CN114105398A - Device and method for treating petrochemical wastewater by high-temperature fluid bed biochemical system - Google Patents
Device and method for treating petrochemical wastewater by high-temperature fluid bed biochemical system Download PDFInfo
- Publication number
- CN114105398A CN114105398A CN202010896517.9A CN202010896517A CN114105398A CN 114105398 A CN114105398 A CN 114105398A CN 202010896517 A CN202010896517 A CN 202010896517A CN 114105398 A CN114105398 A CN 114105398A
- Authority
- CN
- China
- Prior art keywords
- temperature
- water
- fluidized bed
- biochemical
- reaction tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000012530 fluid Substances 0.000 title claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 198
- 238000005842 biochemical reaction Methods 0.000 claims abstract description 50
- 239000010865 sewage Substances 0.000 claims abstract description 50
- 238000005273 aeration Methods 0.000 claims abstract description 21
- 241000894006 Bacteria Species 0.000 claims abstract description 14
- 238000001816 cooling Methods 0.000 claims abstract description 13
- 230000015556 catabolic process Effects 0.000 claims abstract description 12
- 238000006731 degradation reaction Methods 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 230000033228 biological regulation Effects 0.000 claims abstract description 4
- 238000004062 sedimentation Methods 0.000 claims description 24
- 150000002829 nitrogen Chemical class 0.000 claims description 21
- 150000003017 phosphorus Chemical class 0.000 claims description 21
- 238000010438 heat treatment Methods 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 14
- 239000000945 filler Substances 0.000 claims description 10
- 239000010802 sludge Substances 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000012545 processing Methods 0.000 claims description 8
- 230000003203 everyday effect Effects 0.000 claims description 6
- 238000002955 isolation Methods 0.000 claims description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 4
- 239000011159 matrix material Substances 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 229910052698 phosphorus Inorganic materials 0.000 claims description 4
- 239000011574 phosphorus Substances 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 3
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims description 2
- 238000011049 filling Methods 0.000 claims description 2
- 238000004321 preservation Methods 0.000 claims description 2
- 230000009467 reduction Effects 0.000 claims description 2
- 235000017281 sodium acetate Nutrition 0.000 claims description 2
- 239000001632 sodium acetate Substances 0.000 claims description 2
- 238000010792 warming Methods 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 150000001875 compounds Chemical class 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 41
- 229910000396 dipotassium phosphate Inorganic materials 0.000 description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- 150000003839 salts Chemical class 0.000 description 9
- 238000009826 distribution Methods 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 7
- 231100000719 pollutant Toxicity 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 5
- 230000014759 maintenance of location Effects 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- -1 aromatic amine compounds Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000004071 biological effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000036760 body temperature Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 150000002391 heterocyclic compounds Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000011272 standard treatment Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/08—Aerobic processes using moving contact bodies
- C02F3/085—Fluidized beds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/004—Apparatus and plants for the biological treatment of water, waste water or sewage comprising a selector reactor for promoting floc-forming or other bacteria
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
Abstract
The invention belongs to the technical field of environmental protection, and particularly relates to a device and a method for treating petrochemical wastewater by a high-temperature fluid bed biochemical system. The device comprises a multi-stage compressed air aeration system, a fluidized bed biochemical reaction tank, a multi-tube water inlet system and a backflow heat exchange unit, and sewage is treated through the steps of high-temperature bacteria domestication, water inlet temperature regulation, biochemical degradation, mud-water separation and effluent discharge. The high-temperature sewage directly enters a biochemical system without cooling, the investment of cooling equipment is reduced, the working time is reduced, the high-molecular compound which is difficult to process at normal temperature in a biochemical way is degraded through a biochemical working area of the fluidized bed, the effect is obvious, meanwhile, the biochemical reaction tank of the fluidized bed has the function of integrated temperature rise and degradation of the sewage, the space utilization rate is improved, the state that the flow rate of the air water at the lower part is lower is ensured, and the upper part has a certain air water flow rate.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and particularly relates to a device and a method for treating petrochemical wastewater by a high-temperature fluid bed biochemical system.
Background
Petrochemical is a series of organic matter processing processes which mainly use petroleum as raw materials and adopt processes such as cracking, refining, fractionation, reforming, synthesis and the like. The production process is long, the production devices are more, the produced sewage is large in water quantity, and the sewage contains various pollutants such as petroleum, COD, ammonia nitrogen, sulfur, phenol and the like. Meanwhile, due to different products, chemical enterprises generate sewage containing various characteristic pollutants related to organic chemical products, such as polycyclic aromatic hydrocarbon compounds, aromatic amine compounds, heterocyclic compounds and the like, so that the sewage is not only complex in water quality, but also rich in toxic substances.
The sewage treatment system of the enterprise faces multiple challenges, not only needs to contain more than a plurality of complex pollutants, but also changes the sewage quantity and the content and the property of the pollutants when the upstream system is started and stopped, overhauled, changes the raw material source and other production fluctuations, and increases the impact load of the sewage treatment facility. In many sewage treatment plants, biochemical effluent still contains high-content and difficultly-degradable substances which cannot be discharged outside, and further other technologies such as targeted advanced oxidation and the like are needed, so that the economic and management costs are greatly increased.
In addition, the waste temperature of some chemical wastewater is higher, and is above 50 ℃. The waste water with the temperature of 50-70 ℃ is cooled to below 37 ℃ by cooling equipment, and then enters a biological treatment system. The required cooling equipment has large investment, easy corrosion, high cost and frequent maintenance.
Patent CN1295166C provides a method for directly treating high-temperature high-turbidity PVC mother liquor water by a biological filter, the mother liquor enters a hydrolysis tank after being primarily cooled, then the effluent enters an aeration biological filter for biochemical reaction, and the effluent is recycled in PVC production through air flotation and filtration. The method aims at the development goal of the PVC mother liquor, namely sewage recycling, the technical design does not relate to other sewage, and high-temperature biochemistry is a link of the process and bears the impact of the high-temperature sewage. The method does not provide more technical targets and structural designs around high-temperature biochemistry, and the strain domestication method is specific.
The patent CN107129030A provides a device and a method for treating medium-high temperature organic wastewater, wherein a computer control system detects the fed water suspended matters to control the feeding of a flocculating agent, the higher total microbial quantity and the higher biological activity of a biochemical tank are kept, and a membrane module is selected according to the water inlet temperature to filter the outlet water. The invention focuses on the design combination of the device, and no proposal is provided for strain selection and domestication of the biochemical unit.
In summary, the current application of high temperature biochemical technology has the following technical problems:
1. the research aiming at the operating conditions of the high-temperature biochemical system and the design lack of a matching device;
2. the development of high-temperature biochemical strain culture means is less.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the device and the method for treating petrochemical sewage by the high-temperature fluid bed biochemical system overcome the defects of the prior art, the domesticated microorganisms directly treat high-temperature wastewater in the device through high-temperature bacteria domestication, and the fluid bed biochemical system can degrade various pollutants which are difficult to degrade more quickly and efficiently, reduce the downstream treatment pressure and reduce the environmental damage.
The device for treating petrochemical sewage by the high-temperature fluid bed biochemical system comprises a multi-stage compressed air aeration system, a fluid bed biochemical reaction tank, a multi-pipe water inlet system and a reflux heat exchange unit, wherein the multi-stage compressed air aeration system comprises a multi-stage compressor, a main air inlet pipe and a plurality of air inlet branch pipes, the multi-stage compressor, the main air inlet pipe and the air inlet branch pipes are sequentially connected, the air inlet branch pipes are arranged at the bottom in the fluid bed biochemical reaction tank, and a plurality of aeration heads are arranged on the air inlet branch pipes; the biochemical reaction tank of the fluidized bed is internally provided with an isolation sieve plate which divides the biochemical reaction tank of the fluidized bed into a biochemical working area of the fluidized bed and a heating area from top to bottom, and the biochemical working area of the fluidized bed is filled with a filler; the multi-pipe water inlet system comprises a water inlet main pipe and a plurality of water inlet branch pipes, wherein the water inlet main pipe is connected with the water inlet branch pipes in sequence, the water inlet branch pipes are arranged in the heating area, and water outlet holes are formed in the water inlet branch pipes and are annularly arranged in a multilayer manner; the backflow heat exchange unit comprises a sedimentation tank, a water outlet at the upper part of the biochemical reaction tank of the fluidized bed is connected with a water inlet of the sedimentation tank, a water outlet pipe is arranged at the upper part of the sedimentation tank, an outlet at the bottom of the sedimentation tank is connected with a biochemical working area of the fluidized bed, a coil pipe is arranged in the sedimentation tank, and an outlet and an inlet of the coil pipe are connected with a water inlet main pipe.
The fluidized bed biochemical reaction tank is a deep-well type fluidized bed biochemical reaction tank, structures can be built underground and overground, the bottom width and the top width are adopted, the included angle between the outer wall and the bottom surface is 75-80 degrees, preferably 75 degrees, the outer cylinder body and the prism body can be used, and when the cylinder body is adopted, the radius ratio of the top of the tank to the bottom of the tank is 0.18-0.64, preferably 0.45-0.64; the outer wall is provided with a heat-insulating layer, and the top is provided with a sealing cover and an exhaust passage.
The volume of the deep-well type flowing bed biochemical reaction tank accounts for 40-55%, preferably 55% of the volume of the flowing bed biochemical reaction tank, an isolation sieve plate is arranged at the lower boundary of the flowing bed biochemical reaction area, the reaction tank is divided into a heating area and a flowing bed working area, the isolation sieve plate is preferably made of stainless steel, and the diameter of a sieve pore is 20 mm. A mixed flow pump can be additionally arranged to pump the sewage at the upper part of the heating area into a biochemical working area of the fluidized bed, so that the water temperature and water quality mixing rate at two sides of the sieve plate is improved. The method is characterized in that the fluidized bed filler is selected but not limited to MBBR filler, the type is selected to be phi larger than 30 mm, the thickness is 12-14 mm, the volume of a biochemical working area of the fluidized bed is 50-60% of the volume of the fluidized bed, the filler is a commercially available product, is made of plastic materials, is shaped like a flat cylinder, has a plastic structure inside, is large in specific surface area, and is attached with high-temperature bacteria.
According to the multi-stage compressed air aeration system, compressed air is prepared by adopting a multi-stage compressor, and the type of a product sold in the market is selected according to the balance of the treated water quantity and the temperature. The compressed air firstly provides dissolved oxygen for the biological bed, has the stirring effect and secondly provides the heat required by constant temperature for the reaction tank at high temperature. The compressed air inlet main pipe is divided into a plurality of inlet branch pipes after entering the reaction tank, each inlet branch pipe is provided with a plurality of aeration heads, the diameters of the aeration heads are 50-80 cm, the optimal selection is 50 cm, and the installation interval is 10-15 cm. The high-temperature compressed air realizes heat exchange with the water body and inlet water in the reaction tank at the lower part of the reaction tank, the temperature of the whole reaction tank is kept constant, and the operation temperature of the system is controlled between 45 ℃ and 65 ℃ by adjusting the temperature of the compressed air and the temperature of the supplied air.
The multi-pipe water inlet system distributes water in multiple layers and multiple points, and exchanges heat with high-temperature air quickly and uniformly. The water inlet main pipe enters the reaction tank and is divided into a plurality of water inlet branch pipes which are annularly arranged, small holes are formed in the pipes, the diameter of each pipe is 5-20 mm, and the diameter of each pipe can be adjusted according to the amount of treated water; the horizontal height and the annular inner diameter of the annular branch pipes are different, so that multi-point water outlet is three-dimensional and hemispherical, the vertical distance between every two branch pipes is 80-120 cm, and the horizontal distance is 50-80 cm. The number of the annular branch pipes is related to the volume of the lower part of the reaction tank, the water inlet quantity and the water inlet temperature, preferably more than 3 layers, and fixing measures are needed.
The backward flow heat transfer unit, the main part is the sedimentation tank, well upper portion is equipped with the coil pipe, diameter 30 ~ 80 millimeters, preferred 50 millimeters, when the temperature of intaking is great than the system's difference in temperature, gets into the coil pipe and goes out water and carry out the heat transfer, reentrant reaction tank after tentatively rising temperature. And (4) providing a mud-water separation function, returning the sludge to a working area of the fluidized bed, and cooling and discharging effluent to the downstream.
The method for processing the petrochemical sewage by the high-temperature fluidized bed biochemical system comprises high-temperature bacteria domestication, inflow temperature adjustment, biochemical degradation, sludge-water separation and effluent discharge, wherein aerobic bacteria collected from a sewage plant at the downstream of sewage to be processed are subjected to high-temperature bacteria domestication in a reaction tank, after the domestication is finished, the high-temperature sewage is pumped into the lower part of a deep-well type fluidized bed biochemical reaction tank through a pump, exchanges heat with high-temperature compressed air and an internal water body and then rises to a fluidized bed biochemical working area at the upper part of the reaction tank. The high-temperature compressed air has the functions of providing heat to ensure the constant temperature of the reaction tank and providing an air source for the survival of high-temperature bacteria. The high-temperature bacteria in the biochemical area carry out biochemical degradation on pollutants in sewage, the mixed liquid is pumped to the backflow heat exchange unit from the upper part of the reaction tank by a pump, partial heat can be preliminarily preheated and recycled by the coil pipe in the equipment when the temperature of inlet water is lower, and after mud-water separation, the effluent of supernatant is discharged for other purposes.
The method specifically comprises the following steps:
first, high temperature bacteria domestication
Putting active slurry in an aeration tank of a downstream sewage plant into a fluidized bed biochemical reaction tank, gradually heating for acclimatization, introducing sewage to be degraded, adding nitrogen salt and phosphorus salt to ensure that the mass ratio of phosphorus to nitrogen to COD is more than 1:5:100, and controlling MLSS to be 3-5 g/L;
secondly, temperature regulation by water inflow
After the domestication is finished, adding the sewage into a fluidized bed biochemical reaction tank through a main water inlet pipe and a branch water inlet pipe, starting a multi-stage compressed air aeration system, and heating the sewage in a temperature rising area of the fluidized bed biochemical reaction tank; when the inlet temperature of the sewage is lower than that of the effluent water discharged by the water outlet pipe in the fifth step by more than 5 ℃, the sewage firstly enters the coil pipe in the sedimentation tank from the main water inlet pipe, and then enters the sedimentation tank from the main water inlet pipe after heat exchange. If the temperature difference is not large, the inlet water can directly enter the reaction tank, and in the heating area at the lower part, the high-temperature and high-pressure air provided by the multistage compressor exchanges heat with the water body and the inlet water in the tank, so that the constant temperature of the system is ensured. For example, the operation temperature of the device is set to 55 ℃, the inlet water is 52 ℃, high-temperature high-pressure gas is used for providing two parts of heat, the inlet water is heated to 55 ℃ in the heating area, and the part emitted by the environment of the reaction tank is compensated to ensure that the operation temperature of the system is kept at 55 ℃; if the temperature of the inlet water is 60 ℃, the operation temperature is set to 55 ℃, external heat is not added, the temperature of the system is naturally cooled to 53 ℃, and the heat provided by the high-temperature high-pressure gas is only required to be increased from 53 ℃ to 55 ℃.
The multilayer multi-point water inlet and distribution system enables water inlet to be distributed in a hemispherical shape and to efficiently exchange heat with high-temperature and high-pressure air in the reaction tank.
Third, biochemical degradation
The sewage enters a fluidized bed biochemical working area at the upper part of a fluidized bed biochemical reaction tank under the driving of water vapor for degradation treatment; through the chimney type structure, the speed can be further increased and then the sewage flows into a biochemical working area of the moving bed, so that pollutants are degraded. Most of high-temperature bacteria are enriched in MBBR (moving bed biofilm reactor) fillers, the degradation efficiency of a mobile biological bed is higher than that of a fixed biological bed when the working volume of a biochemical region is the same under the same water quality condition, and the retention time of substances which are difficult to degrade, such as phenols and polycyclic aromatic hydrocarbons, can be adjusted according to control indexes to reach different degradation degrees.
Fourthly, separating mud from water
Discharging the degraded sludge-water mixed liquor from the upper part of the fluidized bed biochemical reaction tank into a sedimentation tank of the reflux heat exchange unit for separation, and refluxing sludge to a fluidized bed biochemical working area; MLSS of the biochemical working area of the fluidized bed is reduced by a sludge discharge mode, and the reduction amplitude of the MLSS is lower than 1g/L every week.
Fifth, the effluent is discharged
The upper part of the sedimentation tank of the reflux heat exchange unit is discharged through a water outlet pipe, and the effluent is subjected to subsequent standard treatment or recycling treatment according to the water quality.
Wherein:
the domestication step in the first step is as follows:
(1) introducing sewage to be degraded, cooling the sewage to the temperature of inoculated active slurry by an external heat exchanger, gradually reducing the load of the heat exchanger until the heat exchanger is removed along with the increase of the acclimation temperature, and when BOD/COD is not less than 0.1 and not more than 0.2 and BOD is not more than 50mg/L, adding a co-matrix to help initial acclimation, wherein the co-matrix is preferably sodium acetate, and the BOD is increased to 10-20 mg/L; when BOD/COD is more than or equal to 0.2, directly domesticating, adding nitrogen salt and phosphorus salt to ensure that the mass ratio of phosphorus to nitrogen to COD is more than 1:5:100, controlling the MLSS (mixed liquor suspended solid concentration) to be 3-5 g/L, and raising the water temperature of a system by 1 ℃ every day when the water temperature is less than 40 ℃;
(2) keeping the temperature for 72 hours after the water temperature reaches 40 ℃, and controlling the MLSS to be 3-5 g/L;
(3) when domestication is carried out at 40-45 ℃, the water temperature rises by 1 ℃ every 48 hours, and MLSS is controlled to be 3-5 g/L;
(4) keeping the temperature for 72 hours after the water temperature reaches 45 ℃, and controlling the MLSS to be 3-5 g/L;
(5) when domestication is carried out at 45-50 ℃, 1 ℃ is raised every 72 hours, and MLSS is controlled at 3-5 g/L;
(6) when the water temperature reaches 50 ℃, keeping for 12 hours; after the temperature of the system is reduced to 48 ℃, keeping for 24 hours; the water temperature rises from 1 ℃ to 50 ℃ every 24 hours;
(7) when the water temperature reaches 50-60 ℃, the temperature rises by 1 ℃ every 24 hours, the MLSS is controlled to be 3-5 g/L, and when the water temperature reaches 60 ℃, the MLSS is kept for 12 hours; after the temperature of the system is reduced to 58 ℃, keeping for 12 hours; the water temperature rises from 1 ℃ to 60 ℃ every 24 hours;
(8) and when the water temperature reaches 60-65 ℃, raising the temperature by 1 ℃ every 24 hours, controlling the MLSS at 3-5 g/L, and finishing domestication.
The domestication of the high-temperature bacteria can also be related to the system operation temperature, and the domestication of the high-temperature bacteria can be stopped when the water temperature reaches the system operation temperature, so that the domestication is finished. For example, the system temperature is positioned at 55 ℃, and the domestication temperature of the thermophilic bacteria can be stopped when the domestication temperature is 55-57 ℃.
Compared with the prior art, the invention has the following beneficial effects:
1. the high-temperature wastewater directly enters the biochemical system without being cooled, so that the investment of cooling equipment is reduced, and the working time is shortened.
2. The biochemical working area of the flowing bed can also degrade macromolecular compounds which are difficult to biochemically treat at normal temperature, such as phenols, polycyclic aromatic hydrocarbons and the like, and has obvious effect, and the degradation efficiency of the flowing biological bed is higher than that of a fixed biological bed when the volumes of the biochemical working areas are the same under the same water quality condition.
3. The isolation sieve plate is arranged at the boundary of the biochemical working area of the fluidized bed, so that MBBR packing is protected from entering an elevated temperature area, and the maximum volume of the biochemical working area of the fluidized bed is increased.
4. The multi-stage compressor, multi-point aeration and multi-layer multi-point water distribution combination of the invention finish temperature and aeration quantity regulation and control in the heating zone, and ensure the stable distribution of the water body temperature of the reaction tank.
5. The deep-well type fluidized bed biochemical reaction tank has the function of integrated temperature rise and degradation of sewage, improves the space utilization rate and reduces the construction of other structures; the structure of the chimney type with wide lower part and narrow upper part ensures the lower gas-water flow velocity state of the lower part and the certain gas-water flow velocity of the upper part.
6. The reflux heat exchange unit has a mud-water separation reflux function and a heat optimization function, and reduces energy loss.
7. The invention has wide water quality temperature range, short process flow, no need of cooling equipment investment, small occupied area and reduced environmental damage.
Drawings
FIG. 1 is a schematic diagram of the apparatus of the present invention;
FIG. 2 is a schematic structural diagram of an apparatus for a fluidized bed biochemical reaction tank according to the present invention;
in the figure: 1. a multistage compressor; 2. a fluidized bed biochemical reaction tank; 3. a sedimentation tank; 4. a water outlet pipe; 5. a coil pipe; 6. a main water inlet pipe; 7. a water inlet branch pipe; 8. an intake branch pipe; 9. an aeration head; 10. a main air inlet pipe; 11. a biochemical working area of the fluidized bed; 12. a filler; 13. isolating the sieve plate; 14. a temperature rising zone; 15. a mixed flow pump; 16. sealing the cover; 17. an exhaust passage.
Detailed Description
The invention is further described below with reference to the accompanying drawings and examples.
As shown in fig. 1-2, the device for treating petrochemical wastewater by using a high-temperature fluid bed biochemical system comprises a multi-stage compressed air aeration system, a fluid bed biochemical reaction tank 2, a multi-tube water inlet system and a reflux heat exchange unit, wherein the multi-stage compressed air aeration system comprises a multi-stage compressor 1, a main air inlet pipe 10 and a plurality of branch air inlet pipes 8 arranged at the bottom in the fluid bed biochemical reaction tank 2, which are sequentially connected, and a plurality of aeration heads 9 are arranged on the branch air inlet pipes 8; an isolation sieve plate 13 is arranged in the fluidized bed biochemical reaction tank 2 to divide the fluidized bed biochemical reaction tank 2 into a fluidized bed biochemical working area 11 and an elevated temperature area 14 from top to bottom, and the fluidized bed biochemical working area 11 is filled with a filler 12; the multi-pipe water inlet system comprises a water inlet main pipe 6 and a plurality of water inlet branch pipes 7, wherein the water inlet main pipe 6 is connected with the water inlet branch pipes 7 in sequence, the water inlet branch pipes 7 are arranged in a heating area 14, and water outlet holes are formed in the water inlet branch pipes 7 and are annularly arranged in a multilayer manner; the backflow heat exchange unit comprises a sedimentation tank 3, a water outlet at the upper part of a flow bed biochemical reaction tank 2 is connected with a water inlet of the sedimentation tank 3, a water outlet pipe 4 is arranged at the upper part of the sedimentation tank 3, an outlet at the bottom of the sedimentation tank 3 is connected with a flow bed biochemical working area 11, a coil pipe 5 is arranged in the sedimentation tank 3, and an outlet and an inlet of the coil pipe 5 are connected with a water inlet main pipe 6.
The fluidized bed biochemical reaction tank 2 is a deep well type fluidized bed biochemical reaction tank, adopts a form of bottom wide and top narrow, the included angle between the outer wall and the bottom surface is 75-80 degrees, the outer wall is provided with a heat preservation layer, and the top is provided with a sealing cover 16 and an exhaust passage 17.
The upper part of the heating area 14 is connected with the fluidized bed biochemical working area 11 through a mixed flow pump 15.
The volume of the fluid bed biochemical working area 11 accounts for 40-55% of the volume of the fluid bed biochemical reaction tank 2, and the filling volume of the filler 12 is 50-60% of the volume of the fluid bed biochemical working area 11.
The following examples use the above apparatus for treating wastewater.
Example 1
Conductivity of a certain chlor-alkali wastewater: 192. mu.S/cm, pH: 7.10, ammonia nitrogen: 4mg/L, COD: 289mg/L and 50-53 ℃ of water.
The diameter of the bottom surface of the cylinder body of the biochemical reaction tank of the fluidized bed is 3 meters, the included angle between the outer wall and the bottom surface is 75 degrees, the diameter of the top part of the cylinder body of the biochemical reaction tank of the fluidized bed is 1.36 meters, the volume of a biochemical working area of the fluidized bed accounts for 45 percent of the volume of the reaction tank, MBBR packing is added according to 50 percent of the volume of the biochemical working area of the fluidized bed, and three layers of annular branch pipes of a water distribution system are arranged.
The domesticated strain is collected from a downstream sewage treatment plant, the measured BOD/COD is more than 0.2, and the residence time of the sewage in the system is 24 hours.
(1) Cooling the wastewater to 37 ℃, introducing the wastewater into a reaction tank, controlling the dissolved oxygen content to be 2.0mg/L, MLSS to be 3-5 g/L, raising the water temperature of a system once every day, and adjusting the water inlet temperature along with the water temperature of a biochemical system;
(2) the water temperature of the system reaches 40 ℃, the system is kept for 72 hours, and NH is added into the reaction tank4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2;
(3) and (3) keeping the temperature of water at 40-45 ℃ and 1 ℃ every 48 hours, keeping the temperature of the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(4) keeping the water temperature at 45 ℃ for 72 hours, and adding NH into the water4Cl、K2HPO4And after addition, COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2;
(5) and (3) raising the water temperature of 45-50 ℃ by 1 ℃ every 72 hours, and keeping the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(6) the water temperature reaches 50 ℃ and is kept for 12 hours; the system is cooled to 48 ℃ and water inlet is increased in NH4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2; keeping for 24 hours; the water temperature rises from 1 ℃ to 50 ℃ every 24 hours, and the domestication is finished.
And (3) enabling the wastewater to enter a reaction tank, and in an elevated temperature zone at the lower part of the reaction tank, exchanging heat between high-temperature and high-pressure air provided by a multistage compressor and a water body and inlet water in the tank, ensuring that the temperature of the system is constant at 50 ℃, controlling the hydraulic retention time for 24 hours, and dissolving 2-2.5 mg/L of oxygen in a biochemical working area of a fluidized bed. And (3) enabling effluent water at the upper part of the reaction tank to enter a reflux heat exchange unit, separating mud from water, refluxing sludge, and removing COD (chemical oxygen demand) of the effluent water by 79.4-83.1%.
Example 2
Conductivity of a certain chlor-alkali wastewater: 190. mu.S/cm, pH: 7.05, ammonia nitrogen: 3.8mg/L, COD: 227mg/L, water temperature: 52 to 54 ℃.
The diameter of the bottom surface of the cylinder body of the biochemical reaction tank of the fluidized bed is 3 meters, the included angle between the outer wall and the bottom surface is 75 degrees, the diameter of the top part of the cylinder body of the biochemical reaction tank of the fluidized bed is 1.36 meters, the volume of a biochemical working area of the fluidized bed accounts for 45 percent of the volume of the reaction tank, MBBR packing is added according to 50 percent of the volume of the biochemical working area of the fluidized bed, and three layers of annular branch pipes of a water distribution system are arranged.
The domesticated strain is collected from a downstream sewage treatment plant, the measured BOD/COD is more than 0.2, and the residence time of the sewage in the system is 24 hours.
(1) Cooling the wastewater to 37 ℃, introducing the wastewater into a reaction tank, controlling the dissolved oxygen content to be 2.0mg/L, MLSS to be 3-5 g/L, raising the water temperature of a system once every day, and adjusting the water inlet temperature along with the water temperature of a biochemical system;
(2) the water temperature of the system reaches 40 ℃, the system is kept for 72 hours, and NH is added into the reaction tank4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2;
(3) and (3) keeping the temperature of water at 40-45 ℃ and 1 ℃ every 48 hours, keeping the temperature of the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(4) keeping the water temperature at 45 ℃ for 72 hours, and adding NH into the water4Cl、K2HPO4The mass ratio of the added mixture to COD is 100:8: 2;
(5) and (3) raising the water temperature of 45-50 ℃ by 1 ℃ every 72 hours, and keeping the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(6) the water temperature reaches 50 ℃ and is kept for 12 hours; the system is cooled to 48 ℃ and water inlet is increased in NH4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2; keeping for 24 hours; the water temperature rises from 1 ℃ to 53 ℃ every 24 hours, and the domestication is finished.
And (3) enabling the wastewater to enter a reaction tank, and in an elevated temperature zone at the lower part of the reaction tank, exchanging heat between high-temperature and high-pressure air provided by a multi-stage compression pump and a water body and inlet water in the tank, ensuring that the temperature of the system is constant at 53 ℃, controlling the hydraulic retention time for 40 hours, and dissolving oxygen in a biochemical working area of a fluidized bed by 2-2.5 mg/L. And (3) the effluent from the upper part of the reaction tank enters a reflux heat exchange unit, mud and water are separated, sludge flows back, and the COD removal rate of the effluent is 84.9-89.6%.
Example 3
Conductivity of a certain refinery wastewater: 2090. mu.S/cm, pH: 8.3, ammonia nitrogen: 51mg/L, COD: 1150mg/L, water temperature: 54-57 ℃.
The diameter of the bottom surface of the cylinder body of the biochemical reaction tank of the fluidized bed is 3 meters, the included angle between the outer wall and the bottom surface is 75 degrees, the diameter of the top part of the cylinder body is 1.36 meters, the volume of a biochemical working area accounts for 45 percent of the volume of the reaction tank, MBBR packing is added according to 50 percent of the volume of the biochemical working area, and three layers of annular branch pipes of a water distribution system are arranged.
The domesticated strain is collected from a downstream sewage treatment plant, the measured BOD/COD is more than 0.2, and the residence time of the sewage in the system is 24 hours.
(1) Cooling the wastewater to 37 ℃, introducing the wastewater into a reaction tank, controlling the dissolved oxygen content to be 2.0mg/L, MLSS to be 3-5 g/L, raising the water temperature of a system once every day, and adjusting the water inlet temperature along with the water temperature of a biochemical system;
(2) the water temperature of the system reaches 40 ℃, the system is kept for 72 hours, and NH is added into the reaction tank4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2;
(3) and (3) keeping the temperature of water at 40-45 ℃ and 1 ℃ every 48 hours, keeping the temperature of the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(4) keeping the water temperature at 45 ℃ for 72 hours, and adding NH into the water4Cl、K2HPO4The mass ratio of the added mixture to COD is 100:8: 2;
(5) and (3) raising the water temperature of 45-50 ℃ by 1 ℃ every 72 hours, and keeping the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(6) the water temperature reaches 50 ℃ and is kept for 12 hours; the system is cooled to 48 ℃ and water inlet is increased in NH4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2; keeping for 24 hours; the water temperature rises from 1 ℃ to 54 ℃ every 24 hours, and the domestication is finished.
And (3) enabling the wastewater to enter a reaction tank, and in an elevated temperature zone at the lower part of the reaction tank, exchanging heat between high-temperature and high-pressure air provided by a multi-stage compression pump and a water body and inlet water in the tank to ensure that the temperature of the system is constant at 54 ℃, controlling the hydraulic retention time of the system for 24 hours, and dissolving oxygen in a biochemical working area of a fluidized bed by 2-2.5 mg/L. And (3) the effluent from the upper part of the reaction tank enters a reflux heat exchange unit, mud and water are separated, sludge flows back, and the COD removal rate of the effluent is 80.7-82.8%.
Example 4
Conductivity of a certain refinery wastewater: 2090. mu.S/cm, pH: 8.3, ammonia nitrogen: 51mg/L, COD: 1150mg/L, water temperature: 54-57 ℃.
The diameter of the bottom surface of the cylinder body of the biochemical reaction tank of the fluidized bed is 3 meters, the included angle between the outer wall and the bottom surface is 80 degrees, the diameter of the top part of the cylinder body of the biochemical reaction tank is 1.36 meters, the volume of a biochemical working area of the fluidized bed accounts for 45 percent of the volume of the reaction tank, MBBR packing is added according to 50 percent of the volume of the biochemical working area, and three layers of annular branch pipes of a water distribution system are arranged.
The domesticated strain is collected from a downstream sewage treatment plant, the measured BOD/COD is more than 0.2, and the residence time of the sewage in the system is 24 hours.
(1) Cooling the wastewater to 37 ℃, introducing the wastewater into a reaction tank, controlling the dissolved oxygen content to be 2.0mg/L, MLSS to be 3-5 g/L, raising the water temperature of a system once every day, and adjusting the water inlet temperature along with the water temperature of a biochemical system;
(2) the water temperature of the system reaches 40 ℃, the system is kept for 72 hours, and NH is added into the reaction tank4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2;
(3) and (3) keeping the temperature of water at 40-45 ℃ and 1 ℃ every 48 hours, keeping the temperature of the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(4) keeping the water temperature at 45 ℃ for 72 hours, and adding NH into the water4Cl、K2HPO4The mass ratio of the added mixture to COD is 100:8: 2;
(5) and (3) raising the water temperature of 45-50 ℃ by 1 ℃ every 72 hours, and keeping the phosphorus salt: nitrogen salt: the mass ratio of COD is more than 1:5: 100;
(6) the water temperature reaches 50 ℃ and is kept for 12 hours; the system is cooled to 48 ℃ and water inlet is increased in NH4Cl、K2HPO4To COD: phosphorus salt: the mass ratio of the nitrogen salt to the salt is 100:8: 2; keeping for 24 hours; the water temperature rises from 1 ℃ to 54 ℃ every 24 hours, and the domestication is finished.
And (3) enabling the wastewater to enter a reaction tank, and in an elevated temperature zone at the lower part of the reaction tank, exchanging heat between high-temperature and high-pressure air provided by a multistage compressor and a water body and inlet water in the tank to ensure that the temperature of the system is constant at 54 ℃, controlling the hydraulic retention time of the system for 40 hours, and dissolving oxygen in a biochemical working area of a fluidized bed by 2-2.5 mg/L. And (3) the effluent from the upper part of the reaction tank enters a reflux heat exchange unit, mud and water are separated, sludge flows back, and the COD removal rate of the effluent is 85.2-90.6%.
Of course, the foregoing is only a preferred embodiment of the invention and should not be taken as limiting the scope of the embodiments of the invention. The present invention is not limited to the above examples, and equivalent changes and modifications made by those skilled in the art within the spirit and scope of the present invention should be construed as being included in the scope of the present invention.
Claims (10)
1. The utility model provides a device of biochemical sewage of high temperature fluid bed biochemical system processing petrochemical, its characterized in that: the multi-stage compressed air aeration system comprises a multi-stage compressed air aeration system, a fluidized bed biochemical reaction tank (2), a multi-pipe water inlet system and a backflow heat exchange unit, wherein the multi-stage compressed air aeration system comprises a multi-stage compressor (1), a main air inlet pipe (10) and a plurality of air inlet branch pipes (8) arranged at the inner bottom of the fluidized bed biochemical reaction tank (2) which are sequentially connected, and a plurality of aeration heads (9) are arranged on the air inlet branch pipes (8); an isolation sieve plate (13) is arranged in the fluidized bed biochemical reaction tank (2) to vertically divide the fluidized bed biochemical reaction tank (2) into a fluidized bed biochemical working area (11) and an warming area (14), and the fluidized bed biochemical working area (11) is filled with a filler (12); the multi-pipe water inlet system comprises a water inlet main pipe (6) and a plurality of water inlet branch pipes (7) which are arranged in a heating area (14) and are connected in sequence, and water outlet holes are formed in the water inlet branch pipes (7) and are annularly arranged in a multilayer manner; the backflow heat exchange unit comprises a sedimentation tank (3), a water outlet at the upper part of a fluidized bed biochemical reaction tank (2) is connected with a water inlet of the sedimentation tank (3), a water outlet pipe (4) is arranged at the upper part of the sedimentation tank (3), an outlet at the bottom of the sedimentation tank (3) is connected with a fluidized bed biochemical working area (11), a coil pipe (5) is arranged in the sedimentation tank (3), and an outlet and an inlet of the coil pipe (5) are connected with a water inlet main pipe (6).
2. The apparatus of claim 1, wherein the apparatus comprises: the fluidized bed biochemical reaction tank (2) is a deep well type fluidized bed biochemical reaction tank, adopts a form of bottom wide and top narrow, the included angle between the outer wall and the bottom surface is 75-80 degrees, the outer wall is provided with a heat preservation layer, and the top is provided with a sealing cover (16) and an exhaust channel (17).
3. The apparatus of claim 1, wherein the apparatus comprises: the upper part of the heating area (14) is connected with the biochemical working area (11) of the fluidized bed through a mixed flow pump (15).
4. The apparatus of claim 1, wherein the apparatus comprises: the volume of the fluidized bed biochemical working area (11) accounts for 40-55% of the volume of the fluidized bed biochemical reaction tank (2), and the filling volume of the filler (12) is 50-60% of the volume of the fluidized bed biochemical working area (11).
5. A method for treating petrochemical wastewater by using the high-temperature fluid bed biochemical system according to any one of claims 1 to 4, wherein the method comprises the following steps: the method comprises the following steps:
first, high temperature bacteria domestication
Putting active slurry into a fluidized bed biochemical reaction tank (2), gradually heating for acclimatization, introducing sewage to be degraded, adding nitrogen salt and phosphorus salt to ensure that the mass ratio of phosphorus to nitrogen to COD is more than 1:5:100, and controlling MLSS to be 3-5 g/L;
secondly, temperature regulation by water inflow
After the domestication is finished, adding sewage into the fluidized bed biochemical reaction tank (2) through the main water inlet pipe (6) and the branch water inlet pipe (7), starting the multi-stage compressed air aeration system, and heating the sewage in the temperature rising area (14) of the fluidized bed biochemical reaction tank (2);
third, biochemical degradation
The sewage enters a fluidized bed biochemical working area (11) at the upper part of the fluidized bed biochemical reaction tank (2) under the driving of water vapor for degradation treatment;
fourthly, separating mud from water
The degraded sludge-water mixed liquor is discharged from the upper part of the fluidized bed biochemical reaction tank (2) to a sedimentation tank (3) of the reflux heat exchange unit for separation, and the sludge flows back to a fluidized bed biochemical working area (11);
fifth, the effluent is discharged
The upper part of the sedimentation tank (3) of the reflux heat exchange unit is discharged through a water outlet pipe (4) for subsequent standard reaching treatment or recycling treatment.
6. The method for processing petrochemical wastewater by using a high-temperature fluid bed biochemical system according to claim 5, wherein the method comprises the following steps: the domestication step in the first step is as follows:
(1) introducing sewage to be degraded, cooling the sewage to the temperature of inoculating active slurry, and adding a co-matrix to increase BOD to 10-20 mg/L when BOD/COD is not more than 0.1 and not more than 0.2 and BOD is not more than 50 mg/L; when BOD/COD is more than or equal to 0.2, directly domesticating, adding nitrogen salt and phosphorus salt to ensure that the mass ratio of phosphorus to nitrogen to COD is more than 1:5:100, controlling the MLSS to be 3-5 g/L, and raising the temperature by 1 ℃ every day when the water temperature is less than 40 ℃;
(2) keeping the temperature for 72 hours after the water temperature reaches 40 ℃, and controlling the MLSS to be 3-5 g/L;
(3) when domestication is carried out at 40-45 ℃, the water temperature rises by 1 ℃ every 48 hours, and MLSS is controlled to be 3-5 g/L;
(4) keeping the temperature for 72 hours after the water temperature reaches 45 ℃, and controlling the MLSS to be 3-5 g/L;
(5) when domestication is carried out at 45-50 ℃, 1 ℃ is raised every 72 hours, and MLSS is controlled at 3-5 g/L;
(6) when the water temperature reaches 50 ℃, keeping for 12 hours; after the temperature of the system is reduced to 48 ℃, keeping for 24 hours; the water temperature rises from 1 ℃ to 50 ℃ every 24 hours;
(7) when the water temperature reaches 50-60 ℃, the temperature rises by 1 ℃ every 24 hours, the MLSS is controlled to be 3-5 g/L, and when the water temperature reaches 60 ℃, the MLSS is kept for 12 hours; after the temperature of the system is reduced to 58 ℃, keeping for 12 hours; the water temperature rises from 1 ℃ to 60 ℃ every 24 hours;
(8) and when the water temperature reaches 60-65 ℃, raising the temperature by 1 ℃ every 24 hours, controlling the MLSS at 3-5 g/L, and finishing domestication.
7. The method for processing petrochemical wastewater by using a high-temperature fluid bed biochemical system according to claim 6, wherein the method comprises the following steps: and (5) stopping when the temperature of the high-temperature bacteria acclimatization water reaches the system operation temperature, and finishing the acclimatization.
8. The method for processing petrochemical wastewater by using a high-temperature fluid bed biochemical system according to claim 6, wherein the method comprises the following steps: the co-matrix in the step (1) is sodium acetate.
9. The method for processing petrochemical wastewater by using a high-temperature fluid bed biochemical system according to claim 5, wherein the method comprises the following steps: when the water inlet temperature of the sewage in the step two is lower than that of the water discharged by the water outlet pipe (4) in the step five by more than 5 ℃, the sewage enters the coil pipe (5) in the sedimentation tank (3) from the water inlet main pipe (6) first, and then enters from the water inlet main pipe (6) after heat exchange.
10. The method for processing petrochemical wastewater by using a high-temperature fluid bed biochemical system according to claim 5, wherein the method comprises the following steps: in the fourth step, the sludge flows back to the biochemical working area (11) of the fluidized bed, MLSS of the biochemical working area (11) of the fluidized bed is reduced in a sludge discharge mode, and the reduction amplitude of the MLSS is lower than 1g/L every week.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010896517.9A CN114105398A (en) | 2020-08-31 | 2020-08-31 | Device and method for treating petrochemical wastewater by high-temperature fluid bed biochemical system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010896517.9A CN114105398A (en) | 2020-08-31 | 2020-08-31 | Device and method for treating petrochemical wastewater by high-temperature fluid bed biochemical system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114105398A true CN114105398A (en) | 2022-03-01 |
Family
ID=80359980
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010896517.9A Pending CN114105398A (en) | 2020-08-31 | 2020-08-31 | Device and method for treating petrochemical wastewater by high-temperature fluid bed biochemical system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114105398A (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2029391A (en) * | 1978-04-10 | 1980-03-19 | Albersmeyer W | Biochemical Thermophilic Waster Water Treatment |
| JP2003251374A (en) * | 2002-02-27 | 2003-09-09 | Hiroyuki Daimon | Method for enhancing biodegradability of hardly degradable wastewater using high temperature and high pressure water reaction |
| CN1597569A (en) * | 2003-09-15 | 2005-03-23 | 中国石油化工股份有限公司 | Culturing method of microbe for high temperature waste water biochemical treatment |
| CN101274783A (en) * | 2006-03-31 | 2008-10-01 | 东洋工程公司 | Method of treating at a high-temperature waste liquid from production plant for hydrocarbons or oxygen-containing compounds |
| CN101948181A (en) * | 2009-09-28 | 2011-01-19 | 中国石油天然气集团公司 | Method for treating thick oil sewage and application of thermophile bacteria in method |
| CN202361461U (en) * | 2011-12-14 | 2012-08-01 | 石家庄国融安能分布能源技术有限公司 | Device for recycling waste heat from industrial sewage for heat supply |
| CN104649405A (en) * | 2015-03-20 | 2015-05-27 | 中蓝连海设计研究院 | Cultivating method for activated sludge for biochemically treating high-temperature salt-containing wastewater |
| CN206660672U (en) * | 2016-07-22 | 2017-11-24 | 河北建研节能设备有限公司 | A kind of activity zone effluent cycle system based on heat exchange station |
| CN109368813A (en) * | 2018-07-03 | 2019-02-22 | 宜兴市永洁环保设备有限公司 | A kind of method of efficient process waste water |
| CN210012647U (en) * | 2019-03-27 | 2020-02-04 | 苏州巨耀环保科技有限公司 | Sewage biological treatment device |
| CN111440756A (en) * | 2020-05-22 | 2020-07-24 | 西安文理学院 | Method for treating petroleum sewage by using thermophilic bacteria |
-
2020
- 2020-08-31 CN CN202010896517.9A patent/CN114105398A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2029391A (en) * | 1978-04-10 | 1980-03-19 | Albersmeyer W | Biochemical Thermophilic Waster Water Treatment |
| JP2003251374A (en) * | 2002-02-27 | 2003-09-09 | Hiroyuki Daimon | Method for enhancing biodegradability of hardly degradable wastewater using high temperature and high pressure water reaction |
| CN1597569A (en) * | 2003-09-15 | 2005-03-23 | 中国石油化工股份有限公司 | Culturing method of microbe for high temperature waste water biochemical treatment |
| CN101274783A (en) * | 2006-03-31 | 2008-10-01 | 东洋工程公司 | Method of treating at a high-temperature waste liquid from production plant for hydrocarbons or oxygen-containing compounds |
| CN101948181A (en) * | 2009-09-28 | 2011-01-19 | 中国石油天然气集团公司 | Method for treating thick oil sewage and application of thermophile bacteria in method |
| CN202361461U (en) * | 2011-12-14 | 2012-08-01 | 石家庄国融安能分布能源技术有限公司 | Device for recycling waste heat from industrial sewage for heat supply |
| CN104649405A (en) * | 2015-03-20 | 2015-05-27 | 中蓝连海设计研究院 | Cultivating method for activated sludge for biochemically treating high-temperature salt-containing wastewater |
| CN206660672U (en) * | 2016-07-22 | 2017-11-24 | 河北建研节能设备有限公司 | A kind of activity zone effluent cycle system based on heat exchange station |
| CN109368813A (en) * | 2018-07-03 | 2019-02-22 | 宜兴市永洁环保设备有限公司 | A kind of method of efficient process waste water |
| CN210012647U (en) * | 2019-03-27 | 2020-02-04 | 苏州巨耀环保科技有限公司 | Sewage biological treatment device |
| CN111440756A (en) * | 2020-05-22 | 2020-07-24 | 西安文理学院 | Method for treating petroleum sewage by using thermophilic bacteria |
Non-Patent Citations (2)
| Title |
|---|
| 邹克华等: "高温优势菌生物膜法处理采油废水", 《城市环境与城市生态》 * |
| 郭同玲等: "生化法实现高氯高温稠油污水COD达标排放", 《中国海上油气》 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110776099B (en) | Self-circulation efficient biological denitrification device and working method thereof | |
| CN101503267B (en) | Coal chemical industry wastewater treating method | |
| CN102491584B (en) | Mixed treatment method of explosive waste water and nitrobenzene and aniline waster water | |
| CN103588349B (en) | A kind for the treatment of process of terephthalic acid wastewater | |
| CN102260021A (en) | Process and device for deep denitrogenation of domestic wastewater without additional carbon source | |
| WO2012075615A1 (en) | Integrated bioreactor and use thereof and method for treating high content organic wastewater | |
| CN110902945B (en) | Integrated sewage treatment method | |
| CN109734198B (en) | Dioxygen layer biofilm reactor for wastewater treatment and wastewater treatment method | |
| CN108083579B (en) | Modularized integrated system and process for treating non-fermented bean product production wastewater | |
| CN105753270A (en) | Water purifying system suitable for high-ammonia nitrogen livestock and poultry breeding wastewater | |
| CN102363547A (en) | Low concentration coal chemical industrial wastewater processing system | |
| CN102351366A (en) | Device and method for treating pharmaceutical waste water through synchronous biological denitrification and devulcanization and autotrophic biological denitrification | |
| CN210505759U (en) | Self-circulation efficient biological denitrification device | |
| CN106587349B (en) | Treatment device for high-ammonia-nitrogen high-organic-matter corn deep processing wastewater | |
| CN102642925B (en) | Annular aeration biological filter sewage low carbon treatment reactor | |
| CN114105398A (en) | Device and method for treating petrochemical wastewater by high-temperature fluid bed biochemical system | |
| CN206219393U (en) | F T synthetic wastewater processing systems | |
| CN114105397A (en) | High-temperature biochemical treatment device and method for petrochemical sewage | |
| CN202766381U (en) | Integrated anaerobic, anoxic and aerobic high-concentration wastewater treatment device | |
| CN202124543U (en) | Device for treating pharmaceutical wastewater through synchronous biological denitrification and devulcanization as well as autotrophic denitrification | |
| CN114105286A (en) | Device and method for high-temperature biochemical treatment of petrochemical wastewater | |
| CN110902946B (en) | Integrated sewage treatment device | |
| CN109942085B (en) | Continuous flow upflow type aerobic granular sludge reactor | |
| CN209778574U (en) | High ammonia-nitrogen concentration waste water treatment reaction unit | |
| CN202808480U (en) | Annular biological aerated filter sewage low-carbon treatment reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20220301 |
|
| RJ01 | Rejection of invention patent application after publication |