CN116854227B - Defoaming method - Google Patents
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- CN116854227B CN116854227B CN202310799812.6A CN202310799812A CN116854227B CN 116854227 B CN116854227 B CN 116854227B CN 202310799812 A CN202310799812 A CN 202310799812A CN 116854227 B CN116854227 B CN 116854227B
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- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 55
- 239000006260 foam Substances 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 claims abstract description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 50
- 239000000243 solution Substances 0.000 claims description 39
- 239000007788 liquid Substances 0.000 claims description 20
- 238000004062 sedimentation Methods 0.000 claims description 16
- 239000011550 stock solution Substances 0.000 claims description 16
- 239000012141 concentrate Substances 0.000 claims description 9
- 238000012937 correction Methods 0.000 claims description 6
- 230000000694 effects Effects 0.000 abstract description 20
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000008394 flocculating agent Substances 0.000 description 8
- 239000006228 supernatant Substances 0.000 description 8
- 238000002474 experimental method Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000005189 flocculation Methods 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 239000000149 chemical water pollutant Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000016615 flocculation Effects 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 150000003841 chloride salts Chemical class 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- -1 hydrogen ions Chemical class 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000002518 antifoaming agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003851 biochemical process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical class OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- NBBQQQJUOYRZCA-UHFFFAOYSA-N diethoxymethylsilane Chemical compound CCOC([SiH3])OCC NBBQQQJUOYRZCA-UHFFFAOYSA-N 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 150000004673 fluoride salts Chemical class 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a defoaming method, and belongs to the technical field of concentrated solution treatment. The defoaming method is used for removing foam generated during the treatment of concentrated solution with the bicarbonate concentration higher than 2000mg/L in raw water, and comprises the following steps: adding the solution with the addition concentration Q into a raw solution pool 1 Is added into a reaction tank with the addition concentration of Q 2 Is a flocculant of (2). The invention is applied to the aspect of concentrated solution treatment, solves the problems of high foam removal difficulty caused by the generation of a large amount of foam when the existing concentrated solution with the alkalinity higher than 2000mg/L is treated, and greatly influences the production efficiency and the concentrated solution treatment effect, and has the characteristics of high foam removal rate, convenient operation and good concentrated solution treatment effect.
Description
Technical Field
The invention belongs to the technical field of concentrated solution treatment, and particularly relates to a defoaming method.
Background
The concentrated solution has the characteristics of high salt content, complex pollution components, high organic pollutant content, easy scaling and the like, is limited by treatment technology and economic rationality, and is a difficult point in the industry all the time. The general thinking about concentrate treatment at the present stage is control in a system, so that the concentrate is reduced, and finally, the concentrate is reasonably treated as far as possible.
Chinese patent CN104478157a discloses a method for treating a landfill leachate nanofiltration concentrate, and specifically discloses the following steps: pumping the landfill leachate nanofiltration concentrated solution into a reaction tank, and then adding a coagulant, a defoaming agent and a flocculating agent into the reaction tank for reaction; after the reaction is finished, the mixture flows into a sedimentation tank through a pipe to carry out solid-liquid separation, so as to obtain sediment sludge and sediment clear liquid; the precipitated sludge is pumped into a dehydrator for separation, and the generated dehydrated clear liquid and the precipitated clear liquid are sent into a micro-electrolysis reactor for oxidization; adding alkali into the oxidized effluent to adjust the pH value to 7-9, then sending the effluent into an ozone reaction tank for further oxidation, and introducing ozone generated by an ozone generator into the ozone reaction tank for aeration; the nanofiltration concentrated solution treated by the steps can flow back to a biochemical system. The technology is skillfully combined with a biochemical process through a physical-chemical reaction, so that the technology has the advantages of stable operation, easy operation and maintenance, lower operation cost and high treatment efficiency, and simultaneously solves the problem of insufficient carbon source of landfill leachate.
However, when the alkalinity of the concentrated solution is higher and reaches more than 2000mg/L, after the acid flocculation reagent is added in the pretreatment flocculation process, a large amount of foam can be generated in the tank body of the reaction tank, the foam escapes from the reaction tank and enters the next-stage sedimentation tank, the sedimentation effect of the sedimentation tank is greatly influenced, meanwhile, as the components of the concentrated solution are complex and substances such as mud are often mixed, the foam removal difficulty is extremely high, the foam is usually removed manually in the existing treatment mode, but the working efficiency is low, and meanwhile, the problem of poor treatment effect exists.
Disclosure of Invention
Aiming at the defects existing in the prior art, the invention aims to solve the technical problems that the foam removal difficulty is high and the production efficiency and the concentrate treatment effect are greatly influenced due to the generation of a large amount of foam when the existing concentrate with the alkalinity higher than 2000mg/L is treated, and provides the defoaming method with high foam removal rate, convenient operation and good concentrate treatment effect.
In order to solve the technical problems, the invention adopts the following technical scheme:
the invention provides a defoaming method, which is used for removing foam generated during the treatment of concentrated solution with the bicarbonate concentration higher than 2000mg/L in raw water, and comprises the following steps: adding the solution with the addition concentration Q into a raw solution pool 1 Is added into a reaction tank with the addition concentration of Q 2 Is a flocculant of the formula Q 1 And said Q 2 The units of the (B) are mL/L, and the mass fraction of the sulfuric acid solution is 98%;
the Q is 1 Calculated by the following formula:
Q l ＝a×T 1
in the formula, a is a correction coefficient, and the value of a is any value of 0.90-1.20; t (T) 1 The unit mL/L is the theoretical addition concentration of the sulfuric acid solution required for meeting the expected alkalinity removal rate of the effluent of the stock solution pond;
the T is 1 Calculated by the following formula:
in the above-mentioned formula(s),the concentration of bicarbonate in raw water is mg/L; r1 is the expected alkalinity removal rate in the stock solution pool;
the Q is 2 Calculated by the following formula:
Q 2 ＝b×T 2 +c×T 3
in the formula, b and c are correction coefficients, wherein the value range of b is any one value of 0.80-1.20, and the value range of c is any one value of 0.80-1.20; t (T) 2 The unit mL/L is the theoretical addition concentration of the flocculant required for meeting the expected alkalinity removal rate of the effluent of the reaction tank; t (T) 3 The unit mL/L is the theoretical addition concentration of the flocculant required for meeting the expected COD removal rate of the effluent of the reaction tank;
the T is 2 Calculated by the following formula:
in the above-mentioned formula(s),the unit of bicarbonate concentration in the reaction tank is mg/L; r2 is the expected alkalinity removal rate in the reaction tank; m is the molecular weight of the flocculant;
the T is 3 Calculated by the following formula:
T 3 ＝-0.0008A 3 +0.1485A 2 -8.8199A+177.3
in the above formula, a is a value obtained by multiplying the expected COD removal rate by 100.
Preferably, if the expected alkalinity removal rate R1 in the stock solution tank is any value of 60% -65%, the value of a is any value of 0.9-1.0; if the expected alkalinity removing rate R1 in the original liquid pool is any value of 65% -70%, the value of a is any value of 1.0-1.2.
Preferably, if the expected alkalinity removal rate R2 in the reaction tank is any value of 30% -35%, the value b is any value of 0.8-1.0; if the expected alkalinity removing rate R2 in the reaction tank is any value of 35% -40%, the value b is any value of 1.0-1.2.
Preferably, when the pH value of the inlet water is regulated to 3-6, if the expected COD removal rate in the reaction tank is any value of 50% -60%, the value of c is any value of 0.8-1.0; if the expected COD removal rate in the reaction tank is any value of 60% -70%, the value of c is any value of 1.0-1.2.
Preferably, the RI has a value of 60% or more and 70% or less than R1.
Preferably, the value of R2 is more than or equal to 30% and less than or equal to 40% of R2.
Preferably, the value of A is more than or equal to 50 and less than or equal to 70.
Preferably, the value of M is 200.
Preferably, the flocculant is an SC-101L flocculant.
Preferably, foam in the sedimentation tank guide cylinder is pumped into the raw liquid pool by adopting a pneumatic diaphragm pump pumping mode to perform defoaming.
Compared with the prior art, the invention has the beneficial effects that:
the invention provides a defoaming method, which is characterized in that sulfuric acid solution is added into a stock solution tank, flocculant is added into a reaction tank, and meanwhile, the calculation method of the addition concentration of the sulfuric acid solution and the flocculant is limited, so that the foam dissolution speed can be effectively reduced, the foam production amount is reduced, the escape of foam in the reaction tank and a sedimentation tank is reduced under the condition of considering the COD removal rate, and the defoaming method has the characteristics of high foam removal rate, convenience in operation and good concentrated solution treatment effect.
Drawings
FIG. 1 is an experimental diagram of example 1 of the present invention;
FIG. 2 is a diagram showing experimental results of example 2 of the present invention;
FIG. 3 is a diagram showing experimental results of example 3 of the present invention;
FIG. 4 is a diagram showing experimental results of example 4 of the present invention;
FIG. 5 is a diagram showing experimental results of example 5 of the present invention;
FIG. 6 is a diagram showing experimental results of example 6 of the present invention;
FIG. 7 is a graph showing experimental results of comparative examples 1-2 according to the present invention.
Detailed Description
The technical scheme in the specific embodiment of the invention 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 invention. 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 invention.
The invention provides a defoaming method, which is used for removing foam generated during the treatment of concentrated solution with the bicarbonate concentration higher than 2000mg/L in raw water, and comprises the following steps: adding the solution with the addition concentration Q into a raw solution pool 1 Is added into a reaction tank with the addition concentration of Q 2 Is a flocculant of the formula Q 1 And said Q 2 The units of the (B) are mL/L, and the mass fraction of the sulfuric acid solution is 98%;
the Q is 1 Calculated by the following formula:
Q 1 ＝a×T I
in the formula, a is a correction coefficient, and the value of a is any value of 0.90-1.20; t (T) 1 The unit mL/L is the theoretical addition concentration of the sulfuric acid solution required for meeting the expected alkalinity removal rate of the effluent of the stock solution pond;
the T is 1 Calculated by the following formula:
in the above-mentioned formula(s),the concentration of bicarbonate in raw water is mg/L; r1 is the expected alkalinity removal rate in the stock solution pool; wherein 98 is the molecular weight of sulfuric acid; 1.84 is the density of the sulfuric acid solution in g/cm 3 The method comprises the steps of carrying out a first treatment on the surface of the 0.98% of sulfuric acid by mass fraction, 98%;
the Q is 2 Calculated by the following formula:
Q 2 ＝b×T 2 +c×T 3
in the formula, b and c are correction coefficients, and the value of b is in the range of 0.80-1.20The value of c is any value in the range of 0.80-1.20; t (T) 2 The unit mL/L is the theoretical addition concentration of the flocculant required for meeting the expected alkalinity removal rate of the effluent of the reaction tank; t (T) 3 The unit mL/L is the theoretical addition concentration of the flocculant required for meeting the expected COD removal rate of the effluent of the reaction tank;
the T is 2 Calculated by the following formula:
in the above-mentioned formula(s),the unit of bicarbonate concentration in the reaction tank is mg/L; r2 is the expected alkalinity removal rate in the reaction tank; m is the molecular weight of the flocculant; wherein 1.45 is the density of the flocculant, the unit g/cm 3 ；
The T is 3 Calculated by the following formula:
T 3 ＝-0.0008A 3 +0.1485A 2 -8.8199A+177.3
in the above formula, a is a value obtained by multiplying the expected COD removal rate by 100.
As introduced in the background art, when the alkalinity (i.e. bicarbonate concentration) of the concentrated solution is higher and reaches more than 2000mg/L, a large amount of foam can be generated in the reaction tank body after the flocculating agent is added in the pretreatment flocculation process, the foam escapes from the reaction tank and enters the next-stage sedimentation tank, the sedimentation effect of the sedimentation tank is greatly affected, and meanwhile, as the components of the concentrated solution are complex and substances such as mud and the like are often mixed, the foam removal difficulty is extremely high. In order to reduce the generation of foam, the method can reduce the dissolution rate of the foam and simultaneously ensure the removal rate of COD by adding the sulfuric acid solution into the raw liquid pool and adding the flocculating agent into the reaction tank, and particularly, the method has the characteristics of high foam removal rate, convenient operation and good concentrated solution treatment effect by adding the flocculating agent into the reaction tank to remove a part of alkalinity (60% -70%) and COD (defoaming+COD) after removing a part of alkalinity (60% -70%) and adding the flocculating agent into the raw liquid pool, wherein the COD removal rate reaches 50% -70%, and the calculation mode of the addition amount of the sulfuric acid solution and the flocculating agent is limited according to the project removal rate requirement. The alkalinity in the wastewater mainly refers to the sum of carbonate and bicarbonate content, and in terms of HCO3-, generally, after an acidic flocculation reagent is added in the pretreatment flocculation process, the bicarbonate in the tank body of the reaction tank and hydrogen ions in the acidic flocculant generate carbon dioxide, namely a large amount of foam is generated. It is emphasized that adding sulfuric acid solution into the stock solution pond, hydrogen ions of bicarbonate and sulfuric acid generate carbon dioxide to escape, and the defoaming effect is guaranteed, however, adding concentrated sulfuric acid also can cause great influence on the removal rate of COD, and is unfavorable for removal of COD, so that when all alkalinity is removed at one time by adding sulfuric acid solution into the stock solution pond, the COD removal effect is not obtained by adjusting the adding amount of the flocculant at any time later.
In a preferred embodiment, if the expected alkalinity removal rate R1 in the stock solution tank is any value of 60% -65%, then a takes on any value of 0.9-1.0; if the expected alkalinity removing rate R1 in the original liquid pool is any value of 65% -70%, the value of a is any value of 1.0-1.2. This embodiment specifically defines that the value of a is adjusted according to the alkalinity removal rate of the effluent of the stock solution tank (i.e., the expected alkalinity removal rate R1 in the stock solution tank), so as to ensure the defoaming effect.
In a preferred embodiment, if the desired alkalinity removal rate R2 in the reaction tank is any value from 30% to 35%, then b takes on any value from 0.8 to 1.0; if the expected alkalinity removing rate R2 in the reaction tank is any value of 35% -40%, the value b is any value of 1.0-1.2. This example specifically defines the adjustment of the value of b according to the alkalinity removal rate requirement of the reactor effluent (i.e., the expected alkalinity removal rate R2 in the reactor), further ensuring the defoaming effect.
In a preferred embodiment, c is any value from 0.8 to 1.0 when the pH of the feed water is adjusted to 3-6, if the expected COD removal rate in the reaction tank is any value from 50% to 60%; if the expected COD removal rate in the reaction tank is any value of 60% -70%, the value of c is any value of 1.0-1.2. This example defines in particular that the pH of the feed to the reaction tank is adjusted to 3-6, since at this pH a better action of the flocculant is favored.
In a preferred embodiment, the value of R1 satisfies 60% to 70% of R1. In a preferred embodiment, the value of R2 satisfies 30% to 40% of R2. In a preferred embodiment, the value of A satisfies 50.ltoreq.A.ltoreq.70. It is understood that the above-described desired alkalinity removal rate and desired COD removal rate are the alkalinity removal rate and COD removal rate required to be achieved based on the processing needs of the project.
In a preferred embodiment, the value of M is 200. Further, the flocculant is an SC-101L flocculant. The flocculant is a covalent bond type inorganic-organic composite flocculant and is prepared by the following method: adding AlCl quantitatively into a three-neck flask according to the Si/Al molar ratio of 0.1-0.4 3 Mixing the solution and gamma-aminopropyl diethoxymethyl silane, stirring at room temperature, dripping NaOH solution with constant flow pump to obtain the final product 3 The ratio is 0.5-2.0, the alkalization degree B=0.5-2.0, and the obtained solution is stood for complete reaction, thus obtaining the covalent bond inorganic-organic composite flocculant.
In a preferred embodiment, foam in the sedimentation tank guide cylinder is pumped into the raw liquid pool by adopting a pneumatic diaphragm pump for defoaming. In the defoaming process, raw water firstly enters a raw liquid pool, sulfuric acid solution is added into the raw liquid pool, and the adding quantity Q of the sulfuric acid solution added into the raw liquid pool is limited 1 Removing oneAfter part of alkalinity (60% -70%), the purpose of defoaming is achieved, the treatment liquid treated by the stock solution pond enters a reaction tank, and flocculant is added into the reaction tank, and the adding amount Q of the flocculant added into the reaction tank is limited 2 The defoaming requirement is guaranteed, the removal efficiency of COD is guaranteed, meanwhile, because less foam is generated in the reaction tank (a large amount of foam is generated in the original liquid pool), the foam in the reaction tank is removed in a manual skimming mode, and the treatment liquid in the reaction tank further enters the sedimentation tank for sedimentation, so that the sedimentation effect of the sedimentation tank is effectively guaranteed. Meanwhile, as the foam in the guide cylinder of the sedimentation tank is serious, the foam is pumped into the raw liquid tank for defoaming in a limited mode by utilizing the pneumatic diaphragm pump to suck, and the defoaming effect is further ensured.
In order to more clearly describe the defoaming method provided by the embodiments of the present invention in detail, the following description will be made with reference to specific embodiments.
Example 1
The raw water quality analysis results are shown in Table 1.
TABLE 1 raw water quality analysis results
The experimental steps are as follows: taking 500mL of raw water in a 500mL beaker, adding 1mL/L concentrated sulfuric acid, and measuring pH; 2mL/LSC-101L flocculant was added, stirred for 10min, precipitated for about 1h, and the supernatant COD was determined.
Example 2
Raw water quality is the same as in example 1.
The experimental steps are as follows: taking 500mL of raw water in a 500mL beaker, adding 0.8mL/L concentrated sulfuric acid, and measuring pH; 1mL/LSC-101L flocculant was added, stirred for 10min, precipitated for about 1h, and the supernatant COD was determined.
Example 3
Raw water quality is the same as in example 1.
The experimental steps are as follows: taking 500mL of raw water in a 500mL beaker, adding 0.6mL/L concentrated sulfuric acid, and measuring pH; 1mL/LSC-101L flocculant was added, stirred for 10min, precipitated for about 1h, and the supernatant COD was determined.
Example 4
Raw water quality is the same as in example 1.
The experimental steps are as follows: taking 500mL of raw water in 2 500mL beakers, adding 0.4mL/L of concentrated sulfuric acid, and measuring pH; 1 and 2mL/LSC-101L flocculant were added, stirred for 10min, precipitated for about 1h, and the COD of the supernatant was determined.
Example 5
Raw water quality is the same as in example 1.
The experimental steps are as follows: taking 500mL of raw water in 2 500mL beakers, adding 0.2mL/L of concentrated sulfuric acid, and measuring pH; 1 and 2mL/LSC-101L flocculant were added, stirred for 10min, precipitated for about 1h, and the COD of the supernatant was determined.
Example 6
Raw water quality is the same as in example 1.
The experimental steps are as follows: taking 500mL of raw water in a 500mL beaker, adding 0.1mL/L of concentrated sulfuric acid, and measuring pH; 5mL/LSC-101L flocculant was added, stirred for 10min, precipitated for about 1h, and the supernatant COD was determined.
Comparative example 1
Raw water quality is the same as in example 1.
The experimental steps are as follows: 500mL of raw water was placed in a 500mL beaker, 3mL of SC-101L flocculant was added to the beaker at a time, stirred for 10min, precipitated for about 1h, and the COD of the supernatant was measured.
Comparative example 2
Raw water quality is the same as in example 1.
The experimental steps are as follows: 500mL of raw water was placed in a 500mL beaker, 5mL of SC-101L flocculant was added to the beaker at a time, stirred for 10min, precipitated for about 1h, and the COD of the supernatant was measured.
Results of Performance test
The experimental results of examples 1 to 6 are shown in Table 1, and the experimental phenomena are shown in FIGS. 1 to 6, wherein experiment one is example 1, experiment two is example 2, experiment three is example 3, experiment four is example 4, experiment five is example 5, and experiment six is example 6.
TABLE 1 Experimental results for examples 1-6
As can be seen from the results in Table 1 and FIGS. 1 to 6, the addition of the concentrated sulfuric acid, followed by the addition of the SC-101L flocculant, did not effectively eliminate foam, but had a large effect on COD removal rate and on COD of the effluent water. Among them, fig. 1 shows that the defoaming effect is better (because the amount of the concentrated sulfuric acid added in fig. 1 is relatively maximum), but it affects the removal rate of COD, and in example 4, although the removal rate of COD is higher, the defoaming effect is poor, and the addition amount of the sulfuric acid solution and the addition amount of the flocculant in example 6 are obtained according to the addition amount calculation method provided by the present invention, as can be seen in table 1 and fig. 6, both the defoaming effect and the removal rate of COD meet the expected requirements.
The results of experiments of comparative examples 1 to 2 are shown in Table 2, and the defoaming effect is shown in FIG. 7, and the foam is serious although the removal rate of COD is ensured.
Table 2 Experimental results for comparative examples 1-2
Description of the preferred embodiments
The water quality of the feed water of a certain concentrate treatment project is shown in Table 3.
Table 3 item of influent water quality
| Detecting items | Concentrated solution (mg/L) |
| Conductivity of | 83100 |
| PH | 6.7 |
| COD | 2000 |
| Soluble solid TDS | 55500 |
| Total nitrogen | 154 |
| Ammonia nitrogen | 25.9 |
| Fluoride compounds | 0.54 |
| Chlorides (CPS) | 20600 |
| Sulfate salt | 9930 |
| Calcium | 931 |
| Magnesium (Mg) | 392 |
| Total hardness (mmol/L) | 43 |
| Bicarbonate salt | 2030 |
| Nitrate nitrogen | 117 |
Adding a reagent in two sections, namely adding concentrated sulfuric acid into a stock solution pond in a first section, adding a flocculating agent into a deep flocculation reaction tank (reaction tank) in a second section, wherein the adding amount of the sulfuric acid in the first section is 0.53mL/L, the adding amount of the flocculating agent in the second section is 6.48mL/L, and the determining process of the adding amount is as follows:
Q 1 ＝a×T I
the T is 1 Calculated by the following formula:
wherein, the value of a is 0.9, the expected alkalinity removal rate R1 in the stock solution pool is 60 percent, calculating to obtain T 1 ＝0.54。
The Q is 2 Calculated by the following formula:
Q 2 ＝b×T 2 +c×T 3
wherein, the value of b is 0.8, and the value of c is 0.80;
the T is 2 Calculated by the following formula:
the expected alkalinity removal rate R2 in the reaction tank was 30%, m=200,calculating to obtain T 2 ＝0.55。
T 3 ＝-0.0008A 3 +0.1485A 2 -8.8199A+177.3
In the above formula, A is 50, and T is calculated 3 ＝7.55。
Treatment results: the alkalinity removing rate is 75%, the COD removing rate is 50%, and the expected treatment result of project requirements is achieved.
Claims (10)
1. A defoaming method for removing foam generated in the treatment of a concentrate having a bicarbonate concentration of more than 2000mg/L in raw water, comprising: adding the solution with the addition concentration Q into a raw solution pool 1 Is added into a reaction tank with the addition concentration of Q 2 Is a flocculant of the formula Q 1 And said Q 2 The units of the (B) are mL/L, and the mass fraction of the sulfuric acid solution is 98%;
the Q is 1 Calculated by the following formula:
Q 1 ＝a×T 1
in the formula, a is a correction coefficient, and the value of a is any value of 0.90-1.20; t (T) 1 The unit mL/L is the theoretical addition concentration of the sulfuric acid solution required for meeting the expected alkalinity removal rate of the effluent of the stock solution pond;
the T is 1 Calculated by the following formula:
in the above-mentioned formula(s),the concentration of bicarbonate in raw water is mg/L; r1 is the expected alkalinity removal rate in the stock solution pool;
the Q is 2 Calculated by the following formula:
Q 2 ＝b×T 2 +c×T 3
in the formula, b and c are correction coefficients, and the value range of b is 0.80-any value of 1.20, said value of c being in the range of any value of 0.80-1.20; t (T) 2 The unit mL/L is the theoretical addition concentration of the flocculant required for meeting the expected alkalinity removal rate of the effluent of the reaction tank; t (T) 3 The unit mL/L is the theoretical addition concentration of the flocculant required for meeting the expected COD removal rate of the effluent of the reaction tank;
the T is 2 Calculated by the following formula:
in the above-mentioned formula(s),the unit of bicarbonate concentration in the reaction tank is mg/L; r2 is the expected alkalinity removal rate in the reaction tank; m is the molecular weight of the flocculant;
the T is 3 Calculated by the following formula:
T 3 ＝-0.0008A 3 +0.1485A 2 -8.8199A+177.3
in the above formula, a is a value obtained by multiplying the expected COD removal rate by 100.
2. The defoaming method according to claim 1, wherein,
if the expected alkalinity removal rate R1 in the original liquid pool is any value of 60% -65%, the value of a is any value of 0.9-1.0;
if the expected alkalinity removing rate R1 in the original liquid pool is any value of 65% -70%, the value of a is any value of 1.0-1.2.
3. The defoaming method according to claim 1, wherein,
if the expected alkalinity removal rate R2 in the reaction tank is any value of 30% -35%, b is any value of 0.8-1.0;
if the expected alkalinity removing rate R2 in the reaction tank is any value of 35% -40%, the value b is any value of 1.0-1.2.
4. The defoaming method according to claim 1, wherein when the pH value of the inlet water is adjusted to 3 to 6,
if the expected COD removal rate in the reaction tank is any value of 50% -60%, c is any value of 0.8-1.0;
if the expected COD removal rate in the reaction tank is any value of 60% -70%, the value of c is any value of 1.0-1.2.
5. The defoaming method according to claim 1, wherein the value of R1 satisfies 60% to 70% of R1.
6. The defoaming method according to claim 1, wherein the value of R2 satisfies 30% to 40% of R2.
7. The defoaming method according to claim 1, wherein the value of a satisfies 50.ltoreq.a.ltoreq.70.
8. The method of defoaming according to claim 1, wherein said M has a value of 200.
9. The method of defoaming according to claim 8, wherein the flocculant is an SC-101L flocculant.
10. The defoaming method according to claim 1, wherein foam in the sedimentation tank guide cylinder is pumped into the raw liquid tank by a pneumatic diaphragm pump for defoaming.
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| JP2017023918A (en) * | 2015-07-17 | 2017-02-02 | 国立大学法人北見工業大学 | Treatment method of drainage water containing medicine and treatment device of drainage water |
| CN112499743A (en) * | 2020-12-03 | 2021-03-16 | 东莞道汇环保科技股份有限公司 | Defoaming device for leachate recharge and using method thereof |
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| JP2017023918A (en) * | 2015-07-17 | 2017-02-02 | 国立大学法人北見工業大学 | Treatment method of drainage water containing medicine and treatment device of drainage water |
| CN112499743A (en) * | 2020-12-03 | 2021-03-16 | 东莞道汇环保科技股份有限公司 | Defoaming device for leachate recharge and using method thereof |
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Address after: No. 20 Ningde Road, Laoshan District, Qingdao City, Shandong Province, 266071 Patentee after: Qingdao Water Group Co.,Ltd. Country or region after: China Patentee after: Qingdao Jieyuan environment Co.,Ltd. Patentee after: Qingdao Solid Waste Disposal Co.,Ltd. Patentee after: Beijing Origin Water Technology Co.,Ltd. Patentee after: Zhongqi Guoyun Environmental Protection Technology Co.,Ltd. Patentee after: Qingdao Xiaojianxi leachate treatment Co.,Ltd. Address before: 266000 No. 55 Taiping Road, Shinan District, Qingdao, Shandong Patentee before: Qingdao Water Group Co.,Ltd. Country or region before: China Patentee before: Qingdao Jieyuan environment Co.,Ltd. Patentee before: Qingdao Solid Waste Disposal Co.,Ltd. Patentee before: Beijing Origin Water Technology Co.,Ltd. Patentee before: Zhongqi Guoyun Environmental Protection Technology Co.,Ltd. Patentee before: Qingdao Xiaojianxi leachate treatment Co.,Ltd. |