet of the drying unit is connected with the inlet of the secondary mother liquid pool.
Preferably, the flocculation reagent storage and addition unit is further provided with a flocculation reagent added into the primary flocculation reaction tank, and a liquid alkali storage and addition unit is provided with a liquid alkali added into the alkali reaction tank.
Preferably, the flocculating agent is prepared by the following method:
AlCl is mixed according to the mole ratio of Si/Al of 0.1-0.4 3 Mixing the solution and gamma-aminopropyl diethoxymethyl silane, stirring at room temperature, dropwise adding NaOH solution by adopting a constant flow pump until the alkalization degree B reaches 0.5-2.0, and completely reacting to obtain the flocculation medicament.
Preferably, the addition amount of the flocculation reagent is 0.8-1.0wt% of the total amount of the concentrated solution entering the primary flocculation reaction tank; the reaction time in the primary flocculation reaction tank is 10min, and the residence time in the primary flocculation sedimentation tank is 3h.
Preferably, the sediment in the intermediate basin is transported by a pump to the second sludge storage tank.
In another aspect, the present application provides a method for performing full-scale treatment on a concentrated solution by using the full-scale treatment system for a concentrated solution according to any one of the above aspects, comprising the steps of:
the concentrated solution enters a primary flocculation reaction tank after passing through a raw liquid pool, and a flocculation reagent is added into the primary flocculation reaction tank to carry out flocculation reaction; the concentrated solution after flocculation reaction enters a primary flocculation sedimentation tank for sedimentation, after sedimentation, supernatant in the primary flocculation sedimentation tank enters an intermediate water tank, and sediment in the primary flocculation sedimentation tank is pumped into a first sludge storage tank; the supernatant in the intermediate water tank enters an alkali reaction tank and reacts with liquid alkali, the reaction product enters a sedimentation tank, after sedimentation, the supernatant in the sedimentation tank is filtered by a silicon carbide membrane unit, the filtrate enters an acid reaction tank for reaction treatment, and sediment in the sedimentation tank and sediment obtained by filtration by the silicon carbide membrane unit are pumped into a second sludge storage tank; and the filter pressing liquid generated after the sediment in the first sludge storage tank is dehydrated by the filter press enters the alkali reaction tank for subsequent treatment, and the filter pressing liquid generated after the sediment in the second sludge storage tank is dehydrated by the filter press enters the acid reaction tank for subsequent treatment.
Preferably, the method further comprises: the treatment liquid in the acid reaction tank enters an intermediate water tank for precipitation, supernatant obtained by precipitation in the intermediate water tank enters an evaporation unit for treatment to obtain primary mother liquid, the primary mother liquid enters a primary mother liquid tank for treatment, and then enters a secondary mother liquid tank for subsequent treatment after being treated by a drying unit.
Preferably, the water content of the mud cake produced after dehydration by the filter press is lower than 60%.
Preferably, the water yield of the silicon carbide film unit is more than 90%; the concentration yield of the drying unit is below 50%.
Compared with the prior art, the application has the beneficial effects that:
the application provides a concentrated solution full-quantification treatment system, which effectively removes organic matters in concentrated solution by additionally arranging a primary flocculation reaction tank and a primary flocculation sedimentation tank, wherein the removal rate of the organic matters is more than 30 percent; the water yield of the silicon carbide film unit reaches more than 90%, and the chemical washing frequency is 1 time/d; the problems of scaling of the evaporator, foaming of the drying system and the like are effectively relieved; the stable operation period of the evaporation unit is increased, and the evaporation unit can stably operate for more than 15 days; meanwhile, the treatment capacity of the evaporation unit is improved by 20-60%, and the yield of mother liquor is reduced by 10%; the concentration rate of the drying unit is maintained within 50%, so that digestion in a park can be realized, external transportation is not needed, and the aim of full quantization treatment is fulfilled.
Drawings
FIG. 1 is a schematic process flow diagram of a method for full-quantifying a concentrated solution according to an embodiment of the present application;
FIG. 2 is a schematic diagram of the analysis results of the organic matters in and out of the primary flocculation provided by the embodiment of the application;
FIG. 3 shows the effluent conditions of the stages of the method for full-scale treatment of a concentrated solution according to the embodiment of the present application;
FIG. 4 is a schematic illustration of the scaling of the tube bundles before and after primary flocculation as provided by an embodiment of the present application.
Detailed Description
The technical scheme in the specific embodiment of the application will be fully described in detail. It is apparent that the described embodiments are only some specific implementations, but not all implementations, of the general technical solution of the present application. All other embodiments, which are obtained by those skilled in the art based on the general inventive concept, fall within the scope of the present application.
In one aspect, the application provides a concentrated solution full-quantification treatment system, as shown in fig. 1, which comprises a raw liquid pool, a primary flocculation reaction tank, a primary flocculation sedimentation tank, an intermediate water tank, an alkali reaction tank, a sedimentation tank, a silicon carbide membrane unit, an acid reaction tank, a first sludge storage tank, a second sludge storage tank and a filter press; the outlet of the raw liquid pool is connected with the inlet of the primary flocculation reaction tank; the outlet of the primary flocculation reaction tank is connected with the inlet of the primary flocculation sedimentation tank; the supernatant outlet of the primary flocculation sedimentation tank is connected with the inlet of the intermediate water tank; the outlet of the intermediate water tank is connected with the inlet of the alkali reaction tank; the outlet of the alkali reaction tank is connected with the inlet of the sedimentation tank; the supernatant outlet of the sedimentation tank is connected with the inlet of the silicon carbide membrane unit; the supernatant outlet of the silicon carbide film unit is connected with the inlet of the acid reaction tank; further comprises: a pump for conveying the sediment in the primary flocculation sedimentation tank to the first sludge storage tank, and conveying the sediment filtered by the silicon carbide membrane unit and the sediment in the sedimentation tank to the second sludge storage tank; and a high-pressure pump for delivering the sediment in the first sludge storage tank and the second sludge storage tank to the filter press for dehydration; the liquid outlet of the filter press is connected with the inlet of the alkali reaction tank and/or the inlet of the acid reaction tank; the primary flocculation sedimentation tank adopts a central diversion cylinder type water distribution; the maximum transmembrane pressure difference of the silicon carbide film in the silicon carbide film unit is 0.4Mpa, and the film flux is 0.3m 3 /m 2 H. The concentrated solution full-quantization treatment system adopts a deep flocculation and silicon carbide pretreatment treatment process as an evaporation pretreatment process, and effectively removes organic matters in the concentrated solution by adding a primary flocculation reaction tank and a primary flocculation sedimentation tank, wherein the removal rate of the organic matters is more than 30%; the water yield of the silicon carbide film unit reaches more than 90%, and the chemical washing frequency is 1 time/d; the problems of scaling of the evaporator, foaming of the drying system and the like are effectively relieved; the stable operation period of the evaporation unit is increased, and the evaporation unit can stably operate for more than 15 days; at the same time, the treatment capacity of the evaporation unit is improved by 20-60%, and the mother liquor is producedThe amount is reduced by 10%; the concentration rate of the drying unit is maintained within 50%, so that digestion in a park can be realized, external transportation is not needed, and the aim of full quantization treatment is fulfilled.
Regarding the concentrated solution full-quantification treatment system, wherein a raw liquid pool is used as a water inflow regulating pool, the retention time is 10h, and the concentrated solution full-quantification treatment system is mainly used for buffering fluctuation of water quality and water quantity of inflow water; the primary flocculation reaction tank and the primary flocculation sedimentation tank (deep flocculation process) belong to a pretreatment module, a flocculating agent is added into the primary flocculation reaction tank, the reaction time is 10min, the retention time of the primary flocculation sedimentation tank is 3h, a central guide cylinder type water distribution is adopted, the inclined tube filler is added to accelerate the mud-water separation effect, the water inlet disturbance is reduced, the water outlet is ensured to be clear, and the main function is to remove organic matters (COD) in water and ensure the stable operation of the subsequent process; the alkali reaction tank, the sedimentation tank and the silicon carbide membrane unit also belong to a pretreatment module, wherein liquid alkali is added in the alkali reaction tank and used for converting the hardness of calcium and magnesium in water into sediment, the subsequent silicon carbide membrane is used for carrying out mud-water separation, the silicon carbide membrane adopts an inorganic silicon carbide material, the friction of the membrane surface is increased in a cross-flow mode, and suspended matters are prevented from being deposited on the membrane surface. It is noted that, because the precipitation produced by softening the concentrated solution has smaller particle size and poorer precipitation effect, and the solid-liquid separation cannot be carried out by adopting a general sedimentation method, the technical scheme of the application adopts the silicon carbide membrane unit to carry out the separation, on one hand, the maximum transmembrane pressure difference and the membrane flux of the silicon carbide membrane are limited, and more importantly, the technical scheme of the application is limited to firstly remove COD by utilizing a primary flocculation reaction tank and a primary flocculation sedimentation tank, and then remove hardness by utilizing an alkali reaction tank and a sedimentation tank, namely, the pretreatment of the concentrated solution is carried out in a mode of removing the COD before and after the hardness is removed, thereby not only ensuring the high-efficiency removal of organic matters and the hardness, but also ensuring the stable operation of the silicon carbide membrane, improving the water production rate, reducing the chemical cleaning frequency and avoiding the irreversible damage of a membrane column. In addition, the technical scheme of the application also specifically limits that the first sludge storage tank and the second sludge storage tank are used for respectively storing flocculated sludge (acidic) and softened sludge (alkaline), so that the two types of sludge are separated for filter pressing, and organic matters in the flocculated sludge are effectively prevented from being released again due to acid-base neutralization.
In a preferred embodiment, the device further comprises an intermediate water tank, an evaporation unit, a primary mother liquor tank, a drying unit and a secondary mother liquor tank; the inlet of the intermediate water tank is connected with the outlet of the acid reaction tank, and the supernatant outlet of the intermediate water tank is connected with the inlet of the evaporation unit; the outlet of the evaporation unit is connected with the inlet of the primary mother liquid pool; the outlet of the primary mother liquor pool is connected with the inlet of the drying unit; and the outlet of the drying unit is connected with the inlet of the secondary mother liquid pool. The concentrated solution full-quantification treatment system realizes the 'deep flocculation + silicon carbide + MVR evaporation + drying decrement + incineration cooperative' treatment by designing each unit, thereby further realizing the aim of the concentrated solution full-quantification treatment. The evaporation unit and the drying unit evaporate the concentrated solution through a horizontal falling film evaporation and plate type forced circulation evaporation system, the generated distilled water is discharged up to the standard, the mother solution is transported out in a cooperated mode, and the salt mud is buried.
In a preferred embodiment, the flocculation reagent storage and addition unit for adding a flocculation reagent to the primary flocculation reaction tank and the liquid alkali storage and addition unit for adding liquid alkali to the alkali reaction tank are further included. In a preferred embodiment, the flocculating agent is prepared by the following method: alCl is mixed according to the mole ratio of Si/Al of 0.1-0.4 3 Mixing the solution and gamma-aminopropyl diethoxymethyl silane, stirring at room temperature, dropwise adding NaOH solution by adopting a constant flow pump until the alkalization degree B reaches 0.5-2.0, and completely reacting to obtain the flocculation medicament. The embodiment further limits the preparation method of the flocculating agent, based on the morphological structure matching mechanism and morphological regulation method principle of the flocculating agent, through the relation of the flocculating agent and pollutants in morphological structure, reaction mechanism and treatment effect, the original innovation is carried out on the molecular structure of the flocculating agent, the effective groups are added, the molecular structure is optimized, and a new chemical structure form is formed, so that the reaction mechanism is regulated and controlled, the removal effect of small molecular organic matters is improved, the application limit of the traditional flocculating agent is broken through, the flocculating agent is applied to the treatment of landfill leachate concentrate, and the treatment effect of the landfill leachate concentrate with complex components and difficult treatment is improved.
In a preferred embodiment, the flocculating agent is added in an amount of 0.8 to 1.0wt% based on the total amount of concentrate entering the primary flocculation reaction tank; the reaction time in the primary flocculation reaction tank is 10min, and the residence time in the primary flocculation sedimentation tank is 3h. The embodiment specifically limits the adding amount of the flocculating agent, because the purpose of full quantification treatment of the concentrated solution can be realized under the adding amount, and the problem that the sedimentation problem of the sedimentation tank is influenced due to the increase of the foam production amount caused by the large adding amount of the flocculating agent is avoided. It will be appreciated that the amount of flocculating agent added may also be 0.9wt% based on the total amount of concentrate entering the primary flocculation reaction tank.
In a preferred embodiment, the sediment in the intermediate basin is transported by a pump to the second sludge storage tank. This embodiment specifically defines the manner of transfer of the sediment in the intermediate basin, it being understood that this transfer may also be other ways reasonably selected by the person skilled in the art in combination with the common general knowledge in the art.
In another aspect, the present application provides a method for performing full-scale treatment on a concentrated solution by using the full-scale treatment system for a concentrated solution according to any one of the above aspects, comprising the steps of:
the concentrated solution enters a primary flocculation reaction tank after passing through a raw liquid pool, and a flocculation reagent is added into the primary flocculation reaction tank to carry out flocculation reaction; the concentrated solution after flocculation reaction enters a primary flocculation sedimentation tank for sedimentation, after sedimentation, supernatant in the primary flocculation sedimentation tank enters an intermediate water tank, and sediment in the primary flocculation sedimentation tank is pumped into a first sludge storage tank; the supernatant in the intermediate water tank enters an alkali reaction tank and reacts with liquid alkali, the reaction product enters a sedimentation tank, after sedimentation, the supernatant in the sedimentation tank is filtered by a silicon carbide membrane unit, the filtrate enters an acid reaction tank for reaction treatment, and sediment in the sedimentation tank and sediment obtained by filtration by the silicon carbide membrane unit are pumped into a second sludge storage tank; the filter pressing liquid generated after the sediment in the first sludge storage tank is dehydrated by a filter press enters the alkali reactionAnd (3) carrying out subsequent treatment in the tank, wherein filter pressing liquid generated after the sediment in the second sludge storage tank is dehydrated by the filter press enters the acid reaction tank for subsequent treatment. According to the treatment method, the primary flocculation precipitation process is additionally arranged, so that organic matters in the concentrated solution are effectively removed, the removal rate of the organic matters reaches more than 30%, the problem that salt is prevented from nucleating in the crystallizer due to high concentration of the organic matters in the concentrated solution, and solid salt cannot be separated out even if the crystallizer reaches the saturation degree of the salt is solved, the stable operation period of the evaporation unit is effectively ensured, and the treatment effect is improved. Further, the water content of the mud cake generated after the filter press is dehydrated is lower than 60%; the water yield of the silicon carbide film unit is more than 90%; the concentration yield of the drying unit is below 50%. It is understood that the filter press adopted in the process is a normal pressure plate-and-frame filter press, and the filtering area is 200m 2 The model of 108C polypropylene is selected, and the product can resist strong acid and alkali.
In a preferred embodiment, further comprising: the treatment liquid in the acid reaction tank enters an intermediate water tank for precipitation, supernatant obtained by precipitation in the intermediate water tank enters an evaporation unit for treatment to obtain primary mother liquid, the primary mother liquid enters a primary mother liquid tank for treatment, and then enters a secondary mother liquid tank for subsequent treatment after being treated by a drying unit.
In order to more clearly describe the full-scale treatment system and method for concentrated solutions provided by the embodiments of the present application, the following description will refer to specific embodiments.
Description of the preferred embodiments
The concentrated solution full-quantification treatment system and the concentrated solution full-quantification treatment process are shown in fig. 1, and are specifically as follows: the concentrated solution enters a primary flocculation reaction tank after passing through a raw liquid pool, and a flocculation reagent is added into the primary flocculation reaction tank to carry out flocculation reaction; the concentrated solution after flocculation reaction enters a primary flocculation sedimentation tank for sedimentation, after sedimentation, supernatant fluid in the primary flocculation sedimentation tank enters an intermediate water tank, and sediment in the primary flocculation sedimentation tank is pumped into a first sludge storage tank; the supernatant in the intermediate water tank enters an alkali reaction tank and reacts with liquid alkali, the reaction product enters a sedimentation tank, after sedimentation, the supernatant in the sedimentation tank is filtered by a silicon carbide membrane unit, the filtrate enters an acid reaction tank for reaction treatment, and sediment in the sedimentation tank and sediment obtained by filtration by the silicon carbide membrane unit are pumped into a second sludge storage tank; the treatment liquid in the acid reaction tank enters an intermediate water tank for precipitation, supernatant obtained by precipitation in the intermediate water tank enters an evaporation unit for treatment to obtain primary mother liquor, the primary mother liquor enters a primary mother liquor tank for treatment, then enters a secondary mother liquor tank for subsequent treatment after being treated by a drying unit, and the precipitate obtained by precipitation in the intermediate water tank is conveyed to a second sludge storage tank by a pump; and the filter pressing liquid generated after the sediment in the first sludge storage tank is dehydrated by the filter press enters the alkali reaction tank for subsequent treatment, and the filter pressing liquid generated after the sediment in the second sludge storage tank is dehydrated by the filter press enters the acid reaction tank for subsequent treatment.
Analysis of results
1. Pretreatment system result analysis (first-order flocculation operation analysis)
1) And (3) improving the organic matter removal effect of the pretreatment section: as can be seen from fig. 2 and 3, the average removal efficiency of the organic matters is about 50%, the expected effect is achieved, and the chromaticity of the effluent is reduced;
2) Processing capacity improves: as can be seen from Table 1, the running water quantity under stable conditions was 500m 3 And/d, the maximum treatment capacity can reach 576m 3 /d；
3) Optimizing the optimal operation parameters of primary flocculation: the adding concentration is about 4mL/L, the pH is about 3, the sludge discharge proportion is about 20%, the process operation stability is good, and the organic matter removal effect is optimal;
4) The utilized tank body can meet the design parameters of the primary flocculation sedimentation tank: as can be seen from the table 1, under the optimal dosage condition of the primary flocculation sedimentation tank, the sludge sedimentation effect is better, the SS of the effluent is lower than that of the raw water, the effluent is clear, the parameters of the old sedimentation tank are proved to meet the sedimentation requirement of the primary flocculation sedimentation tank, and the investment cost is reduced to the greatest extent.
TABLE 1 Primary flocculation run data analysis (2023 4 months 1 day-30 days)
2. Evaporation system result analysis
The concentrated solution is concentrated by an evaporation A, B, C machine to produce evaporation mother liquor, the evaporation mother liquor enters a drying A, B machine to be dried, the super-concentrated solution and salt mud are separated by a centrifugal machine, the super-concentrated solution is transported to an incineration plant for back spraying, the salt mud is treated in a salt mud park, condensed water enters an RO system and then is discharged after reaching the standard, and A, B, C evaporation alternately operates. By comparing the operation parameters of the evaporation system under the same operation conditions before and after the test, the following conclusion is obtained:
1) And (3) lifting the treated water: as can be seen from Table 2, after the test, the overall treatment water quantity of the A, B, C machine system is obviously improved by more than 60 percent. Considering that the water volume is greatly improved, there are two main reasons: firstly, the A, B machine just changes the heating tube bundle, so that the equipment performance is improved; the second is that the pretreatment removes organic matters and hardness in the water, the water quality entering the evaporation system is better, the scaling is delayed, and the treatment efficiency is improved;
2) The concentration discharge rate is reduced: as can be seen from Table 2, after the primary flocculation test, the comprehensive average concentration discharge rate of the A, B, C machine is about 22%,2021 is limited by the performance of evaporation equipment and the reasons of tube bundle scaling, the concentration discharge rate of the A, B machine is maintained above 35%, the stability is poor, and the cleaning is frequent; the average concentration discharge rate of the machine C is also reduced;
TABLE 2 analysis of evaporation system throughput and evaporation mother liquor generation
3) MVR (C machine) heat exchange efficiency promotes: as can be seen from table 3, the heat exchange efficiency of the first-effect plate heat exchanger and the second-effect plate heat exchanger of the machine C is obviously improved, which indicates that the scaling of the plate heat exchanger is relieved;
TABLE 3 comparative analysis of heat exchange efficiency of MVR evaporation (C machine) system
4) Improvement of scale properties: as can be seen from fig. 4, the scale formation properties of the machine a tube bundles before and after the primary flocculation test are different, the scale of the tube bundles before transformation is more compact, the color is black brown, and the tube bundles are difficult to clean; after transformation, the scale color of the tube bundle is grey white, the scale is loose, and the cleaning is easy;
5) The main inorganic component of the scale is CaSO 4 : as can be seen from Table 4, the scale after the test is grey in color, and the colored organic matters in the water are mainly removed; in addition, XRD inorganic component analysis shows that the scale is mainly CaSO before and after test 4 The gypsum produced by sintering shows the necessity of further removing the hardness in water, the pH value is strictly controlled to be more than 12 by pretreatment, the magnesium hardness and most of the calcium hardness in water are completely removed, and meanwhile, sodium carbonate can be added in the pretreatment section to continuously reduce the risk of calcium hardness scaling.
TABLE 4 analysis of evaporated scale inorganic components before and after transformation
Claims (9)
1. The concentrated solution full-quantification treatment system is characterized by comprising a raw liquid pool, a primary flocculation reaction tank, a primary flocculation sedimentation tank, an intermediate water tank, an alkali reaction tank, a sedimentation tank, a silicon carbide membrane unit, an acid reaction tank, a first sludge storage tank, a second sludge storage tank and a filter press; the outlet of the raw liquid pool is connected with the inlet of the primary flocculation reaction tank; the outlet of the primary flocculation reaction tank is connected with the inlet of the primary flocculation sedimentation tank; the supernatant outlet of the primary flocculation sedimentation tank is connected with the inlet of the intermediate water tank; the outlet of the intermediate water tank is connected with the inlet of the alkali reaction tank; the outlet of the alkali reaction tank is connected with the inlet of the sedimentation tank; the supernatant outlet of the sedimentation tank is connected with the inlet of the silicon carbide membrane unit; the supernatant outlet of the silicon carbide film unit is connected with the inlet of the acid reaction tank;
further comprises: a pump for conveying the sediment in the primary flocculation sedimentation tank to the first sludge storage tank, and conveying the sediment obtained by filtering the silicon carbide membrane unit and the sediment in the sedimentation tank to the second sludge storage tank; and a high-pressure pump for delivering the sediment in the first sludge storage tank and the second sludge storage tank to the filter press for dehydration; the liquid outlet of the filter press is connected with the inlet of the alkali reaction tank and the inlet of the acid reaction tank; the method comprises the steps of respectively storing acid flocculated sludge and alkaline softened sludge by adopting a first sludge storage tank and a second sludge storage tank, so that the two types of sludge are subjected to separate filter pressing;
the primary flocculation sedimentation tank adopts a central diversion cylinder type water distribution;
the maximum transmembrane pressure difference of the silicon carbide film in the silicon carbide film unit is 0.4Mpa, and the film flux is 0.3m 3 /(m 2 •h)；
The device also comprises a middle water tank, an evaporation unit, a primary mother liquor tank, a drying unit and a secondary mother liquor tank; the inlet of the intermediate water tank is connected with the outlet of the acid reaction tank, and the supernatant outlet of the intermediate water tank is connected with the inlet of the evaporation unit; the outlet of the evaporation unit is connected with the inlet of the primary mother liquid pool; the outlet of the primary mother liquor pool is connected with the inlet of the drying unit; and the outlet of the drying unit is connected with the inlet of the secondary mother liquid pool.
2. The concentrated solution full-scale treatment system according to claim 1, further comprising a flocculation reagent storage and addition unit that adds a flocculation reagent to the primary flocculation reaction tank, and a liquid alkali storage and addition unit that adds liquid alkali to the alkali reaction tank.
3. The concentrate full-scale treatment system of claim 2, wherein the flocculating agent is prepared by:
AlCl is mixed according to the mole ratio of Si/Al of 0.1-0.4 3 Mixing the solution and gamma-aminopropyl diethoxymethyl silane, stirring at room temperature, dropwise adding NaOH solution by adopting a constant flow pump until the alkalization degree B reaches 0.5-2.0, and completely reacting to obtain the flocculation medicament.
4. The concentrated solution full-scale treatment system according to claim 2, wherein the addition amount of the flocculation reagent is 0.8 to 1.0wt% of the total amount of the concentrated solution entering the primary flocculation reaction tank; the reaction time in the primary flocculation reaction tank is 10min, and the residence time in the primary flocculation sedimentation tank is 3h.
5. The concentrate full scale treatment system of claim 2, wherein the sediment in the intermediate pond is pumped to the second sludge storage tank.
6. A method for performing a full-scale treatment of a concentrate using the full-scale treatment system for a concentrate according to any one of claims 1 to 5, comprising the steps of:
the concentrated solution enters a primary flocculation reaction tank after passing through a raw liquid pool, and a flocculation reagent is added into the primary flocculation reaction tank to carry out flocculation reaction; the concentrated solution after flocculation reaction enters a primary flocculation sedimentation tank for sedimentation, after sedimentation, supernatant in the primary flocculation sedimentation tank enters an intermediate water tank, and sediment in the primary flocculation sedimentation tank is pumped into a first sludge storage tank; the supernatant in the intermediate water tank enters an alkali reaction tank and reacts with liquid alkali, the reaction product enters a sedimentation tank, after sedimentation, the supernatant in the sedimentation tank is filtered by a silicon carbide membrane unit, the filtrate enters an acid reaction tank for reaction treatment, and sediment in the sedimentation tank and sediment obtained by filtration by the silicon carbide membrane unit are pumped into a second sludge storage tank; and the filter pressing liquid generated after the sediment in the first sludge storage tank is dehydrated by the filter press enters the alkali reaction tank for subsequent treatment, and the filter pressing liquid generated after the sediment in the second sludge storage tank is dehydrated by the filter press enters the acid reaction tank for subsequent treatment.
7. The method as recited in claim 6, further comprising: the treatment liquid in the acid reaction tank enters an intermediate water tank for precipitation, supernatant obtained by precipitation in the intermediate water tank enters an evaporation unit for treatment to obtain primary mother liquid, the primary mother liquid enters a primary mother liquid tank for treatment, and then enters a secondary mother liquid tank for subsequent treatment after being treated by a drying unit.
8. The method of claim 6, wherein the water content of the sludge cake produced after dewatering by the filter press is less than 60%.
9. The method of claim 7, wherein the silicon carbide membrane unit has a water production rate of 90% or more; the concentration yield of the drying unit is below 50%.
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