CN111392952B - Treatment process of high-salt high-organic matter waste liquid and used waste liquid treatment equipment - Google Patents
Treatment process of high-salt high-organic matter waste liquid and used waste liquid treatment equipment Download PDFInfo
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- CN111392952B CN111392952B CN202010497119.XA CN202010497119A CN111392952B CN 111392952 B CN111392952 B CN 111392952B CN 202010497119 A CN202010497119 A CN 202010497119A CN 111392952 B CN111392952 B CN 111392952B
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention discloses a treatment process of high-salt high-organic matter waste liquid and waste liquid treatment equipment used by the same, wherein the treatment process comprises the following steps: heating the waste liquid to 60-90 deg.C, adding a blending agent capable of increasing TDS or reducing COD into the waste liquid, and making the pH of the waste liquid be greater than 5; the waste liquid is sent into the drying machine to be dried into solid materials, the treatment equipment comprises a blending tank, a raw liquid pump, a waste liquid pump, a first heat exchanger, a dispensing tank, a dosing pump, the drying machine, a device drainage pipeline and a control system, the waste liquid is sent into the blending tank through the raw liquid pump, the dosing pump sends a blending agent blended in the dispensing tank into the blending tank, the first heat exchanger heats the waste liquid in the blending tank to a specified temperature, the waste liquid pump sends the blended waste liquid in the blending tank into the drying machine, and the control system controls the drying machine and the waste liquid pump to operate and controls the raw liquid pump and the dosing pump to start and stop in a linkage manner.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a treatment process of high-salt high-organic matter waste liquid and waste liquid treatment equipment used in the treatment process.
Background
With the continuous and high-speed development of industrialization, a large amount of waste liquid containing high salt and high organic matters is generated in the industries of coal chemical industry, printing and dyeing, papermaking, pharmacy, electroplating and the like. The waste liquid has the following characteristics:
(1) the salt content is high, and the salt content is as high as tens of thousands or even hundreds of thousands of milligrams per liter;
(2) high organic concentrations, typically greater than 2000 milligrams per liter, even up to tens of thousands of milligrams per liter;
(3) the biodegradability is poor, and the BOD/COD value is less than 0.3;
(4) the components are complex and the toxicity is high;
(5) strong acid and strong alkali properties, etc.
The discharge amount of the catalyst is gradually increased year by year, which poses serious threat to the environment and restricts the development of the industry.
Because the waste liquid contains a large amount of toxic substances such as refractory organic matters, heavy metals and the like and has the function of inhibiting ultrahigh salinity, the existing biochemical technology is difficult to be applied. Although the advanced oxidation and evaporative crystallization method can better realize the decomposition of organic matters and the removal of salt, the method has the defects of complex operation, incomplete oxidation, high operation cost and the like. The direct incineration method is a simple method capable of realizing partial resource recovery, but the energy consumption in the incineration process is high due to the large water content in the waste liquid.
Therefore, a more reasonable treatment method for such waste liquid is to remove most of the water therein by a weight reduction technique and then to perform incineration treatment or resource recovery on the reduced residue or concentrated liquid. The current commonly used reduction technology is as follows: the atmospheric enhanced evaporation, multiple-effect evaporation, MVR evaporation and the like, and the evaporation equipment has the following technical problems:
only the high-salt high-organic-matter waste liquid can be concentrated into a viscous concentrated liquid, the concentrated liquid has high water content, the reduction is not thorough, and the subsequent treatment is complicated;
the heat exchanger is easy to be scaled and blocked, and the heat exchange efficiency is low;
the system is difficult to operate stably and needs to be cleaned regularly.
Therefore, it is very urgent to explore an effective reduction processing technology for environmental protection and social development.
Disclosure of Invention
In order to overcome the defects, the invention provides a treatment process of high-salt high-organic-matter waste liquid and used waste liquid treatment equipment, the treatment process of the high-salt high-organic-matter waste liquid and the used waste liquid treatment equipment can automatically and accurately allocate the waste liquid, the waste liquid is directly dried into a solid material with the water content of less than 10%, and the reduction is more thorough.
The technical scheme adopted by the invention for solving the technical problem is as follows: a treatment process of high-salt high-organic matter waste liquid comprises the following specific steps:
the method comprises the following steps: raising the temperature of the waste liquid to 60-90 ℃;
step two: adding a blending agent capable of increasing TDS or reducing COD into the waste liquid to ensure that the pH of the waste liquid is more than 5, and simultaneously ensuring that the TDS and the COD in the waste liquid meet the following formula:
TDS/COD=2～16；
step three: sending the mixed waste liquid into a drier, and directly drying the mixed waste liquid into the waste liquid with the water content of less than 10% and the melting temperature T by the driermSolid material at temperature higher than 100 deg.c.
As a further improvement of the invention, the blending agent in the second step is an inorganic salt blending agent or an oxidation blending agent, wherein the inorganic salt blending agent is one or a combination of ferrous sulfate, sodium sulfate, magnesium sulfate, sodium hydroxide and sodium silicate, and the oxidation blending agent is hydrogen peroxide, sodium hypochlorite or calcium hypochlorite;
the formula for calculating the adding amount of the inorganic salt blending agent is as follows:
adding amount of the inorganic salt blending agent = (2-16) = (original COD of waste liquid) -original TDS of waste liquid;
the formula for calculating the adding amount of the oxidation blending agent is as follows:
adding amount of the oxidation blending agent = (0.3-5) × original COD of the waste liquid;
wherein the unit of the adding amount of the inorganic salt blending agent and the adding amount of the oxidation blending agent is mg/L.
A waste liquid treatment device used in a treatment process of high-salt high-organic matter waste liquid comprises a blending tank, a raw liquid pump, a waste liquid pump, a first heat exchanger, a dispensing tank, a dosing pump, a drying machine, a device drainage pipeline and a control system, wherein the waste liquid is sent into the blending tank through the raw liquid pump, the dosing pump sends a blending agent liquid medicine blended in the blending tank into the blending tank, the waste liquid pump sends the waste liquid blended in the blending tank into the drying machine, the drying machine can dry the waste liquid into a solid material, a discharge hole for discharging the solid material, a steam condensate discharge hole for discharging steam condensate in a drying process and an exhaust hole for discharging secondary steam are formed in the drying machine, the steam condensate discharge hole of the drying machine is communicated with a water inlet of the first heat exchanger, the first heat exchanger is positioned in the blending tank, the first heat exchanger can heat the waste liquid in the blending tank to a designated temperature, a water discharge hole of the first heat exchanger is communicated with inlets of the device drainage pipeline and the dispensing tank, the device is characterized in that a discharge valve is arranged on a drainage pipeline of the device, a water inlet valve is arranged at an inlet of the dispensing groove, the control system controls the discharge valve and the water inlet valve to be linked with each other, the control system controls the raw liquid pump and the dosing pump to be started and stopped in a linked manner, and the control system also controls the drying machine and the waste liquid pump to operate.
As a further improvement of the invention, the drying machine is further provided with a steel structure platform, a heat-insulating layer and a solid material collecting tank, wherein the blending tank and the dosing tank are respectively and fixedly arranged on the steel structure platform, the solid material collecting tank is arranged right below a discharge port of the drying machine, and the heat-insulating layer is coated on the outer sides of the blending tank and the dosing tank.
As a further improvement of the invention, the automatic liquid medicine dispensing device is also provided with a dispensing stirrer and a dispensing stirrer, wherein the dispensing stirrer can stir liquid in the dispensing tank, and the control system controls the dispensing stirrer and the dispensing stirrer to start and stop and controls the dispensing stirrer to be linked with the medicine feeding pump.
As a further improvement of the invention, a pH meter and a temperature sensor are arranged in the blending tank, the pH meter can detect the pH value of the liquid in the blending tank and transmit the pH value to the control system, and the temperature sensor can detect the temperature of the liquid in the blending tank and transmit the temperature to the control system.
As a further improvement of the invention, the drying machine is also provided with a dust and foam removing integrated machine, an air outlet of the drying machine is communicated with an air inlet of the dust and foam removing integrated machine through a pipeline, and the dust and foam removing integrated machine can perform dust removal and foam removing purification treatment on secondary steam entering the drying machine and discharge the secondary steam through the air outlet.
As a further improvement of the invention, the system is also provided with a secondary steam condensing system, the secondary steam condensing system comprises a second heat exchanger, an induced draft fan and an air pipe, an air outlet of the dust and foam removing integrated machine is connected with an air inlet of the second heat exchanger, a condensed water discharge outlet is arranged on the second heat exchanger and is communicated with a wastewater treatment system of a factory, the air outlet of the second heat exchanger is communicated with the air inlet of an exhaust gas pretreatment system of the factory through the air pipe, and the induced draft fan is arranged in the air pipe.
As a further improvement of the invention, the liquid level meter for blending and the liquid level meter for dispensing are also arranged, the liquid level meter for blending can sense the liquid level height in the blending groove and transmit the liquid level height to the control system, and the liquid level meter for dispensing can sense the liquid level height in the blending groove and transmit the liquid level height to the control system.
As a further improvement of the invention, the drier is any one of a disc drier, a spray drier, a film scraper drier, a roller scraper drier and a disc drier.
The invention has the beneficial effects that: the method comprises the steps of firstly adding a pre-blended blending agent into the wastewater, adjusting the pH value of the wastewater to be more than 5, simultaneously adjusting the proportion of a substance which can form a solid state after water in the waste liquid is evaporated to a substance which can form a thick liquid state, further realizing that the waste liquid is sent into a drier to be dried and then forms a solid material with a melting temperature Tm being more than 100 ℃, and realizing that the waste liquid is dried into the solid material with the water content being less than 10% through automatic precise blending by the waste liquid treatment equipment of the invention, so that the reduction is more thorough, and simultaneously avoiding the complicated procedure that the thick paste discharge needs to be further cured; the mode of non-direct contact heat exchange or material film stripping by a scraper blade is adopted, so that the scaling and blockage of the heat exchanger are thoroughly avoided, and the high efficiency and stability of the heat transfer efficiency are ensured; the system disclosed by the invention forms an integrated device, realizes full-automatic control, does not need complicated manual operation, saves manpower, fully utilizes steam condensate of the drying machine to preheat waste liquid through the first heat exchanger, and simultaneously serves as dispensing water, so that the energy consumption and water resources are saved.
Drawings
FIG. 1 is an assembly diagram of a treatment facility for high-salt high-organic matter waste liquid;
FIG. 2 is a schematic diagram of the process of the present invention;
FIG. 3 is a schematic diagram of the configuration of the dispensing system of the present invention.
Drying integrated equipment-1 discharge port-2 allocation system-3
Steel structure platform-301 insulating layer-302 allocation groove-303
Dosage tank-304 blending stirrer-305 blending stirrer-306
315 as medicine feeding pump 313 raw liquid pump 314 butt joint valve
Dust and foam removing integrated machine-4 second heat exchanger-5 induced draft fan-6
Drier-7 waste liquid pump-8 solid material collecting tank-9
Waste liquid-10 solid material-11 steam-12
Condensate water-13 steam condensate water-14 tail gas-15
Detailed Description
Example (b): a treatment process of high-salt high-organic matter waste liquid comprises the following specific steps:
the method comprises the following steps: raising the temperature of the waste liquid 10 to 60-90 ℃;
step two: adding a blending agent into the waste liquid 10 to ensure that the pH of the waste liquid 10 is more than 5, and simultaneously ensuring that TDS and COD in the waste liquid 10 meet the following formula:
TDS/COD=2～16；
step three: sending the mixed waste liquid 10 into a drier 7, and directly drying the mixed waste liquid 10 into a product with the water content of less than 10% and the melting temperature T by the drier 7m Solid material 11 at > 100 ℃.
When the waste liquid 10 is treated, the waste liquid 10 enters the drier 7 after being preheated and added with the blending agent, the waste liquid 10 is directly dried into the solid material 11 with the water content of less than 10% in the drier 7, the reduction is more thorough, meanwhile, the complicated procedure that the thick pasty discharging material needs to be further cured is avoided, the energy is saved, and the treatment is convenient.
Waste liquid 10The regulation principle of adding the blending agent is as follows: the melting temperature of the discharged material after drying the waste liquid 10 is related to the material formed by the waste liquid 10 after water evaporation, part of the material left after water evaporation in the waste liquid 10 forms solid material at a high temperature of 100-150 ℃, and the other part forms thick liquid material, when the proportion of the solid material formed by the material left after water evaporation in the waste liquid 10 at the high temperature of 100-150 ℃ reaches a certain ratio, the waste liquid 10 can be dried to form the melting temperature TmThe solid material 11 with the temperature higher than 100 ℃ is difficult to obtain in the waste liquid 10 when the waste liquid 10 is treated because the proportion of the solid material left after the water in the waste liquid 10 is evaporated at the high temperature of 100-150 ℃, but because the proportion of the solid material left after the water in the waste liquid 10 is evaporated at the high temperature of 100-150 ℃ and the proportion of TDS and COD in the waste liquid 10 are in corresponding relation, when the waste liquid 10 is treated, only the TDS and COD data in the waste liquid 10 need to be detected, and the proportion of the solid material left after the water evaporation to the thick liquid material left at the high temperature of 100-150 ℃ in the waste liquid 10 is judged by the proportion relation between TDS and COD, although the proportion relation between the solid material left after the water evaporation in the waste liquid 10 at the high temperature of 100-150 ℃ and the thick liquid material left after the water evaporation in the waste liquid 10 is different, however, when the ratio of the solid substances formed by the residual substances after the water in the waste liquid 10 is evaporated at a high temperature of 100-150 ℃ to the thick liquid substances formed by the waste liquid 10 after the water is evaporated is adjusted to a proper ratio, the TDS and the COD in the waste liquid 10 can meet the formula, and the discharge temperature T can be realizedm＞100℃。
The ratio of solid substances to thick liquid substances in the waste liquid 10 at a high temperature of 100-150 ℃ is adjusted by adding a blending agent into the waste liquid 10, the ratio enables the substances in the waste liquid 10 to meet the formula, and further enables the solid substances and the thick liquid substances to form a mixture according to a certain range of proportion after the water in the waste liquid 10 is evaporated, the mixture can form solid materials 11 in a sheet, block or strip shape, and the melting temperature T of the solid materials 11mIs > 100 ℃ and thusEnsuring that the discharge material is in a stable solid form.
The blending agent in the second step is an inorganic salt blending agent or an oxidation blending agent, wherein the inorganic salt blending agent is one or a combination of more of ferrous sulfate, sodium sulfate, magnesium sulfate, sodium hydroxide and sodium silicate, and the oxidation blending agent is hydrogen peroxide, sodium hypochlorite or calcium hypochlorite;
the formula for calculating the adding amount of the inorganic salt blending agent is as follows:
adding amount of the inorganic salt blending agent = (2-16) = (original COD of waste liquid) -original TDS of waste liquid;
the formula for calculating the adding amount of the oxidation blending agent is as follows:
adding amount of the oxidation blending agent = (0.3-5) × original COD of the waste liquid;
wherein the dosage unit of the inorganic salt blending agent and the dosage unit of the oxidation blending agent is mg/L.
The blending agent is reasonably selected according to the components and the pH value of the waste liquid 10, the pH value of the waste liquid 10 is adjusted, and the melting temperature of the produced solid material 11 is improved, wherein the hydrogen peroxide is 27.5% hydrogen peroxide, and the sodium hypochlorite is a solution with the effective content of 13%.
After the inorganic salt blending agent is put into the waste liquid 10, the inorganic salt blending agent can form solid substances after water in the waste liquid 10 is evaporated, and the solid substance can keep stable solid form unchanged at a high temperature of 100-150 ℃, further increasing the amount of solid substances at the high temperature of 100-150 ℃ of the substances remained after the water in the waste liquid 10 is evaporated, and the amount of thick liquid substances at the high temperature of 100-150 ℃ after the water in the waste liquid 10 is evaporated does not change, in this case, the ratio of the solid matter to the thick liquid matter at a high temperature of 100 to 150 ℃ after the water contained in the waste liquid 10 is evaporated is increased to a desired range, wherein, sodium hydroxide in inorganic salt is put into the waste liquid 10 and reacts with acid substances in the waste liquid 10 to generate salt, the salt can keep a solid state at a high temperature of 100-150 ℃ after water in the waste liquid 10 is evaporated, and simultaneously, the pH value of the waste liquid 10 is also adjusted.
After the oxidation blending agent is put into the waste liquid 10, the oxidation blending agent and organic matters which form thick liquid substances after water in the waste liquid 10 is evaporated are subjected to chemical reaction, so that the part of the organic matters in the waste liquid 10 are oxidized into carbon dioxide and water, the quantity of the thick liquid substances at the high temperature of 100-150 ℃ after the water is evaporated in the waste liquid 10 is further reduced, the quantity of the solid substances at the high temperature of 100-150 ℃ after the water is evaporated in the waste liquid 10 is unchanged, and in this case, the ratio of the solid substances to the thick liquid substances at the high temperature of 100-150 ℃ after the water is evaporated in the waste liquid 10 is increased to a required range.
A waste liquid treatment device used in a treatment process of high-salt high-organic matter waste liquid comprises a blending tank 303, a raw liquid pump 314, a waste liquid pump 8, a first heat exchanger 307, a dispensing tank 304, a dosing pump 313, a drying machine 7, a device drainage pipeline and a control system, wherein the waste liquid 10 is sent into the blending tank 303 through the raw liquid pump 314, the dosing pump 313 sends a blending agent liquid medicine blended in the dispensing tank 304 into the blending tank 303, the waste liquid pump 8 sends the waste liquid 10 blended in the blending tank 303 into the drying machine 7, the drying machine 7 can dry the waste liquid 10 into a solid material 11, a discharge hole 2 for discharging the solid material 11, a steam condensate discharge hole for discharging steam condensate 14 in a drying process and an exhaust hole for discharging secondary steam are formed in the drying machine 7, the steam condensate discharge hole of the drying machine 7 is communicated with a water inlet of the first heat exchanger 307, the first heat exchanger is positioned in the blending tank 303, the first heat exchanger 307 can heat the waste liquid 10 in the blending tank 303 to a specified temperature, a water outlet of the first heat exchanger 307 is communicated with a device water drainage pipeline and an inlet of the dispensing tank 304, a discharge valve 311 is arranged on the device water drainage pipeline, a water inlet valve 312 is arranged at the inlet of the dispensing tank 304, the control system controls the discharge valve 311 and the water inlet valve 312 to be in linkage with each other, the control system controls the raw liquid pump 314 and the dosing pump 313 to be started and stopped to be in linkage, and the control system also controls the drying machine 7 and the waste liquid pump 8 to operate.
The equipment carries out automatic treatment on the high-salt and high-organic matter waste liquid, and the specific treatment steps are as follows:
(1) steam 12 in the plant area is introduced into the drier 7, steam condensate 14 generated by drying treatment of the drier 7 is discharged from a steam condensate discharge port of the drier 7 and enters the first heat exchanger 307 in the blending tank 303, and the steam condensate 14 after heat exchange of the first heat exchanger 307 enters the blending tank 304 as required to form dispensing water or is directly discharged through a device drainage pipeline.
(2) Pumping the waste liquid 10 to a blending tank 303 by a raw liquid pump 314, preheating the waste liquid 10 in the blending tank 303 by a first heat exchanger 307, raising the temperature to 60-90 ℃, meanwhile, reasonably selecting components and dosage of a blending agent according to the components of the waste liquid 10, adding the blending agent to a dispensing tank 304, accurately blending the blending agent in the dispensing tank 304 to form a medicament, pumping the medicament into the blending tank 303 by a dosing pump 313 to mix with the waste liquid 10, and realizing accurate dosing of the medicament by the dosing pump 313 under the linkage control of the raw liquid pump 314, so that the pH of the blended waste liquid 10 is more than 5, and the melting temperature T of discharged materialsm＞100℃。
During dispensing, when the dispensing agent is a solid medicament, the steam condensate 14 discharged by the first heat exchanger 307 needs to be added into the dispensing tank 304, at this time, the discharge valve 311 on the equipment drainage pipeline is closed, the water inlet valve 312 at the inlet of the dispensing tank 304 is opened, the steam condensate 14 enters the dispensing tank 304, when the steam condensate 14 in the dispensing tank 304 reaches the required amount, the water inlet valve 312 is closed, and the steam condensate 14 can be discharged from the equipment drainage pipeline by opening the discharge valve 311.
When the blending agent is liquid hydrogen peroxide or sodium hypochlorite solution, the steam condensate 14 does not need to be added into the dispensing tank 304 for blending, and the blending agent can be directly used, at the moment, the water inlet valve 312 at the inlet of the dispensing tank 304 is kept closed, the discharge valve 311 on the equipment drainage pipeline is automatically opened under the linkage of the water inlet valve 312, and the steam condensate 14 is directly discharged from the equipment drainage pipeline.
(3) The discharge port of the allocation tank 303 is communicated with the inlet of the drying machine 7 through a pipeline, the allocated waste liquid 10 is sent into the drying machine 7 through the discharge port of the allocation tank 303 by a waste liquid pump 8, the drying machine 7 directly dries the waste liquid 10 into a solid material 11, and the discharge port of the allocation tank 303 is provided with a butt valve 315 which can be opened and closed and is used for opening and closing the discharge port of the allocation tank 303, and the opening and closing of the discharge port of the allocation tank 303 is controlled by a control system.
The structure makes full use of the steam condensate 14 of the drying machine 7, and the first heat exchanger 307 provides a heat source for the waste liquid 10 in the blending tank 303 and also provides a water source for blending for the blending tank 304, so that the energy and the water are saved, wherein the first heat exchanger 307 is not limited to stainless steel and fluoroplastic, and the shape is not limited to square and cylindrical.
Still be equipped with steel construction platform 301, heat preservation 302 and solid material collecting vat 9, allotment groove 303 and dispensing groove 304 are fixed respectively and are located on steel construction platform 301, and solid material collecting vat 9 is installed under discharge gate 2 of desiccator 7, and heat preservation 302 cladding is in allotment groove 303 and the dispensing groove 304 outside. The heat-insulating layers 302 are arranged around the blending tank 303 and the dispensing tank 304, so that the temperature of liquid in the blending tank 303 and the dispensing tank 304 is kept in a stable state, and the rapid blending is favorably realized.
Still be equipped with allotment agitator 305 and the agitator 306 that dispenses, allotment agitator 305 can stir the interior liquid of blending tank 303, and agitator 306 that dispenses can stir the interior liquid of 304 that dispenses, and control system control allotment agitator 305 and agitator 306 that dispenses start-stop to control allotment agitator 305 and the linkage of dosing pump 313. During dispensing, the blending agent and the steam condensate 14 are sent into the dispensing tank 304, the dispensing stirrer 306 is started, the blending agent is rapidly dissolved through stirring, after the preparation of the agent in the dispensing tank 304 is completed, the agent is quantitatively sent into the dispensing tank 303 through the dosing pump 313 according to the amount of the waste liquid 10 sent into the dispensing tank 303 by the raw liquid pump 314, and meanwhile, the dosing pump 313 is linked to start the blending stirrer 305 to stir the waste liquid 10 in the dispensing tank 303, so that the agent is fully and uniformly mixed in the waste liquid 10.
A pH meter 309 and a temperature sensor are arranged in the blending tank 303, the pH meter 309 can detect the pH value of liquid in the blending tank 303 and transmit the pH value to a control system, and the temperature sensor can detect the temperature of the liquid in the blending tank 303 and transmit the temperature to the control system. The pH value and the temperature value range of the waste liquid 10 in the blending tank 303 are ensured by the pH meter 309 and the temperature sensor, and the blended waste liquid 10 enters the drier 7 to produce the solid material 11 smoothly.
Still be equipped with dust removal defoaming all-in-one 4, the gas vent of desiccator 7 passes through the air inlet intercommunication of pipeline and dust removal defoaming all-in-one 4, and dust removal defoaming all-in-one 4 can remove dust and remove the foam purification treatment to the inside secondary steam of entering. Steam 12 in the plant area enters the drier 7 and then dries the waste liquid 10, secondary steam generated during drying enters the dust and foam removing all-in-one machine 4, and the dust and foam in the secondary steam are removed by the dust and foam removing all-in-one machine 4, so that the secondary steam is purified. Wherein the dust removal in the dust and foam removing integrated machine 4 is not limited to inertial dust removal, cyclone dust removal and cloth bag dust removal; the foam removal is not limited to baffle plate type and wire mesh type single forms or combined forms, the shape of the dust and foam removing integrated machine 4 is not limited to square and cylinder, and the structural form is not limited to vertical and horizontal.
Still be equipped with the secondary steam condensing system, the secondary steam condensing system includes second heat exchanger 5, draught fan 6 and tuber pipe, the gas vent of dust removal defoaming all-in-one 4 and the access connection of second heat exchanger 5 are equipped with comdenstion water discharge port on the second heat exchanger 5, comdenstion water discharge port and the effluent disposal system intercommunication of mill, the gas vent of second heat exchanger 5 passes through the air inlet intercommunication of the waste gas pretreatment systems of tuber pipe and mill, installs draught fan 6 in the tuber pipe. The secondary steam purified by the dust and foam removing integrated machine 4 enters the second heat exchanger 5 for heat exchange and is condensed into condensed water 13, and the condensed water 13 is discharged to a wastewater treatment system for treatment, so that the condensed water reaches the discharge standard. The air speed of the air pipe is adjusted to be 10-30 m/s through the draught fan 6 in the air pipe, the temperature of secondary steam entering the secondary steam condensing system is controlled to be 40-80 ℃, the pretreated tail gas 15 enters the waste gas treatment system to be treated and discharged after reaching the standard, and the second heat exchanger 5 is not limited to plate type and fin type.
A blending liquid level meter 308 and a dispensing liquid level meter 310 are further arranged, wherein the blending liquid level meter 308 can sense the liquid level height in the blending groove 303 and transmit the liquid level height to the control system, and the dispensing liquid level meter 310 can sense the liquid level height in the dispensing groove 304 and transmit the liquid level height to the control system. The liquid level in the blending tank 303 and the dispensing tank 304 is prevented from overflowing excessively, when the liquid level in the blending tank 303 and the dispensing tank 304 reaches the limit value, the control system controls the raw liquid pump 314 to stop supplying liquid and controls the water inlet valve 312 to be closed, and the discharge valve 311 is opened.
The drier 7 is any one of a disc drier, a spray drier, a film scraper drier, a roller scraper drier and a disc drier, and the drier 7 thoroughly avoids the scaling and blockage of a heat exchanger by a mode of non-direct contact heat exchange or a mode of stripping a material film by a scraper, and ensures high efficiency and stability of heat transfer efficiency.
The above treatment equipment comprises the following stages for preparing the waste liquid 10:
a preheating stage: the waste liquid 10 is pumped to the blending tank 303 through a raw liquid pump 314, the raw liquid pump 314 is controlled by a blending liquid level meter 308, a discharge valve 311 on a drainage pipeline of equipment is opened, a water inlet valve 312 at an inlet of the blending tank 304 is closed, and steam condensate 14 generated by the drier 7 preheats the waste liquid 10 to 60-90 ℃ through a first heat exchanger 307 arranged in the blending tank 303;
a dispensing stage: the blending agent is put into the blending tank 304, the program is started, a discharge valve 311 on a drainage pipeline of the equipment is closed, a water inlet valve 312 at the inlet of the blending tank 304 is opened, the steam condensate 14 discharged by the first heat exchanger 307 enters the blending tank 304, and meanwhile, the blending stirrer 306 is opened to stir and dissolve the blending agent; wherein the discharge valve 311 and the water inlet valve 312 are controlled by the dosage liquidometer 310, when the liquid level in the dosage tank 304 reaches the designated liquid level height, the water inlet valve 312 is closed, and the discharge valve 311 is opened;
a blending stage: the dosing pump 313 is started, the blended dosing agent is pumped into the dosing tank 303 from the dosing tank 304, the dosing stirrer 305 is started simultaneously, the dosing pump 313 is controlled by the raw liquid pump 314 in a linkage mode to achieve automatic and accurate dosing amount control, the dosing stirrer 305 is linked by the dosing pump 313, the dosing pump 313 is started simultaneously, the dosing stirrer 305 is started automatically, the pH of the waste liquid 10 is ensured to be larger than 5 through the pH meter 309 in the dosing process, and the blended waste liquid 10 enters the drying machine 7 through the butt valve 315.
Example 1:
the COD of the waste liquid 10 generated by the chemical nickel plating in a certain factory is 53900mg/L, and the solid content is 25.8%.
After the waste liquid 10 is preheated in the blending tank 303, the temperature of the waste liquid 10 is higher than 70 ℃, the blending agent in the blending tank 304 is a composition of sodium hydroxide, sodium sulfate and magnesium sulfate, wherein the mass ratio of the sodium hydroxide to the sodium sulfate to the magnesium sulfate is 2: 3: 5, fully stirring and mixing the blending agent and the steam condensate 14 to form a blending agent medicament, and calculating the adding amount of the blending agent medicament according to the following formula:
the addition of the blending agent =5.7 x the original COD of the waste liquid-the original TDS of the waste liquid;
adding the blending agent into the blending tank 303 according to the adding amount, adjusting the pH =6 of the waste liquid 10, and treating the blended waste liquid 10 by the drying integration equipment 1 to obtain a blocky solid material 11, wherein the water content of the solid material 11 is 8.1%, and the melting temperature Tm of the solid material 11 is more than 120 ℃. The wind speed in the wind pipe is adjusted to be 12 m/s, so that the secondary steam condensate 13 is colorless and transparent, and the COD is less than 800 mg/L.
Example 2:
the organic content of the waste liquid 10 generated by the zinc-nickel alloy in a certain plant is 113800mg/L, and the solid content is 20.7%.
After the waste liquid 10 is preheated in the blending tank 303, the temperature of the waste liquid 10 is higher than 80 ℃, the blending agent in the blending tank 304 is a mixture of sodium silicate and magnesium sulfate in a mass ratio of 1:1, the blending agent and the steam condensate 14 are fully stirred and mixed to form a blending agent medicament, and the dosage of the blending agent medicament is calculated according to the following formula:
the addition of the blending agent =2.3 x the original COD of the waste liquid-the original TDS of the waste liquid;
adding the blending agent into the blending tank 303 according to the adding amount, adjusting the pH =14 of the waste liquid 10, and treating the blended waste liquid 10 by the drying integration equipment 1 to obtain a strip-shaped solid material 11, wherein the water content of the solid material 11 is 7.5%, and the melting temperature Tm of the solid material 11 is more than 130 ℃. The wind speed in the air pipe is adjusted to be 15 m/s, so that the secondary steam condensate 13 is colorless and transparent, and the COD is less than 1000 mg/L.
Example 3:
COD in a waste liquid 10 generated by the nanofiltration of organic phosphorus waste water of a certain plant is 6320mg/L, total phosphorus is 623mg/L, and the solid content is 7.2%.
After the waste liquid 10 is preheated in the blending tank 303, the temperature of the waste liquid 10 is higher than 80 ℃, the blending agent in the blending tank 304 is ferrous sulfate, the blending agent and the steam condensate 14 are fully stirred and mixed to form a blending agent, and the adding amount of the blending agent is calculated according to the following formula:
the addition amount of the blending agent =14 × raw COD of waste liquid-raw TDS of waste liquid;
adding the blending agent into the blending tank 303 according to the adding amount, adjusting the pH =8 of the waste liquid 10, and treating the blended waste liquid 10 by the drying integration equipment 1 to obtain a strip-shaped solid material 11, wherein the water content of the solid material 11 is 9.0%, and the melting temperature Tm of the solid material 11 is more than 130 ℃. The wind speed in the air duct is adjusted to be 13 m/s, so that the secondary steam condensate 13 is colorless and transparent, the COD is less than 90 mg/L, and the total phosphorus is less than 1 mg/L.
Example 4: the COD of the waste liquid 10 generated by the chemical nickel plating in a certain factory is 65800mg/L, and the solid content is 30.3%.
After the waste liquid 10 is preheated in the blending tank 303, the temperature of the waste liquid 10 is higher than 70 ℃, the blending agent in the blending tank 304 is 27.5% hydrogen peroxide, and the dosage of the blending agent is calculated according to the following formula:
the addition of the blending agent =1 × original COD of the waste liquid;
adding the blending agent into the blending tank 303 according to the adding amount, adjusting the pH =6 of the waste liquid 10, adjusting the TDS/COD =5.3 in the oxidized waste liquid 10, and treating the blended waste liquid 10 by the drying integration equipment 1 to obtain the blocky solid material 11, wherein the water content of the solid material 11 is 9.1%, and the melting temperature Tm of the solid material 11 is more than 120 ℃. The wind speed in the wind pipe is adjusted to be 13 m/s, so that the secondary steam condensate 13 is colorless and transparent, and the COD is less than 1000 mg/L.
Comparative example:
the COD of the waste liquid 10 produced by the electroless nickel plating in a certain factory is 53900mg/L, and the solid content is 25.8% (same as example 1).
And (3) adjusting the pH of the waste liquid 10 to be =6 in a pH adjusting tank, then feeding the waste liquid 10 into a three-effect evaporator, and evaporating and concentrating to obtain a pasty viscous concentrated solution with the water content of 60%.
Claims (10)
1. A treatment process of high-salt high-organic matter waste liquid is characterized by comprising the following steps: the method comprises the following specific steps:
the method comprises the following steps: raising the temperature of the waste liquid to 60-90 ℃;
step two: adding inorganic salt blending agent capable of increasing TDS or oxidation blending agent capable of reducing COD into the waste liquid to make the pH of the waste liquid be greater than 5, and simultaneously making TDS and COD in the waste liquid meet the following formula:
TDS/COD=2～16；
step three: sending the mixed waste liquid into a drier, and directly drying the mixed waste liquid into the waste liquid with the water content of less than 10% and the melting temperature T by the driermSolid material at temperature higher than 100 deg.c.
2. The process for treating high-salt high-organic matter waste liquid according to claim 1, characterized in that: the inorganic salt blending agent is one or a composition of more of ferrous sulfate, sodium sulfate, magnesium sulfate, sodium hydroxide and sodium silicate, and the oxidation blending agent is hydrogen peroxide, sodium hypochlorite or calcium hypochlorite;
the formula for calculating the adding amount of the inorganic salt blending agent is as follows:
adding amount of the inorganic salt blending agent = (2-16) = (original COD of waste liquid) -original TDS of waste liquid;
the formula for calculating the adding amount of the oxidation blending agent is as follows:
adding amount of the oxidation blending agent = (0.3-5) × original COD of the waste liquid;
wherein the unit of the adding amount of the inorganic salt blending agent and the adding amount of the oxidation blending agent is mg/L.
3. A waste liquid treatment apparatus used in the treatment process of a high-salt high-organic matter waste liquid according to claim 1, characterized in that: the drying machine comprises a blending tank, a raw liquid pump, a waste liquid pump, a first heat exchanger, a dispensing tank, a dosing pump, a drying machine, an equipment drainage pipe and a control system, wherein waste liquid is sent into the blending tank through the raw liquid pump, the dosing pump sends blended liquid medicine in the blending tank into the blending tank, the waste liquid pump sends the blended waste liquid in the blending tank into the drying machine, the drying machine can dry the waste liquid into solid materials, a discharge hole for discharging the solid materials, a steam condensate discharge hole for discharging steam condensate in the drying process and an exhaust hole for discharging secondary steam are formed in the drying machine, the steam condensate discharge hole of the drying machine is communicated with a water inlet of the first heat exchanger, the first heat exchanger is positioned in the blending tank and can heat the waste liquid in the blending tank to a specified temperature, a water outlet of the first heat exchanger is communicated with the equipment drainage pipe and an inlet of the dispensing tank, and a discharge valve is arranged on the equipment drainage pipe, the inlet of the dispensing groove is provided with a water inlet valve, the control system controls the linkage switch of the discharge valve and the water inlet valve, the control system controls the starting and stopping linkage of the raw liquid pump and the dosing pump, and the control system also controls the running of the drying machine and the waste liquid pump.
4. The liquid waste treatment apparatus according to claim 3, characterized in that: still be equipped with steel construction platform, heat preservation and solid material collecting vat, the surge tank is fixed respectively with the tank of dispensing on locating the steel construction platform, and the solid material collecting vat is installed under the desiccator discharge gate, and the heat preservation cladding is in the surge tank and the tank outside of dispensing.
5. The liquid waste treatment apparatus according to claim 3, characterized in that: still be equipped with the allotment agitator and the agitator that dispenses, the allotment agitator can stir the blending tank interior liquid, and the agitator that dispenses can stir the blending tank interior liquid, and control system control allotment agitator and the agitator that dispenses open and stop to control allotment agitator and dosing pump linkage.
6. The liquid waste treatment apparatus according to claim 3, characterized in that: a pH meter and a temperature sensor are arranged in the blending tank, the pH meter can detect the pH value of liquid in the blending tank and transmit the pH value to the control system, and the temperature sensor can detect the temperature of the liquid in the blending tank and transmit the temperature to the control system.
7. The liquid waste treatment apparatus according to claim 3, characterized in that: still be equipped with dust removal defoaming all-in-one, the gas vent of desiccator passes through the air inlet intercommunication of pipeline and dust removal defoaming all-in-one, and dust removal defoaming all-in-one can remove dust and remove the foam purification treatment and discharge through its gas vent to the inside secondary steam of getting into.
8. The liquid waste treatment apparatus according to claim 7, characterized in that: still be equipped with the secondary steam condensing system, the secondary steam condensing system includes second heat exchanger, draught fan and tuber pipe, and the gas vent of dust removal defoaming all-in-one is connected with the air inlet of second heat exchanger, is equipped with the comdenstion water discharge port on the second heat exchanger, and the comdenstion water discharge port communicates with the effluent disposal system of mill, and the gas vent of second heat exchanger passes through the air inlet intercommunication of the waste gas pretreatment system of tuber pipe and mill, and installs the draught fan in the tuber pipe.
9. The liquid waste treatment apparatus according to claim 3, characterized in that: the liquid level meter is also provided with a blending liquid level meter and a dispensing liquid level meter, wherein the blending liquid level meter can sense the liquid level height in the blending tank and transmit the liquid level height to the control system, and the dispensing liquid level meter can sense the liquid level height in the dispensing tank and transmit the liquid level height to the control system.
10. The liquid waste treatment apparatus according to claim 3, characterized in that: the drier is any one of a disc drier, a spray drier, a film scraper drier, a roller scraper drier and a disc drier.
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| CN103274380A (en) * | 2013-05-08 | 2013-09-04 | 山东潍坊润丰化工有限公司 | Glyphosate mother liquid treatment method and device |
| JP2015128754A (en) * | 2014-01-08 | 2015-07-16 | 三菱重工業株式会社 | Water treatment system and method |
| CN107162298A (en) * | 2017-04-20 | 2017-09-15 | 中交天航环保工程有限公司 | A kind of near-zero release processing method of high salt organic waste water |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103274380A (en) * | 2013-05-08 | 2013-09-04 | 山东潍坊润丰化工有限公司 | Glyphosate mother liquid treatment method and device |
| JP2015128754A (en) * | 2014-01-08 | 2015-07-16 | 三菱重工業株式会社 | Water treatment system and method |
| CN107162298A (en) * | 2017-04-20 | 2017-09-15 | 中交天航环保工程有限公司 | A kind of near-zero release processing method of high salt organic waste water |
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