CN109574321A - Oil-mud-water three-phase integratedization separator and separation method - Google Patents
Oil-mud-water three-phase integratedization separator and separation method Download PDFInfo
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- CN109574321A CN109574321A CN201910032848.5A CN201910032848A CN109574321A CN 109574321 A CN109574321 A CN 109574321A CN 201910032848 A CN201910032848 A CN 201910032848A CN 109574321 A CN109574321 A CN 109574321A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 238000000926 separation method Methods 0.000 title claims abstract description 85
- 238000006243 chemical reaction Methods 0.000 claims abstract description 72
- 239000002351 wastewater Substances 0.000 claims abstract description 60
- 238000004062 sedimentation Methods 0.000 claims abstract description 50
- 238000000034 method Methods 0.000 claims abstract description 31
- 239000010802 sludge Substances 0.000 claims abstract description 26
- 239000003814 drug Substances 0.000 claims abstract description 24
- 238000001556 precipitation Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 16
- 230000014759 maintenance of location Effects 0.000 claims description 16
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 15
- 229920002401 polyacrylamide Polymers 0.000 claims description 15
- 229910052742 iron Inorganic materials 0.000 claims description 9
- 238000005504 petroleum refining Methods 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 230000005484 gravity Effects 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- 150000002505 iron Chemical class 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 5
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 5
- 150000003839 salts Chemical class 0.000 claims description 5
- 239000002131 composite material Substances 0.000 claims description 4
- 238000009434 installation Methods 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims description 3
- -1 iron ions Chemical class 0.000 claims description 3
- 230000001737 promoting effect Effects 0.000 claims description 3
- 239000011259 mixed solution Substances 0.000 claims description 2
- 239000000243 solution Substances 0.000 claims description 2
- 238000005191 phase separation Methods 0.000 claims 1
- 238000007670 refining Methods 0.000 abstract description 3
- 239000011148 porous material Substances 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 136
- 238000005345 coagulation Methods 0.000 description 14
- 230000015271 coagulation Effects 0.000 description 14
- 238000005188 flotation Methods 0.000 description 14
- 238000004065 wastewater treatment Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 5
- 239000010410 layer Substances 0.000 description 5
- 239000012528 membrane Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 238000010008 shearing Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 2
- 239000002344 surface layer Substances 0.000 description 2
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical group ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 2
- 238000004566 IR spectroscopy Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003657 drainage water Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000010720 hydraulic oil Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 239000011499 joint compound Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F2001/007—Processes including a sedimentation step
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a kind of oil-mud-water three-phase integratedization separator and separation methods.The separator includes the reaction tank and sedimentation basin that ecto-entad is arranged with one heart, and reaction tank is the tube structure being connected to sedimentation basin, and sedimentation basin ecto-entad is divided into in sedimentation basin equipped with guide shell the oil separation area and settling zone of bottom connection.The separation method is the following steps are included: waste water to be processed reacts in reaction tank with water-oil separating medicament；Mixed liquor, which enters, realizes oil and mud-water separation in oil separation area, oil is back to reaction tank through intercommunicating pore and is discharged through oil collector sump tank, muddy water precipitation and separation in settling zone, and overflow launder discharge is flowed through on clear water.The separator and method applicable object include but is not limited to the oil refining waste water of oil removal treated different scales；It is low to be discharged oil content, advantageously reduces subsequent biological treatment water outlet COD value；Oil is recyclable in water；Sludge can be directly dehydrated with Chamber Type Diaphragm Filter Press and moisture content is low；It is easy to operate；It is low to invest operating cost.
Description
Technical Field
The invention relates to the field of wastewater treatment, in particular to an oil-mud-water three-phase integrated separation device and a separation method.
Background
The petroleum refining wastewater is treated by adopting a method of pretreatment and biological treatment, and the good pretreatment can remove oil and mud, which is the technical key for realizing high-efficiency biological treatment.
Oil removal (including tank-in-tank oil removal) is a common oil removal technology, and petroleum refining wastewater after oil removal still contains part emulsified oil and silt with oil, and if the petroleum refining wastewater directly enters a biological treatment system, negative effects can be caused on the operation and treatment effects of the system. In order to solve the problem, the existing common method adopts two-stage coagulation air flotation, but the coagulation air flotation technology generally has the following 3 problems:
(1) a large amount of oil residue (scum) to be further treated appears, and the oil residue is not easy to dehydrate and reduce the volume;
(2) the operation is not stable enough, and the effluent often carries high-concentration oil-containing suspended solids, so that the COD of the effluent after the subsequent biological treatment is difficult to reach below 30 mg/L;
(3) the system is not easy to seal, and the smell of the treatment place is heavy.
Therefore, there is a need to develop an economical and effective oil removal method for petroleum refining wastewater after oil removal.
Disclosure of Invention
The invention aims to solve the technical problem of solving the common problem caused by the coagulation air flotation technology adopted by the water outlet of the traditional oil separation tank, and provides an oil-mud-water three-phase integrated separation device and a separation method. The oil-sludge-water three-phase integrated separation device has a simple structure, the separation method is suitable for objects including but not limited to petroleum refining wastewater of different scales treated by an oil separation tank, the operation effect is stable, oil in water can be recovered, the oil content of effluent is low, the COD value of effluent of subsequent biological treatment can be reduced, the treated sludge can be directly dewatered by a box type membrane filter press, the water content is low, the operation is convenient, and the investment operation cost is low.
The invention solves the technical problems through the following technical scheme.
The invention provides an oil-mud-water three-phase integrated separation device which comprises a reaction tank and a sedimentation tank which are sleeved from outside to inside in a concentric manner, wherein the reaction tank and the sedimentation tank are of communicated barrel structures; wherein,
a propeller is arranged in the reaction tank, and an oil collecting device for intercepting an oil layer is arranged at the upper part of the reaction tank;
an overflow groove for draining water is formed in the upper portion of the sedimentation tank along the inner side of the tank wall, a guide cylinder is further arranged in the sedimentation tank, the top of the guide cylinder is connected with the tank bottom of the overflow groove or the wall surface on one side close to the axis, and the guide cylinder divides the sedimentation tank into an oil separation area and a sedimentation area which are communicated with each other at the bottom from outside to inside;
the wall of the sedimentation tank is provided with a communicating hole communicated with the reaction tank, and the installation height of the communicating hole is higher than the bottom of the guide cylinder.
In the invention, preferably, the reaction tank is connected with a water inlet pipe; more preferably, the water inlet pipe is positioned at the bottom of the outer wall of the reaction tank.
In the invention, preferably, the reaction tank is further provided with a dosing device for adding a medicament.
In the present invention, the number of the propellers is at least one, and preferably, the number of the propellers is at least 2.
In the present invention, preferably, the propeller is located at the bottom of the reaction tank.
In the present invention, the oil collecting device may be an oil collecting device conventional in the art, preferably, the oil collecting device is an oil collecting tank and/or an oil collecting pipe, and further, the oil collecting device is radially arranged at the upper part of the reaction tank.
In the present invention, preferably, the oil collecting device is connected to an oil outlet pipe.
In the invention, preferably, the communication hole is located at the upper part of the cylinder wall of the sedimentation tank and is lower than the tank bottom of the overflow tank.
In the invention, the distance between the bottom of the guide shell and the bottom of the sedimentation tank is preferably 1/3-1/2 of the height of the wall of the sedimentation tank. The guide cylinder guides the material flow to the bottom of the sedimentation tank, so that the sedimentation height of flocs or silt in the material flow is reduced, the sedimentation time is reduced, and the separation process of the silt and water in a sedimentation area is promoted.
In the present invention, preferably, the overflow trough is connected with a water outlet pipe.
In the invention, preferably, a weir plate for making the effluent uniform is further arranged in the sedimentation tank, and the weir plate is fixedly connected with a notch of the overflow groove; more preferably, the weir plate is a triangular weir plate.
In the invention, preferably, a mud scraper is arranged in a settling zone of the settling tank, and a mud collecting hopper is arranged at the bottom of the settling tank; more preferably, the sludge collecting hopper is connected with a sludge discharging device for discharging sludge, and the sludge discharging device is preferably a pump or an air stripper. Preferably, the sludge discharge device is connected with a sludge dewatering device, and the sludge dewatering device is preferably a box-type membrane filter press.
The invention also provides a method for separating oil, mud and water by using the oil-mud-water three-phase integrated separation device, which comprises the following steps:
(1) introducing wastewater to be treated into the reaction tank to react with a medicament for promoting oil-water separation, wherein the liquid level in the reaction tank is higher than the installation height of the communicating hole, and a mixed solution after reaction enters an oil separation zone of the sedimentation tank through the communicating hole;
(2) in the oil separation area, oil and mud are separated under the action of gravity, an oil layer obtained by separation in the oil separation area returns to the reaction tank through the communicating hole and is discharged through the oil collecting device, residual mixed liquid is precipitated in the precipitation tank, and clear liquid obtained after precipitation is discharged through the overflow groove.
In the invention, the wastewater to be treated can be petroleum refining wastewater conventional in the field, preferably petroleum refining wastewater subjected to oil removal treatment, the oil removal treatment can be oil removal treatment conventional in the field, and further, the oil content of the wastewater to be treated is 10-30 mg/L.
In the present invention, the agent can be an agent conventionally used in the art for promoting oil-water separation, and preferably, the agent comprises an iron salt and an organic polymeric flocculant, wherein the iron salt can be a single or composite solid agent or a liquid agent containing iron ions, and the iron salt is preferably polymeric ferric sulfate (such as liquid polymeric ferric sulfate); the organic polymeric flocculant can be a single or composite solid medicament, and is preferably polyacrylamide (such as solid cationic polyacrylamide).
In the invention, the dosage of the medicament can be the dosage which is conventional in the field, and preferably, the mass-volume ratio of the ferric salt (such as polymeric ferric sulfate) to the wastewater to be treated in the medicament is 20-200 mg/L based on iron; the mass-volume ratio of the organic polymeric flocculant (such as cationic polyacrylamide) to the wastewater to be treated is 0.2-5.0 mg/L. Preferably, in the medicament, the mass-volume ratio of the ferric salt to the wastewater to be treated is 50-100 mg/L based on iron; the mass volume ratio of the organic polymeric flocculant to the wastewater to be treated is 0.5-2.0 mg/L.
In the present invention, preferably, the drug can be added through the drug adding device. Preferably, the dosing inlets of the ferric salt and the organic polymeric flocculant are sequentially arranged according to the flowing direction of the wastewater to be treated.
In the present invention, the medicament is preferably added continuously, preferably in the form of a solution.
In the reaction tank, pending waste water with the medicament reacts, particularly, iron ion in the molysite is right emulsified oil in the pending waste water carries out the electrical property neutralization and forms the floc with silt, through organic polymer flocculant's bridging effect, the floc grow gradually. The oil after the electrical property neutralization and the oil in the silt are condensed on the surfaces of the flocs or the silt to form large oil drops, and the oil drops are separated from the surfaces of the flocs or the silt under the action of hydraulic stirring and shearing of the propeller.
In the invention, the propeller can be a propeller which is conventional in the field, and preferably, the input power density of a motor of the propeller is 0.50-2.00W/m3The motor input power density of the propeller can influence the flow velocity of material flows in the reaction tank, and then the hydraulic stirring shearing action is influenced, the motor input power density is too low, oil drops are not favorably separated from the surfaces of flocs or silt, and the motor input power density is too high, so that severe turbulence can be caused, and oil drops are not favorably floated.
In the present invention, preferably, the average flow velocity of the material flow in the reaction tank is 0.3 to 0.5 m/s.
In the invention, the hydraulic retention time of the reaction tank is 4-10 h; more preferably, the hydraulic retention time of the reaction tank is 6-8 h.
In the invention, the hydraulic retention time of the oil separating area is preferably 15-30 min. In the oil separation area, under the action of gravity, oil and mud are separated, the separated oil floats to the surface layer of the reaction tank through the communicating holes and is discharged after being intercepted by the oil collecting device, and floc is left in the water phase to realize the separation of the oil and the mud and the water. The guide cylinder drains water and flocs to the bottom of the sedimentation tank, so that the sedimentation height of the flocs is reduced, the sedimentation time is shortened, and the separation process of mud and water in a sedimentation area is promoted.
In the invention, the hydraulic retention time of the settling zone is preferably 4-12 h. In the settling zone, under the action of gravity, flocs are left at the bottom of the settling tank, and water overflows upwards to realize separation of mud and water.
On the basis of the common knowledge in the field, the above preferred conditions can be combined randomly to obtain the preferred embodiments of the invention.
The reagents and starting materials used in the present invention are commercially available.
The positive progress effects of the invention are as follows:
(1) the separation of low-concentration oil in the wastewater is realized;
(2) the operation effect is stable, the oil content of the effluent is low, and the COD value of the effluent after the subsequent biological treatment is favorably reduced;
(3) the sludge obtained by treatment is easy to dehydrate, and the water content of the dehydrated sludge cake is less than 60%;
(4) the application range is wide, and the water treatment amount is large;
(5) the investment and the operation cost are low;
(6) the automation degree of the treatment process is high, and the operation is simple.
Drawings
FIG. 1 is a schematic view of the structure of the separation apparatus of the present invention;
FIG. 2 is a schematic view of section A-A of FIG. 1;
FIG. 3 is a process flow diagram of wastewater treatment according to example 1 of the present invention.
Description of reference numerals:
1-a reaction tank, 2-a sedimentation tank and 3-a communication hole;
11-a water inlet pipe, 12-a propeller, 13-an oil collecting device and 131-an oil outlet pipe;
21-an overflow groove, 22-a weir plate, 23-a guide shell and 24-a mud collecting bucket;
201-oil separation zone, 202-precipitation zone.
Detailed Description
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention. The experimental methods without specifying specific conditions in the following examples were selected according to the conventional methods and conditions, or according to the commercial instructions.
In the following examples, methods for measuring COD and oil content were performed according to national standards, specifically with reference to "Water and wastewater monitoring and analysis method", national environmental sciences Press, fourth edition, 2002; specifically, the COD detection method is a potassium dichromate method; the detection method of the oil content is carbon tetrachloride extraction-infrared spectrophotometry.
Example 1
As shown in fig. 1 to 2, the present embodiment provides an oil-mud-water three-phase integrated separation device, the size of the separation device is Φ 36 × 6m, the separation device includes a reaction tank 1 and a sedimentation tank 2 that are concentrically sleeved from outside to inside, and the reaction tank 1 and the sedimentation tank 2 are of a mutually communicated cylinder structure; wherein the width of the reaction tank 1 is 4m, i.e. the difference between the outer diameter and the inner diameter of the reaction tank 1 is 8m, and the effective volume of the reaction tank 1 is 2200m3。
The reaction tank 1 is connected with a water inlet pipe 11, the bottom of the reaction tank 1 is provided with two propellers 12 for pushing fluid to flow in the reaction tank 1, the upper part of the reaction tank 1 is radially provided with an oil collecting device 13, the oil collecting device 13 is specifically set as an oil collecting tank, and during actual manufacturing, selection can be carried out between the oil collecting tank or an oil collecting pipe. The fluid in the reaction tank 1 flows under the driving of the propeller 12, the oil layer floating on the upper layer is intercepted when passing through the oil collecting device 13, the oil collecting device 13 is connected with an oil outlet pipe 131, and the collected oil is discharged through the oil outlet pipe 131.
The reaction tank 1 is also provided with a dosing device, the medicament is added through the dosing device, the addition mode can be continuous addition, and when the medicament is a solid medicament, the medicament is dissolved and then added into the system.
An annular overflow trough 21 for draining water is formed inwards along the wall of the barrel at the upper part of the sedimentation tank 2, and the overflow trough 21 is connected with a water outlet pipe. A triangular weir plate 22 for making the effluent uniform is also arranged in the sedimentation tank 2, and the weir plate 22 is fixedly connected with the notch of the overflow trough 21. The wall surface of one side of the overflow groove 21 close to the axial center is connected with a guide shell 23, the guide shell 23 divides the sedimentation tank 2 into an oil separation area 201 and a sedimentation area 202 which are communicated at the bottom from outside to inside, and the effective volume of the oil separation area 201 is 130m3The effective volume of the settling zone 202 is 3200m3。
The barrel wall of the sedimentation tank 2 is provided with a communicating hole 3 communicated with the reaction tank 1, and the communicating hole 3 is positioned at the upper part of the barrel wall of the sedimentation tank 2 and is lower than the tank bottom of the overflow tank 21.
A mud scraper is arranged in a settling zone 201 of the settling pond 2, and a mud collecting hopper 24 is arranged at the bottom of the settling pond 2; to the sludge hopper 24 is connected a sludge discharge device for discharging sludge, which can be selected between a pump and a stripper. The sludge discharge device is connected with a sludge dewatering device, and the sludge dewatering device can be specifically arranged into a box-type membrane filter press.
In the embodiment, the wastewater is oil tank cutting water, electric desalting wastewater, refining drainage water and other wastewater from petroleum refining enterprises, and the treated water amount is 6000-12000 m3And d, the COD of the wastewater is 400-3000 mg/L, the oil content is 100-2000 mg/L, the adopted wastewater treatment technical process is oil separation treatment → oil-mud-water three-phase integrated separation → biological treatment, and the process flow chart is shown in figure 3.
It should be noted that, in this embodiment, the treatment water amount, COD, and oil content of the wastewater are changed according to the production conditions of the enterprises, and the oil content is an important index of the oil removal treatment, so that the oil content of the wastewater after the oil removal treatment fluctuates little.
Wherein, the oil separation treatment adopts the prior art to carry out treatment, such as hydraulic oil separation or gravity oil separation, and the actual treatment can be selected according to the requirement. The treated water volume of the wastewater after oil removal treatment is 6000-12000 m3And d, the COD of the wastewater is 270-910 mg/L, and the oil content is 15.3 +/-3.4 mg/L.
The oil-mud-water three-phase integrated separation device is adopted to further treat the wastewater after oil removal treatment, and the specific steps and the operation data statistics in the last half year are as follows:
(1) waste water gets into the reaction tank through the inlet tube, react with liquid polyferric sulfate, polyacrylamide in the reaction tank, polyacrylamide drops into the reaction tank again after dissolving in aqueous, wherein, per L waste water drops into 50mg liquid polyferric sulfate (by iron) and 2.0mg polyacrylamide, liquid polyferric sulfate and polyacrylamide aqueous solution throw in the reaction tank through charge device in succession, set gradually the medicine inlet of liquid polyferric sulfate and polyacrylamide aqueous solution according to the flow direction of waste water, emulsified oil in the waste water carries out the electrical neutralization and forms the floc with silt earlier with liquid polyferric sulfate, through polyacrylamide's bridging effect, the floc grow gradually.
The fluid in the reaction tank flows in the reaction tank under the push of a propeller, and the input power density of a motor of the propeller is 0.57W/m3The average flow velocity of the material flow is 0.3m/s, the electrically neutralized oil and the oil in the silt are condensed on the surfaces of the flocs or the silt to form large oil drops, and the oil drops are separated from the surfaces of the flocs or the silt under the action of hydraulic stirring and shearing. The hydraulic retention time of the reaction tank is 4.4-8.8 h.
(2) The mixed liquid after reaction enters an oil separation area of the sedimentation tank through the communicating holes, the separated oil floats upwards through the communicating holes to the surface layer of the reaction tank under the action of gravity in the oil separation area and is discharged after being intercepted by the oil collecting tank, and flocs are left in the water phase, so that the separation of oil and mud water is realized. The guide cylinder drains water and flocs to the bottom of the sedimentation tank, so that the sedimentation height of the flocs is reduced, the sedimentation time is shortened, and the separation process of mud and water in a sedimentation area is promoted. The hydraulic retention time of the oil separation area is 16-31 min.
(3) In the settling zone, under the action of gravity, flocs are left at the bottom of the settling tank, and water flows upwards to overflow to an overflow tank, so that the separation of mud and water is realized. The hydraulic retention time of the settling zone is 6.4-12.8 h.
(4) The separated oil layer is collected by an oil collecting tank and then temporarily stored, and then transferred to a crude oil refining system; directly dehydrating the separated sludge by using a box-type membrane filter press and then transporting the sludge outwards, wherein the water content of a sludge cake is 40-50%; the oil content of the treated water is 7.4 +/-2.1 mg/L, the treated water enters a biological treatment system for biological treatment, the biological treatment adopts the prior art for treatment, for example, an A/O method, a biofilm method, a biological filter and the like can be adopted, the A/O method is adopted in the embodiment, and the A/O method can be selected according to the requirement during actual treatment. After biological treatment, the COD of the effluent is 24 +/-5 mg/L, and petroleum is not detected.
Example 2
The technical process of wastewater treatment adopted in this example is the same as that of example 1, and is "oil removal treatment → oil-mud-water three-phase integrated separation → biological treatment", wherein the treated water amount of wastewater after oil removal treatment is 8630m3And d, the COD of the wastewater is 761mg/L, and the oil content is 16.9 mg/L.
The oil-mud-water three-phase integrated separation device in the embodiment 1 is adopted to further treat the wastewater after the oil separation treatment, the specific steps are the same as those in the embodiment 1, and the difference is that the adding amount of the medicament in the reaction tank is different. In the reaction tank, 180mg of liquid polymeric ferric sulfate (calculated as iron) and 5.0mg of polyacrylamide are added into each L of wastewater. The hydraulic retention time in the reaction tank, the oil separation zone and the settling zone is 6.1h, 22min and 8.9h respectively, and the rest of the operation parameters are consistent with those in example 1. The oil content of the water treated by the oil-mud-water three-phase integrated separation device is 6.2mg/L, and the COD of the effluent after biological treatment is 25 mg/L.
Example 3
The technical process of wastewater treatment adopted in the embodiment is the same as that of the embodiment 1, namely oil removal treatment → oil-mud-water three-phase integrationSeparation → biological treatment ", wherein the treated water amount of the wastewater after the oil removal treatment is 7380m3And d, the COD of the wastewater is 581mg/L, and the oil content is 14.8 mg/L.
The oil-mud-water three-phase integrated separation device in the embodiment 1 is adopted to further treat the wastewater after the oil separation treatment, the specific steps are the same as those in the embodiment 1, and the difference is that the motor input power density of a propeller in the reaction tank is different, and the motor input power density of the propeller is 1.82W/m3The average flow velocity of the material flow is 0.5m/s, the hydraulic retention time in the reaction tank, the oil separation zone and the precipitation zone is 7.2h, 25min and 10.4h respectively, and the rest of the operation parameters are consistent with those in example 1. The oil content of the water after passing through the oil-mud-water three-phase integrated separation device is 7.8mg/L, and the COD of the effluent after biological treatment is 26 mg/L.
Example 4
The technical process of wastewater treatment adopted in this example is the same as that of example 1, and all the steps are oil removal treatment → oil-mud-water three-phase integrated separation → biological treatment, wherein the treated water amount of the wastewater after the oil removal treatment is 10740m3And d, the COD of the wastewater is 841mg/L, and the oil content is 16.2 mg/L.
The oil-mud-water three-phase integrated separation device in the embodiment 1 is adopted to further treat the wastewater after the oil separation treatment, the specific steps are the same as those in the embodiment 1, and the difference is that the input power density of a motor of a propeller in a reaction tank is 2.27W/m3The average flow velocity of the material flow is 0.7m/s, the hydraulic retention time in the reaction tank, the oil separation zone and the precipitation zone is 4.9h, 17min and 7.2h respectively, and the rest of the operation parameters are consistent with those in example 1. The oil content of the water after passing through the oil-mud-water three-phase integrated separation device is 12.6mg/L, and the COD of the effluent after biological treatment is 44 mg/L.
Example 5
The wastewater treatment technical process adopted in this example is the same as that of example 1, and all the steps are oil removal treatment →Oil-mud-water three-phase integrated separation → biological treatment ", wherein the average treated water volume of the wastewater after the oil removal treatment is 16000m3And d, the COD of the wastewater is 632mg/L, and the oil content is 18.1 mg/L.
The oil-sludge-water three-phase integrated separation device in the embodiment 1 is adopted to further treat the wastewater after oil separation treatment, the specific steps are the same as those in the embodiment 1, the difference is that the hydraulic retention time of the reaction tank, the oil separation zone and the settling zone is different due to the difference of water inflow amount, wherein the hydraulic retention time in the reaction tank, the oil separation zone and the settling zone is respectively 3.3h, 11.7min and 4.8h, and the rest operation parameters are the same as those in the embodiment 1. The oil content of the water after passing through the oil-mud-water three-phase integrated separation device is 12.7mg/L, and the COD of the effluent after biological treatment is 37 mg/L.
Comparative example 1
The technical process of wastewater treatment adopted by the comparative example is oil separation treatment → separation of a secondary coagulation air flotation device → biological treatment, wherein the treatment water volume of the wastewater subjected to the oil separation treatment is 7000-12000 m3And d, the COD of the wastewater is 370-1120 mg/L, and the oil content is 90-170 mg/L.
It should be noted that, in the present comparative example, the oil removal treatment is performed by using gravity oil removal, and the oil removal mode is relatively unstable, which results in large fluctuation of the oil content of the effluent.
The effluent after oil removal treatment is further deoiled by adopting a secondary coagulation air flotation device, and the method comprises the following specific steps:
(1) adding polyaluminium chloride and polyacrylamide into the wastewater, wherein 250mg of polyaluminium chloride and 20mg of polyacrylamide are added into each L of wastewater, and the polyaluminium chloride and the polyacrylamide are mixed and then sequentially enter a primary coagulation air flotation device and a secondary coagulation air flotation device, wherein the primary coagulation air flotation device and the secondary coagulation air flotation device adopt coagulation air flotation devices in the prior art, and small-particle-size oil and emulsified oil in water are driven to float upwards through bubbles;
(2) a large amount of oil residue (scum) is generated in the treatment process, calcium carbonate and polyacrylamide are adopted for treatment, the sludge is transported out for disposal after centrifugal dehydration, the disposal cost is high, and the water content of mud cakes is more than 90%; in the process of treating the secondary coagulation air flotation device, no crude oil is recovered; the oil content of the water treated by the secondary coagulation air flotation device is 20-70 mg/L, so that the stability of system operation is poor and the fluctuation of the oil content of the discharged water is large when the secondary coagulation air flotation device is used for treatment.
The water treated by the secondary coagulation air flotation device is subjected to biological treatment as in example 1, and the COD of the effluent is 80-100 mg/L.
Claims (10)
1. An oil-mud-water three-phase integrated separation device is characterized by comprising a reaction tank and a sedimentation tank which are sleeved from outside to inside in a concentric manner, wherein the reaction tank and the sedimentation tank are of communicated barrel structures; wherein,
a propeller is arranged in the reaction tank, and an oil collecting device for intercepting an oil layer is arranged at the upper part of the reaction tank;
an overflow groove for draining water is formed in the upper portion of the sedimentation tank along the inner side of the tank wall, a guide cylinder is further arranged in the sedimentation tank, the top of the guide cylinder is connected with the tank bottom of the overflow groove or the wall surface on one side close to the axis, and the guide cylinder divides the sedimentation tank into an oil separation area and a sedimentation area which are communicated with each other at the bottom from outside to inside;
the wall of the sedimentation tank is provided with a communicating hole communicated with the reaction tank, and the installation height of the communicating hole is higher than the bottom of the guide cylinder.
2. The oil-sludge-water three-phase integrated separation device as claimed in claim 1, wherein the reaction tank is connected with a water inlet pipe; preferably, the water inlet pipe is positioned at the bottom of the outer wall of the reaction tank;
and/or the reaction tank is also provided with a dosing device;
and/or the number of the propellers is at least one; preferably, the number of said thrusters is at least 2;
and/or the propeller is positioned at the bottom of the reaction tank;
and/or the oil collecting device is an oil collecting groove and/or an oil collecting pipe;
and/or the oil collecting device is radially arranged at the upper part of the reaction tank;
and/or the oil collecting device is connected with an oil outlet pipe;
and/or the communication hole is positioned at the upper part of the cylinder wall of the sedimentation tank and is lower than the tank bottom of the overflow tank;
and/or the distance between the bottom of the guide shell and the bottom of the sedimentation tank is 1/3-1/2 of the height of the wall of the sedimentation tank;
and/or the overflow groove is connected with a water outlet pipe;
and/or a weir plate for enabling water to be uniformly discharged is further arranged in the sedimentation tank, and the weir plate is fixedly connected to a notch of the overflow groove; preferably, the weir plate is a triangular weir plate;
and/or a mud scraper is arranged in a settling zone of the settling tank, and a mud collecting hopper is arranged at the bottom of the settling tank; preferably, the sludge collecting hopper is connected with a sludge discharging device for discharging sludge; more preferably, the sludge discharge device is connected with a sludge dewatering device.
3. A method for oil-mud-water three-phase separation by using the oil-mud-water three-phase integrated separation device of claim 1 or 2, which is characterized by comprising the following steps:
(1) introducing wastewater to be treated into the reaction tank to react with a medicament for promoting oil-water separation, wherein the liquid level in the reaction tank is higher than the installation height of the communicating hole, and a mixed solution after reaction enters an oil separation zone of the sedimentation tank through the communicating hole;
(2) in the oil separation area, oil and mud are separated under the action of gravity, an oil layer obtained by separation in the oil separation area returns to the reaction tank through the communicating hole and is discharged through the oil collecting device, residual mixed liquid is precipitated in the precipitation tank, and clear liquid obtained after precipitation is discharged through the overflow groove.
4. The method of claim 3, wherein the motor input power density of the propeller is 0.50-2.00W/m3。
5. The method according to claim 3 or 4, wherein the average flow velocity of the material flow in the reaction tank is 0.3 to 0.5 m/s.
6. The method according to claim 3, wherein the wastewater to be treated is petroleum refining wastewater after oil separation tank treatment; preferably, the oil content of the wastewater to be treated is 10-30 mg/L.
7. The method of claim 3, wherein the medicament comprises an iron salt and an organic polymeric flocculant, wherein the iron salt is a single or composite solid medicament or liquid medicament containing iron ions, and the iron salt is preferably polymeric ferric sulfate; the organic polymeric flocculant is a single or composite solid medicament; the organic polymeric flocculant is preferably polyacrylamide.
8. The method according to claim 7, wherein the mass-to-volume ratio of the iron salt to the wastewater to be treated in the agent is 20-200 mg/L calculated on the basis of iron; the mass volume ratio of the organic polymeric flocculant to the wastewater to be treated is 0.2-5.0 mg/L;
preferably, in the medicament, the mass-to-volume ratio of the ferric salt to the wastewater to be treated is 50-100 mg/L calculated based on iron; the mass volume ratio of the organic polymeric flocculant to the wastewater to be treated is 0.5-2.0 mg/L.
9. The method of claim 7, wherein the agent is added by a medicating device; preferably, the dosing inlets of the ferric salt and the organic polymeric flocculant are sequentially arranged according to the flowing direction of the wastewater to be treated;
and/or the medicament is added continuously;
and/or the agent is added in the form of a solution.
10. The method according to any one of claims 3 to 9, wherein the hydraulic retention time of the reaction tank is 4 to 10 hours; preferably, the hydraulic retention time of the reaction tank is 6-8 h;
and/or the hydraulic retention time of the oil separation area is 15-30 min;
and/or the hydraulic retention time of the settling zone is 4-12 h.
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