CN110540341A - waste cutting emulsion wastewater treatment system and method - Google Patents
waste cutting emulsion wastewater treatment system and method Download PDFInfo
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- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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Abstract
the invention provides a system and a method for treating cutting emulsion wastewater, wherein the system comprises an adjusting tank, an oil separation tank, a dosing tank, an air flotation unit, a middle tank, a cartridge filter, a catalytic oxidation unit, a middle water tank, a heat exchanger, a UASB reactor, a contact oxidation device, an MBR unit, a clean water tank, a circulating pump and an incineration system; the selected active carbon supported transition metal catalyst has the advantages of high and stable treatment effect, short reaction time, low chemical sludge yield, no hardening of the filler, low backwashing frequency and low filler loss. The catalytic oxidation carries out ring opening and chain breaking on toxic and harmful substances in raw water, improves the biochemical property of the wastewater, provides conditions for the application of a biochemical system, removes organic pollutants, and reduces the sludge production of the biochemical system and the investment and operation cost of a subsequent biochemical system. The system and the method have the advantages of strong impact load resistance, high and stable treatment efficiency, low operation cost, no toxicity or harm and no odor emission, and can be widely applied to treatment of low-biochemical-property and high-concentration organic wastewater.
Description
Technical Field
the invention particularly relates to a waste cutting emulsion wastewater treatment system and a method.
background
The cutting fluid is an industrial fluid used for cooling and lubricating cutters and workpieces in the processes of cutting, cutting and grinding metal, is prepared by scientifically compounding various super-strong functional additives, and has the advantages of good cooling performance, lubricating performance, antirust performance, oil removal and cleaning functions, anticorrosion function and the like. The cutting fluid is generally used for ensuring the quality of the processing technology and prolonging the service life of mechanical equipment and cutters. However, the cutting fluid is gradually deteriorated by frictional heat, metal dust and environmental media during recycling, and the performance thereof is lowered, so that the cutting fluid needs to be periodically replaced to form a waste cutting emulsion.
The waste cutting emulsion usually contains mineral oil, animal and vegetable oil, a surfactant, an antirust agent, a mildew-proof bactericide, suspended matters and the like, COD (chemical oxygen demand) is as high as 104-105 mg/L, biodegradability is poor, and the waste cutting emulsion is one of the most difficult-to-treat industrial waste liquids in the current machining industry. On one hand, oil substances and surfactants in the waste cutting emulsion can form a layer of film on the surface of the water body, so that the water body cannot reoxygenate, and a large amount of water body organisms die. On the other hand, other refractory organic matters added into the cutting fluid have high toxicity, can cause pathological changes of tissues and organs of a human body, and seriously harm the health of the human body.
at present, aiming at the treatment of high-concentration organic wastewater, the commonly used treatment process is a UASB reactor and aerobic combined process and an iron-carbon internal electrolysis and biochemical treatment process. The process of the UASB reactor and the aerobic combined process has the following defects: (1) the anaerobic reactor (UASB reactor) is obviously inhibited by the biological toxicity of toxic and harmful substances in the wastewater, is unstable in operation and easy to acidify, and has low pollutant removal efficiency; the aerobic system has too high load, and the discharged water quality does not reach the standard; (2) the aerobic biochemical system has high load, the daily biological sludge yield is high, and the sludge disposal cost is high; (3) the impact load of water quality and water quantity is large, and the running stability of the system is poor.
the existing treatment process for treating high-concentration refractory organic wastewater by adopting an iron-carbon internal electrolysis method has the following defects: 1) the biochemical property of the iron-carbon microelectrolysis refractory high-concentration toxic and harmful wastewater is improved very limitedly, so that a subsequent biochemical system cannot operate normally; 2) when the iron-carbon catalyst is operated under the condition of low pH value, the reaction time is long, the iron dissolution amount is large, a large amount of iron mud is generated, the iron-carbon filler is easy to block and harden, the backwashing frequency is high, and the filler replacement period is short.
therefore, the process which has high and stable catalytic oxidation effect and less mud production and can effectively improve the biochemical property of the wastewater is developed to be used as pretreatment, conditions are created for the stable operation of a biochemical system, and the development of an economic, reasonable and effective treatment process is necessary for the treatment of the waste cutting emulsion.
disclosure of Invention
The invention aims to provide a waste cutting emulsion wastewater treatment system and a method aiming at the defects of the prior art, and the system and the method can well solve the problems.
in order to meet the requirements, the technical scheme adopted by the invention is as follows: the waste cutting emulsion wastewater treatment system comprises an adjusting tank, an oil separation tank, a dosing tank, an air flotation unit, an intermediate tank, a cartridge filter, a catalytic oxidation unit, an intermediate water tank, a heat exchanger, a UASB reactor, a contact oxidation device, an MBR unit, a clean water tank, a circulating pump and an incineration system; the wastewater is sequentially connected with the regulating tank, the oil separation tank, the dosing tank, the air flotation unit, the intermediate tank, the cartridge filter, the catalytic oxidation unit, the intermediate tank, the heat exchanger, the UASB reactor, the contact oxidation device, the MBR unit and the clean water tank through a water inlet pipe, and the air flotation unit is also connected with the intermediate tank; the UASB reactor is connected with the circulating pump, and the heat exchanger is connected with the intermediate pool, the UASB reactor and the incineration system; the chemical adding pool is provided with a chemical adding port for polyaluminium chloride and a demulsifier, the intermediate pool is provided with a hydrochloric acid adding port, the catalytic oxidation unit is provided with an adding port for adding an oxidant, and the intermediate pool is provided with a sodium bicarbonate adding port; the tops of the UASB reactor, the contact oxidation device and the MBR unit are provided with exhaust ports which are connected with an incineration system through gas pipelines; and the biogas generated by the UASB reactor is connected with an incineration system after being pretreated.
the waste cutting emulsion wastewater treatment method comprises the following steps:
1) the wastewater enters an adjusting tank for homogenizing and equalizing, then enters an oil separation tank for primarily removing mineral oil and animal and vegetable oil suspended in the wastewater, and scum generated by the oil separation tank and residual activated sludge generated by a biochemical system enter a sludge treatment system together to realize harmless treatment; the effluent of the oil separation tank enters a dosing tank, and polyaluminium chloride and a demulsifier are added into the dosing tank and then enter an air floating unit to remove oil substances and suspended matters in the wastewater; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank is an inorganic demulsifier, the concentration of the demulsifier is 2-6 wt%, and the dosage of the demulsifier is 0.5-20 ppm;
2) the effluent of the air floatation unit enters an intermediate tank, and suspended matters in the wastewater in the intermediate tank are controlled to be reduced to below 50mg/L, so that the physical blockage of a catalyst in a catalytic oxidation unit and the anaerobic sludge loss of a UASB (upflow anaerobic sludge blanket) reactor caused by overhigh concentration of the suspended matters are avoided;
3) the effluent of the air floatation unit enters an intermediate tank, a hydrochloric acid adding port is formed in the intermediate tank, and the pH value in the intermediate tank is controlled to be 3-6; the effluent of the intermediate water tank enters a cartridge filter to further control SS in the wastewater, and the effluent of the cartridge filter enters a catalytic oxidation unit; an overrunning pipe is arranged between the air flotation unit and the middle water tank so as to meet the requirement of the UASB reactor on a carbon source, and simultaneously, the water inlet and the load of the catalytic oxidation unit are reduced on the premise of ensuring that the effluent of the system reaches the standard, so that the running cost of the whole system is reduced, and the optimization of the system operation is realized;
4) The catalytic oxidation unit has the reaction conditions of pH of 3-6, hydrogen peroxide addition of 0.6-1.2 times of COD removal amount and reaction time of 30-60 min at normal temperature and normal pressure; the filler in the catalytic oxidation unit is activated carbon loaded transition metal, noble metal and the like, the solid-phase catalyst is prepared by high-temperature sintering, the oxidant is hydrogen peroxide, and the oxidation pretreatment of the wastewater is realized under the normal temperature condition through the adsorption of the solid-phase catalyst, the catalysis of active groups and the oxidation of the oxidant; macromolecular organic matters which are difficult to degrade and have biotoxicity, such as mineral oil, a surfactant, a mildew-proof bactericide and the like in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the subsequent operation of a biochemical system;
5) the effluent of the catalytic oxidation unit enters an intermediate water tank through a heat exchanger, and the temperature in the intermediate water tank is ensured to be 33-36 ℃ in winter in the north;
6) Adding sodium bicarbonate into the intermediate water tank, controlling the pH value in the intermediate water tank to be 7.2-7.4, improving the buffering capacity of the wastewater on the pH change, and adjusting according to the actual operation condition of the UASB reactor; the effluent of the intermediate water tank enters a UASB reactor to further remove organic pollutants in the wastewater;
7) The UASB reactor is connected with a circulating pump, the effluent of the UASB reactor enters the UASB reactor after entering a water inlet pipeline of the UASB reactor so as to improve the impact resistance of the UASB reactor to the change of the inlet water load, and the hydraulic load of the UASB reactor is adjusted at the same time, thereby ensuring the high-efficiency and stable operation of the UASB reactor;
8) the effluent of the UASB reactor is subjected to advanced treatment by a contact oxidation device and an MBR unit to meet the requirements of wastewater discharge or reuse, and the treated wastewater is finally reused or discharged after reaching the standard in a clear water tank;
9) biogas generated by the UASB reactor is used as fuel to cooperate with a contact oxidation device and biological odor generated by the MBR unit to enter an incineration system for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
10) High-temperature flue gas generated by the incineration system is connected with a heat exchanger through a pipeline, waste water entering an intermediate water tank and a USAB reactor is heated through the heat exchanger, the UASB reactor is guaranteed to operate efficiently in the most suitable temperature range, and low-temperature flue gas after heat exchange of the heat exchanger is directly or reprocessed to reach the emission standard; and the surplus heat generated by the incineration system is used for waste heat utilization.
the system and the method have the following advantages:
1) The air flotation unit reduces suspended matters in the wastewater to below 50mg/L, and avoids the phenomena of filler blockage and sludge leakage of an anaerobic system caused by overhigh concentration of the suspended matters.
2) The catalytic oxidation unit partially oxidizes organic pollutants in raw water, and opens and breaks chains of macromolecular organic matters which are difficult to degrade and have biotoxicity, such as mineral oil, a surfactant, a mildew-proof bactericide and the like contained in the wastewater, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the operation of a subsequent biochemical system.
3) the selected activated carbon loaded transition metal catalyst has high and stable treatment effect, the reaction time is only 30-60 min, the chemical sludge yield is low, the hardening phenomenon of the filler does not exist, the filler loss is low, and the effect of removing organic pollutants is stable and high-efficient.
4) The catalytic oxidation unit controls the oxidation of organic pollutants in raw water through the adding amount of the oxidant, controls the water inlet organic load of the biochemical system, and has the advantages of small floor area of the biochemical system, small sludge production, low sludge treatment cost and low operation cost of the aeration system.
5) the alkali liquor added into the middle water tank is sodium bicarbonate, the pH of the wastewater is adjusted to 7.2-7.4, the buffering capacity of the wastewater on pH change is improved, and efficient and stable operation of the UASB reactor is ensured.
6) the combined process is characterized in that no odor is generated in the operation process: biological odor generated by a biochemical system is used as an air source for burning of the burning system, and is combusted in cooperation with biogas generated by the UASB reactor for harmless disposal; the heat generated by the incineration system provides a heat source for the UASB reactor and the low-temperature environment, and ensures the high-efficiency and stable operation of the UASB reactor.
7) The combined process has the advantages of strong water quality adaptability, strong controllability, strong impact load resistance, flexible operation mode, high efficiency, stability and wide application range.
Drawings
the accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
Fig. 1 schematically shows a structural view of a waste cutting emulsion wastewater treatment system according to one embodiment of the present application.
wherein: 1. a regulating tank; 2. an oil separation tank; 3. a medicine adding pool; 4. an air flotation unit; 5. an intermediate tank; 6. a cartridge filter; 7. a catalytic oxidation unit; 8. a middle water tank; 9. a heat exchanger; 10. a UASB reactor; 11. a contact oxidation unit; 12. an MBR unit; 13. a clean water tank; 14. a circulation pump; 15. an incineration system.
Detailed Description
in order to make the objects, technical solutions and advantages of the present application more apparent, the present application will be described in further detail with reference to the accompanying drawings and specific embodiments.
in the following description, references to "one embodiment," "an embodiment," "one example," "an example," etc., indicate that the embodiment or example so described may include a particular feature, structure, characteristic, property, element, or limitation, but every embodiment or example does not necessarily include the particular feature, structure, characteristic, property, element, or limitation. Moreover, repeated use of the phrase "in accordance with an embodiment of the present application" although it may possibly refer to the same embodiment, does not necessarily refer to the same embodiment.
certain features that are well known to those skilled in the art have been omitted from the following description for the sake of simplicity.
according to an embodiment of the present application, there is provided a waste cutting emulsion wastewater treatment system, as shown in fig. 1, including a conditioning tank 1; an oil separation tank 2; a dosing tank 3; an air flotation unit 4; an intermediate tank 5; a cartridge filter 6; a catalytic oxidation unit 7; a middle water tank 8; a heat exchanger 9; a UASB reactor 10; a contact oxidation unit 11; an MBR unit 12; a clean water tank 13; a circulation pump 14; an incineration system 15; the wastewater is sequentially connected with an adjusting tank 1, an oil separation tank 2, a dosing tank 3, an air flotation unit 4, an intermediate tank 5, a cartridge filter 6, a catalytic oxidation unit 7, an intermediate water tank 8, a heat exchanger 9, a UASB reactor 10, a contact oxidation device 11, an MBR unit 12 and a clean water tank 13 through a water inlet pipe, and the air flotation unit 4 is also connected with the intermediate water tank 8; the UASB reactor 10 is connected with a circulating pump 14; the heat exchanger 9 is connected with the intermediate water tank 8, the UASB reactor 10 and the incineration system 15; the dosing tank 3 is provided with a PAC (polyaluminium chloride) and demulsifier dosing port, the intermediate tank 5 is provided with a hydrochloric acid dosing port, the catalytic oxidation unit 7 is provided with an oxidant dosing port, and the intermediate tank 8 is provided with a sodium bicarbonate dosing port; the tops of the UASB reactor 10, the contact oxidation device 11 and the MBR unit 12 are provided with exhaust ports which are connected with an incineration system 15 through gas pipelines; the biogas generated by the UASB reactor 10 is pretreated and then connected with an incineration system 15.
according to one embodiment of the application, wastewater of the waste cutting emulsion wastewater treatment system enters an adjusting tank for homogenizing and equalizing, then enters an oil separation tank for removing suspended matters in the wastewater, effluent of the oil separation tank enters a dosing tank for adding PAC (polyaluminium chloride) and a demulsifier, then enters an air floatation unit for removing emulsified oil and suspended matters existing in the wastewater, effluent of the air floatation unit enters an intermediate tank, the intermediate tank is provided with a hydrochloric acid adding port, and the pH value in the intermediate tank is controlled to be 3-6; the effluent of the intermediate water tank enters a cartridge filter to further control SS in the wastewater, and the effluent of the cartridge filter enters a catalytic oxidation unit; the air floatation unit is also connected with the middle water pool; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank is an inorganic demulsifier, the concentration of the demulsifier is 2-6 wt%, and the dosage of the demulsifier is 0.5-20 ppm; and suspended matters in the wastewater in the intermediate tank are controlled to be reduced to below 50mg/L, so that the physical blockage of a catalyst in a catalytic oxidation unit and the anaerobic sludge loss of a UASB reactor caused by overhigh concentration of the suspended matters are avoided.
According to one embodiment of the application, the filler in the catalytic oxidation unit of the waste cutting emulsion wastewater treatment system is a solid-phase catalyst prepared by high-temperature sintering of activated carbon-supported transition metal, precious metal and the like, and the oxidant is hydrogen peroxide, so that the wastewater is subjected to oxidation pretreatment under the normal temperature condition through adsorption of the solid-phase catalyst, catalysis of active groups and oxidation of the oxidant; when COD is removed, macromolecular organic matters such as mineral oil, animal and vegetable oil, a surfactant, an antirust agent, a mildew-proof bactericide and the like contained in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the operation of a subsequent biochemical system; 5) the catalytic oxidation unit has the reaction conditions of pH of 3-6, hydrogen peroxide addition of 0.6-1.2 times of COD removal amount and reaction time of 30-60 min at normal temperature and normal pressure.
according to one embodiment of the application, the effluent of a catalytic oxidation unit of the waste cutting emulsion wastewater treatment system sequentially enters a heat exchanger and a UASB reactor through an intermediate water tank, and the temperature in the UASB reactor is ensured to be 33-36 ℃ in winter in the north; 1) the volume load of the UASB reactor (10) is 2-6 kg/(m 3. d), and the sludge load of the contact oxidation device is 0.075-0.12 kg/(Mlvss. d); the air flotation unit and the middle water tank are directly provided with the overrun pipe, and when the concentration of organic matters in the effluent of the air flotation unit is low, the requirement of the UASB reactor on the carbon source during normal operation is met; adding sodium bicarbonate into the intermediate water tank, controlling the pH value in the intermediate water tank to be 7.2-7.4, and adjusting according to the actual operation condition of the UASB reactor; the effluent of the intermediate water tank enters a UASB reactor to further remove organic pollutants in the wastewater; the water suction port of the circulating pump is positioned at the lower part of the three-phase separator of the UASB reactor, and the water outlet is positioned on the water inlet pipeline of the UASB reactor and enters the UASB reactor along with the wastewater from the intermediate water tank; the effluent of the UASB reactor is subjected to advanced treatment by a contact oxidation device and an MBR unit to meet the requirements of wastewater discharge or recycling, and the treated wastewater is finally recycled or discharged up to the standard in a clear water tank.
According to one embodiment of the application, biogas generated by a UASB reactor of the waste cutting emulsion wastewater treatment system is used as fuel to cooperate with a contact oxidation device and biological odor generated by an MBR unit to enter an incineration system for combustion as combustion air through a gas pipeline, so that the biological odor is subjected to harmless treatment; high-temperature flue gas generated by the incineration system is connected with a heat exchanger through a pipeline, waste water entering a USAB reactor is heated through the heat exchanger, the UASB reactor is guaranteed to be suitable for the most suitable temperature range to operate efficiently, and low-temperature flue gas after heat exchange of the heat exchanger is directly (or reprocessed) and is discharged up to the standard; and the surplus heat generated by the incineration system is used for waste heat utilization.
According to one embodiment of the present application, the present invention provides a waste cutting emulsion wastewater treatment system and method, comprising the steps of:
1) the wastewater enters an adjusting tank for homogenizing and equalizing, then enters an oil separation tank for primarily removing mineral oil and animal and vegetable oil suspended in the wastewater, and scum generated by the oil separation tank and residual activated sludge generated by a biochemical system enter a sludge treatment system together to realize harmless treatment; the effluent of the oil separation tank enters a dosing tank, PAC (polyaluminium chloride) and a demulsifier are added into the dosing tank, and then the effluent enters an air floatation unit to remove oil substances and suspended matters in the wastewater; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank is an inorganic demulsifier, the concentration of the demulsifier is 2-6 wt%, and the dosage of the demulsifier is 0.5-20 ppm;
2) the effluent of the air floatation unit enters an intermediate tank, and suspended matters in the wastewater in the intermediate tank are controlled to be reduced to below 50mg/L, so that the physical blockage of a catalyst in a catalytic oxidation unit and the anaerobic sludge loss of a UASB (upflow anaerobic sludge blanket) reactor caused by overhigh concentration of the suspended matters are avoided;
3) the effluent of the air floatation unit enters an intermediate tank, a hydrochloric acid adding port is formed in the intermediate tank, and the pH value in the intermediate tank is controlled to be 3-6; the effluent of the intermediate water tank enters a cartridge filter to further control SS in the wastewater, and the effluent of the cartridge filter enters a catalytic oxidation unit; an overrunning pipe is arranged between the air flotation unit and the middle water tank so as to meet the requirement of the UASB reactor on a carbon source, and simultaneously, the water inlet and the load of the catalytic oxidation unit are reduced on the premise of ensuring that the effluent of the system reaches the standard, so that the running cost of the whole system is reduced, and the optimization of the system operation is realized;
4) the catalytic oxidation unit has the reaction conditions of pH of 3-6, hydrogen peroxide addition of 0.6-1.2 times of COD removal amount and reaction time of 30-60 min at normal temperature and normal pressure; the filler in the catalytic oxidation unit is activated carbon loaded transition metal, noble metal and the like, the solid-phase catalyst is prepared by high-temperature sintering, the oxidant is hydrogen peroxide, and the oxidation pretreatment of the wastewater is realized under the normal temperature condition through the adsorption of the solid-phase catalyst, the catalysis of active groups and the oxidation of the oxidant; macromolecular organic matters which are difficult to degrade and have biotoxicity, such as mineral oil, a surfactant, a mildew-proof bactericide and the like in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the subsequent operation of a biochemical system;
5) the effluent of the catalytic oxidation unit enters an intermediate water tank through a heat exchanger, and the temperature in the intermediate water tank is ensured to be 33-36 ℃ in winter in the north;
6) adding sodium bicarbonate into the intermediate water tank, controlling the pH value in the intermediate water tank to be 7.2-7.4, improving the buffering capacity of the wastewater on the pH change, and adjusting according to the actual operation condition of the UASB reactor; the effluent of the intermediate water tank enters a UASB reactor to further remove organic pollutants in the wastewater;
7) The UASB reactor is connected with a circulating pump, the effluent of the UASB reactor enters the UASB reactor after entering a water inlet pipeline of the UASB reactor so as to improve the impact resistance of the UASB reactor to the change of the inlet water load, and the hydraulic load of the UASB reactor is adjusted at the same time, thereby ensuring the high-efficiency and stable operation of the UASB reactor;
8) the effluent of the UASB reactor is subjected to advanced treatment by a contact oxidation device and an MBR unit to meet the requirements of wastewater discharge or reuse, and the treated wastewater is finally reused or discharged after reaching the standard in a clear water tank;
9) Biogas generated by the UASB reactor is used as fuel to cooperate with a contact oxidation device and biological odor generated by the MBR unit to enter an incineration system for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
10) high-temperature flue gas generated by the incineration system is connected with a heat exchanger through a pipeline, waste water entering an intermediate water tank and a USAB reactor is heated through the heat exchanger, the UASB reactor is guaranteed to operate efficiently in the most suitable temperature range, and low-temperature flue gas after heat exchange of the heat exchanger is directly (or reprocessed) and discharged up to the standard; and the surplus heat generated by the incineration system is used for waste heat utilization.
Example 1:
1) The wastewater enters an adjusting tank for homogenizing and equalizing, then enters an oil separation tank for primarily removing mineral oil and animal and vegetable oil suspended in the wastewater, and scum generated by the oil separation tank and residual activated sludge generated by a biochemical system enter a sludge treatment system together to realize harmless treatment; the effluent of the oil separation tank enters a dosing tank, PAC (polyaluminium chloride) and a demulsifier are added into the dosing tank, and then the effluent enters an air floatation unit to remove oil substances and suspended matters in the wastewater; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank is an inorganic demulsifier, the concentration of the demulsifier is 2-6 wt%, and the dosage of the demulsifier is 0.5-20 ppm;
2) the effluent of the air floatation unit enters an intermediate tank, and suspended matters in the wastewater in the intermediate tank are controlled to be reduced to below 50mg/L, so that the physical blockage of a catalyst in a catalytic oxidation unit and the anaerobic sludge loss of a UASB (upflow anaerobic sludge blanket) reactor caused by overhigh concentration of the suspended matters are avoided;
3) the effluent of the air flotation unit enters an intermediate tank, a hydrochloric acid adding port is arranged in the intermediate tank, and the pH value in the intermediate tank is controlled to be 3; the effluent of the intermediate water tank enters a cartridge filter to further control SS in the wastewater, and the effluent of the cartridge filter enters a catalytic oxidation unit; an overrunning pipe is arranged between the air flotation unit and the middle water tank so as to meet the requirement of the UASB reactor on a carbon source, and simultaneously, the water inlet and the load of the catalytic oxidation unit are reduced on the premise of ensuring that the effluent of the system reaches the standard, so that the running cost of the whole system is reduced, and the optimization of the system operation is realized;
4) the catalytic oxidation unit has the reaction conditions of pH 3, hydrogen peroxide addition amount 1.0 time of COD removal amount and reaction time controlled to be 60min at normal temperature and normal pressure; the oxidation pretreatment of the wastewater is realized under the condition of normal temperature; macromolecular organic matters which are difficult to degrade and have biotoxicity, such as mineral oil, a surfactant, a mildew-proof bactericide and the like in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the subsequent operation of a biochemical system;
5) Adding sodium bicarbonate into the intermediate water tank, controlling the pH value in the intermediate water tank to be 7.2-7.4, improving the buffering capacity of the wastewater on the pH change, and adjusting according to the actual operation condition of the UASB reactor; the effluent of the catalytic oxidation unit sequentially enters a heat exchanger and a UASB reactor through an intermediate water tank, and the temperature in the UASB reactor is ensured to be 33-36 ℃ in winter in the north; the volume load of the UASB reactor (10) is 4 kg/(m 3. d), and the sludge load of the contact oxidation device is 0.075-0.12 kg/(Mlvss. d);
6) the UASB reactor is connected with a circulating pump, the effluent of the UASB reactor enters the UASB reactor after entering a water inlet pipeline of the UASB reactor so as to improve the impact resistance of the UASB reactor to the change of the inlet water load, and the hydraulic load of the UASB reactor is adjusted at the same time, thereby ensuring the high-efficiency and stable operation of the UASB reactor;
7) The effluent of the UASB reactor is subjected to advanced treatment by a contact oxidation device and an MBR unit to meet the requirements of wastewater discharge or reuse, and the treated wastewater is finally reused or discharged after reaching the standard in a clear water tank;
8) biogas generated by the UASB reactor is used as fuel to cooperate with a contact oxidation device and biological odor generated by the MBR unit to enter an incineration system for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
9) high-temperature flue gas generated by the incineration system is connected with a heat exchanger through a pipeline, waste water entering an intermediate water tank and a USAB reactor is heated through the heat exchanger, the UASB reactor is guaranteed to operate efficiently in the most suitable temperature range, and low-temperature flue gas after heat exchange of the heat exchanger is directly (or reprocessed) and discharged up to the standard; and the surplus heat generated by the incineration system is used for waste heat utilization.
example 2:
1) the wastewater enters an adjusting tank for homogenizing and equalizing, then enters an oil separation tank for primarily removing mineral oil and animal and vegetable oil suspended in the wastewater, and scum generated by the oil separation tank and residual activated sludge generated by a biochemical system enter a sludge treatment system together to realize harmless treatment; the effluent of the oil separation tank enters a dosing tank, PAC (polyaluminium chloride) and a demulsifier are added into the dosing tank, and then the effluent enters an air floatation unit to remove oil substances and suspended matters in the wastewater; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank is an inorganic demulsifier, the concentration of the demulsifier is 2-6 wt%, and the dosage of the demulsifier is 0.5-20 ppm;
2) The effluent of the air floatation unit enters an intermediate tank, and suspended matters in the wastewater in the intermediate tank are controlled to be reduced to below 50mg/L, so that the physical blockage of a catalyst in a catalytic oxidation unit and the anaerobic sludge loss of a UASB (upflow anaerobic sludge blanket) reactor caused by overhigh concentration of the suspended matters are avoided;
3) the effluent of the air flotation unit enters an intermediate tank, a hydrochloric acid adding port is arranged in the intermediate tank, and the pH value in the intermediate tank is controlled to be 3; the effluent of the intermediate water tank enters a cartridge filter to further control SS in the wastewater, and the effluent of the cartridge filter enters a catalytic oxidation unit; an overrunning pipe is arranged between the air flotation unit and the middle water tank so as to meet the requirement of the UASB reactor on a carbon source, and simultaneously, the water inlet and the load of the catalytic oxidation unit are reduced on the premise of ensuring that the effluent of the system reaches the standard, so that the running cost of the whole system is reduced, and the optimization of the system operation is realized;
4) The reaction condition of the catalytic oxidation unit under normal temperature and normal pressure is that the pH is 4, and the time when the adding amount of oxygen water is 0.8 of the COD removal amount is controlled to be 30 min; the oxidation pretreatment of the wastewater is realized under the condition of normal temperature; macromolecular organic matters which are difficult to degrade and have biotoxicity, such as mineral oil, a surfactant, a mildew-proof bactericide and the like in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the subsequent operation of a biochemical system;
5) adding sodium bicarbonate into the intermediate water tank, controlling the pH value in the intermediate water tank to be 7.2-7.4, improving the buffering capacity of the wastewater on the pH change, and adjusting according to the actual operation condition of the UASB reactor; the effluent of the catalytic oxidation unit sequentially enters a heat exchanger and a UASB reactor through an intermediate water tank, and the temperature in the UASB reactor is ensured to be 33-36 ℃ in winter in the north; the volume load of the UASB reactor is 2 kg/(m 3. d), and the sludge load of the contact oxidation device is 0.075-0.12 kg/(Mlvss. d);
6) the UASB reactor is connected with a circulating pump, the effluent of the UASB reactor enters the UASB reactor after entering a water inlet pipeline of the UASB reactor so as to improve the impact resistance of the UASB reactor to the change of the inlet water load, and the hydraulic load of the UASB reactor is adjusted at the same time, thereby ensuring the high-efficiency and stable operation of the UASB reactor;
7) the effluent of the UASB reactor is subjected to advanced treatment by a contact oxidation device and an MBR unit to meet the requirements of wastewater discharge or reuse, and the treated wastewater is finally reused or discharged after reaching the standard in a clear water tank;
8) biogas generated by the UASB reactor is used as fuel to cooperate with a contact oxidation device and biological odor generated by the MBR unit to enter an incineration system for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
9) high-temperature flue gas generated by the incineration system is connected with a heat exchanger through a pipeline, waste water entering an intermediate water tank and a USAB reactor is heated through the heat exchanger, the UASB reactor is guaranteed to operate efficiently in the most suitable temperature range, and low-temperature flue gas after heat exchange of the heat exchanger is directly (or reprocessed) and discharged up to the standard; the surplus heat generated by the incineration system is used for waste heat utilization;
example 3:
1) The wastewater enters an adjusting tank for homogenizing and equalizing, then enters an oil separation tank for primarily removing mineral oil and animal and vegetable oil suspended in the wastewater, and scum generated by the oil separation tank and residual activated sludge generated by a biochemical system enter a sludge treatment system together to realize harmless treatment; the effluent of the oil separation tank enters a dosing tank, PAC (polyaluminium chloride) and a demulsifier are added into the dosing tank, and then the effluent enters an air floatation unit to remove oil substances and suspended matters in the wastewater; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank is an inorganic demulsifier, the concentration of the demulsifier is 2-6 wt%, and the dosage of the demulsifier is 0.5-20 ppm;
2) the effluent of the air floatation unit enters an intermediate tank, and suspended matters in the wastewater in the intermediate tank are controlled to be reduced to below 50mg/L, so that anaerobic sludge loss of the UASB reactor caused by overhigh concentration of the suspended matters is avoided;
3) all the effluent of the air flotation unit enters an intermediate tank; sodium bicarbonate is added into the intermediate water tank, the pH value in the intermediate water tank is controlled to be 7.2-7.4, and the buffering capacity of the wastewater on pH change is improved;
4) The volume load of the UASB reactor is 2 kg/(m 3. d), and the sludge load of the contact oxidation device is 0.075-0.10 kg/(Mlvss. d);
5) the UASB reactor is connected with a circulating pump, the effluent of the UASB reactor enters the UASB reactor after entering a water inlet pipeline of the UASB reactor so as to improve the impact resistance of the UASB reactor to the change of the inlet water load, and the hydraulic load of the UASB reactor is adjusted at the same time, thereby ensuring the high-efficiency and stable operation of the UASB reactor;
6) The effluent of the UASB reactor is subjected to advanced treatment by a contact oxidation device and an MBR unit to meet the requirements of wastewater discharge or reuse, and the treated wastewater is finally reused or discharged after reaching the standard in a clear water tank;
7) Biogas generated by the UASB reactor is used as fuel to cooperate with a contact oxidation device and biological odor generated by the MBR unit to enter an incineration system for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
8) High-temperature flue gas generated by the incineration system is connected with a heat exchanger through a pipeline, waste water entering an intermediate water tank and a USAB reactor is heated through the heat exchanger, the UASB reactor is guaranteed to operate efficiently in the most suitable temperature range, and low-temperature flue gas after heat exchange of the heat exchanger is directly (or reprocessed) and discharged up to the standard; and the surplus heat generated by the incineration system is used for waste heat utilization.
the above-mentioned embodiments only show some embodiments of the present invention, and the description thereof is more specific and detailed, but should not be construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the claims.
Claims (7)
1. a cutting emulsion effluent disposal system which characterized in that: comprises an adjusting tank (1), an oil separation tank (2), a dosing tank (3), an air flotation unit (4), an intermediate tank (5), a cartridge filter (6), a catalytic oxidation unit (7), an intermediate water tank (8), a heat exchanger (9), a UASB reactor (10), a contact oxidation device (11), an MBR unit (12), a clean water tank (13), a circulating pump (14) and an incineration system (15);
the wastewater is sequentially connected with the adjusting tank (1), the oil separation tank (2), the dosing tank (3), the air flotation unit (4), the intermediate tank (5), the security filter (6), the catalytic oxidation unit (7), the intermediate water tank (8), the heat exchanger (9), the UASB reactor (10), the contact oxidation device (11), the MBR unit (12) and the clean water tank (13) through a water inlet pipe, and the air flotation unit (4) is also connected with the intermediate water tank (8); the UASB reactor (10) is connected with the circulating pump (14), and the heat exchanger (9) is connected with the intermediate water tank (8), the UASB reactor (10) and the incineration system (15);
the chemical adding tank (3) is provided with a chemical adding port for polyaluminium chloride and a demulsifier, the intermediate tank (5) is provided with a hydrochloric acid adding port, the catalytic oxidation unit (7) is provided with an adding port for an oxidant, and the intermediate tank (8) is provided with a sodium bicarbonate adding port;
the tops of the UASB reactor (10), the contact oxidation device (11) and the MBR unit (12) are provided with exhaust ports which are connected with an incineration system (15) through gas pipelines;
and the biogas generated by the UASB reactor (10) is pretreated and then is connected with an incineration system (15).
2. the cutting emulsion wastewater treatment system according to claim 1, wherein: the method comprises the following steps that the wastewater enters an adjusting tank (1) for homogenizing and equalizing, then enters an oil separation tank (2) for removing suspended matters in the wastewater, the effluent of the oil separation tank enters a dosing tank (3) for adding polyaluminium chloride and a demulsifier, then enters an air flotation unit (4) for removing emulsified oil and suspended matters existing in the wastewater, the effluent of the air flotation unit (4) enters an intermediate tank (5), the intermediate tank (5) is provided with a hydrochloric acid adding port, and the pH value in the intermediate tank (5) is controlled to be 3-6;
the effluent of the intermediate water tank (5) enters a cartridge filter (6) to further control SS in the wastewater, and the effluent of the cartridge filter (6) enters a catalytic oxidation unit (7);
The air floatation unit (4) is also connected with an intermediate water pool (8);
The filler in the catalytic oxidation unit (7) is a solid-phase catalyst prepared by activated carbon loaded transition metal, noble metal and the like through high-temperature sintering, the oxidant is hydrogen peroxide, and the oxidation pretreatment of the wastewater is realized under the normal temperature condition through the adsorption of the solid-phase catalyst, the catalysis of active groups and the oxidation of the oxidant; when COD is removed, macromolecular organic matters such as mineral oil, animal and vegetable oil, a surfactant, an antirust agent, a mildew-proof bactericide and the like contained in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the operation of a subsequent biochemical system;
the effluent of the catalytic oxidation unit (7) sequentially enters a heat exchanger (9) and a UASB reactor (10) through an intermediate water tank (8), and the temperature in the UASB reactor (10) is ensured to be 33-36 ℃ in winter in the north;
Sodium bicarbonate is added into the intermediate water tank (8), the pH value in the intermediate water tank (8) is controlled to be 7.2-7.4, and the adjustment is carried out according to the actual operation condition of the UASB reactor (9); the effluent of the intermediate water tank (8) enters a UASB reactor (10) to further remove organic pollutants in the wastewater;
the water suction port of the circulating pump (14) is positioned at the lower part of the three-phase separator of the UASB reactor (10), the water outlet is positioned on the water inlet pipeline of the UASB reactor (10), and the water enters the UASB reactor (10) along with the wastewater from the middle water tank (8);
the effluent of the UASB reactor (10) is subjected to advanced treatment through a contact oxidation device (11) and an MBR unit (12) to meet the requirements of wastewater discharge or recycling, and the treated wastewater is finally recycled or discharged after reaching the standard in a clean water tank (13);
Biogas generated by the UASB reactor (10) is used as fuel to cooperate with a contact oxidation device (11) and biological odor generated by the MBR unit (12) to enter an incineration system (15) for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
high-temperature flue gas generated by the incineration system (15) is connected with a heat exchanger (9) through a pipeline, wastewater entering a USAB reactor (10) is heated through the heat exchanger (9), the UASB reactor (10) is guaranteed to operate efficiently in the most suitable temperature range, and low-temperature flue gas after heat exchange of the heat exchanger (9) is directly (or reprocessed) and discharged up to the standard; and the surplus heat generated by the incineration system (15) is used for waste heat utilization.
3. The cutting emulsion wastewater treatment system according to claim 1, wherein: biogas generated by the UASB reactor (10) is used as fuel to cooperate with a contact oxidation device (11) and biological odor generated by the MBR unit (12) to enter an incineration system (15) for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
high-temperature flue gas generated by the incineration system (15) is connected with a heat exchanger (9) through a pipeline, and waste water entering a USAB reactor (10) is heated through the heat exchanger (9), so that the UASB reactor (10) is guaranteed to operate efficiently in the optimal temperature range;
The low-temperature flue gas after heat exchange of the heat exchanger (9) is directly (or reprocessed) discharged after reaching the standard; and the surplus heat generated by the incineration system (15) is used for waste heat utilization.
4. The cutting emulsion wastewater treatment system according to claim 1, wherein: the flocculating agent used in the dosing tank (2) is polyaluminium chloride, the concentration is 4-8 wt%, and the dosing amount is 10-200 ppm;
The demulsifier used in the dosing tank (2) is an inorganic demulsifier, the concentration is 2-6 wt%, and the dosage is 0.5-20 ppm;
Suspended matters in the wastewater in the intermediate tank (4) are controlled to be reduced to below 50mg/L, so that physical blockage of a catalyst in a catalytic oxidation unit (7) and anaerobic sludge loss of a UASB reactor (10) caused by overhigh concentration of the suspended matters are avoided;
Acid added in the intermediate pool (5) is dilute hydrochloric acid, and the pH of the wastewater in the intermediate pool is controlled to be 3-6;
the catalytic oxidation unit (7) has the reaction conditions of pH of 3-6, hydrogen peroxide addition of 0.6-1.2 times of COD removal amount and reaction time of 30-60 min at normal temperature and normal pressure;
The alkali liquor that adds in middle pond (8) is sodium bicarbonate, adjusts waste water pH and is 7.2~7.4, has improved the buffer capacity of waste water to the pH change simultaneously, ensures the high-efficient steady operation of UASB reactor.
5. the cutting emulsion wastewater treatment system according to claim 1, wherein: the volume load of the UASB reactor (10) is 2-6 kg/(m 3. d), and the sludge load of the contact oxidation device (11) is 0.075-0.12 kg/(Mlvss. d);
The air flotation unit (4) is provided with an overrunning pipe with the middle water tank (8), and when the concentration of organic matters in the effluent of the air flotation unit is low and the biochemical property is good, the effluent of the air flotation unit (4) totally or partially overruns to the middle water tank (8).
6. the cutting emulsion wastewater treatment system according to claim 1, wherein: the aerobic system consists of a contact oxidation device (11) which consists of a plurality of stages of aerobic and MBR units (12).
7. a method for treating cutting emulsion wastewater is characterized by comprising the following steps:
1) The wastewater enters a regulating tank (1) for homogenizing and equalizing, then enters an oil separation tank (2) for primarily removing mineral oil and animal and vegetable oil suspended in the wastewater, and scum generated by the oil separation tank (2) and residual activated sludge generated by a biochemical system enter a sludge treatment system together to realize harmless treatment; the effluent of the oil separation tank (2) enters a dosing tank (3), and the effluent enters an air floating unit (4) after polyaluminium chloride and a demulsifier are added into the dosing tank (3) to remove oil substances and suspended matters in the wastewater; the flocculant used in the dosing tank is polyaluminium chloride, the concentration of the flocculant is 4-8 wt%, and the dosing amount of the flocculant is 10-200 ppm; the demulsifier used in the dosing tank (3) is an inorganic demulsifier, the concentration is 2-6 wt%, and the dosage is 0.5-20 ppm;
2) the effluent of the air flotation unit (4) enters an intermediate tank (5), and suspended matters in the wastewater in the intermediate tank (8) are controlled to be reduced to below 50mg/L, so that the physical blockage of a catalyst in a catalytic oxidation unit (7) and the anaerobic sludge loss of a UASB reactor (10) caused by overhigh suspended matter concentration are avoided;
3) The effluent of the air flotation unit (4) enters an intermediate tank (5), a hydrochloric acid adding port is formed in the intermediate tank (8), and the pH value in the intermediate tank (8) is controlled to be 3-6; the effluent of the intermediate water tank (8) enters a cartridge filter (6) to further control SS in the wastewater, and the effluent of the cartridge filter (6) enters a catalytic oxidation unit; an overrun pipe is arranged between the air flotation unit (4) and the middle water tank (8) to meet the requirement of the UASB reactor (10) on a carbon source, and simultaneously, on the premise of ensuring that the effluent of the system reaches the standard, the water inflow and the load of the catalytic oxidation unit (7) are reduced, so that the operation cost of the whole system is reduced, and the optimization of the system operation is realized;
4) the catalytic oxidation unit (7) has the reaction conditions of pH of 3-6, hydrogen peroxide addition of 0.6-1.2 times of COD removal amount and reaction time of 30-60 min at normal temperature and normal pressure; the filler in the catalytic oxidation unit (7) is activated carbon loaded transition metal, noble metal and the like, the solid-phase catalyst is prepared by high-temperature sintering, the oxidant is hydrogen peroxide, and the oxidation pretreatment of the wastewater is realized under the normal temperature condition through the adsorption of the solid-phase catalyst, the catalysis of active groups and the oxidation of the oxidant; macromolecular organic matters which are difficult to degrade and have biotoxicity, such as mineral oil, a surfactant, a mildew-proof bactericide and the like in the wastewater are subjected to ring opening and chain scission, so that the toxicity of the wastewater is eliminated or reduced, the biodegradability of the wastewater is improved, and a substrate condition is provided for the subsequent operation of a biochemical system;
5) The effluent of the catalytic oxidation unit (7) enters an intermediate water tank (8) through a heat exchanger (9) to ensure that the temperature in the intermediate water tank (8) is 33-36 ℃ in winter in the north;
6) Sodium bicarbonate is added into the intermediate water tank (8), the pH value in the intermediate water tank (8) is controlled to be 7.2-7.4, the buffering capacity of the wastewater on pH change is improved, and the adjustment is carried out according to the actual operation condition of the UASB reactor (10); the effluent of the intermediate water tank (8) enters a UASB reactor (10) to further remove organic pollutants in the wastewater;
7) the UASB reactor (10) is connected with a circulating pump (14), the effluent of the UASB reactor (10) enters a water inlet pipeline of the UASB reactor (10) and then enters the UASB reactor (10) to improve the impact resistance of the UASB reactor (10) to the change of the inlet water load, and the hydraulic load of the UASB reactor (10) is adjusted to ensure the efficient and stable operation of the UASB reactor (10);
8) effluent of the UASB reactor (10) is subjected to advanced treatment through a contact oxidation device (11) and an MBR unit (12) to meet the requirements of wastewater discharge or reuse, and the treated wastewater is finally recycled or discharged after reaching the standard in a clear water tank;
9) biogas generated by the UASB reactor (10) is used as fuel to cooperate with a contact oxidation device (11) and biological odor generated by the MBR unit (12) to enter an incineration system for combustion as combustion air through a gas pipeline, and the biological odor is subjected to harmless treatment;
10) high-temperature flue gas generated by the incineration system (15) is connected with a heat exchanger (9) through a pipeline, waste water entering a middle water tank and a USAB reactor (10) is heated through the heat exchanger (9), the UASB reactor (10) is guaranteed to be in an optimal temperature range to operate efficiently, and low-temperature flue gas after heat exchange of the heat exchanger (9) is directly or reprocessed to reach the standard and is discharged; and the surplus heat generated by the incineration system (15) is used for waste heat utilization.
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|---|---|---|---|---|
| CN114133104A (en) * | 2021-11-22 | 2022-03-04 | 惠州宇新化工有限责任公司 | Maleic anhydride sewage treatment method and system |
| WO2023087371A1 (en) * | 2021-11-22 | 2023-05-25 | 惠州宇新化工有限责任公司 | Maleic anhydride wastewater treatment method and system |
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Application publication date: 20191206 |