CN115057582A - Process and device for reducing drilling wastewater treatment cost - Google Patents
Process and device for reducing drilling wastewater treatment cost Download PDFInfo
- Publication number
- CN115057582A CN115057582A CN202210691957.XA CN202210691957A CN115057582A CN 115057582 A CN115057582 A CN 115057582A CN 202210691957 A CN202210691957 A CN 202210691957A CN 115057582 A CN115057582 A CN 115057582A
- Authority
- CN
- China
- Prior art keywords
- reactor
- treatment
- carbon dioxide
- hardness removal
- absorption liquid
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 66
- 230000008569 process Effects 0.000 title claims abstract description 58
- 238000005553 drilling Methods 0.000 title claims abstract description 22
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 19
- 238000010521 absorption reaction Methods 0.000 claims abstract description 107
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000007788 liquid Substances 0.000 claims abstract description 57
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 52
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 51
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 51
- 239000002351 wastewater Substances 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 18
- 239000003513 alkali Substances 0.000 claims abstract description 16
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 9
- 230000003068 static effect Effects 0.000 claims description 42
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims description 27
- 230000015271 coagulation Effects 0.000 claims description 20
- 238000005345 coagulation Methods 0.000 claims description 20
- 239000007789 gas Substances 0.000 claims description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 239000003546 flue gas Substances 0.000 claims description 18
- 230000003647 oxidation Effects 0.000 claims description 17
- 238000007254 oxidation reaction Methods 0.000 claims description 17
- 238000004062 sedimentation Methods 0.000 claims description 17
- 230000007246 mechanism Effects 0.000 claims description 12
- 238000004519 manufacturing process Methods 0.000 claims description 11
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 10
- 229910001424 calcium ion Inorganic materials 0.000 claims description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- 229920002401 polyacrylamide Polymers 0.000 claims description 8
- 239000003344 environmental pollutant Substances 0.000 claims description 4
- 239000003345 natural gas Substances 0.000 claims description 4
- 231100000719 pollutant Toxicity 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 3
- 239000011575 calcium Substances 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 3
- 239000011248 coating agent Substances 0.000 claims description 3
- 238000000576 coating method Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 239000002957 persistent organic pollutant Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 239000002253 acid Substances 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 239000000779 smoke Substances 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 23
- 238000003756 stirring Methods 0.000 description 3
- 241001074085 Scophthalmus aquosus Species 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a process and a device for reducing the treatment cost of drilling wastewater, and the process and the device comprise a wastewater treatment process, wherein the wastewater treatment process comprises an absorption treatment process and a reaction treatment process, the absorption treatment process adopts a carbon dioxide absorption tower for treatment and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogeneous receiving tank and a section of hardness removal treatment. According to the invention, the sodium hydroxide solution is adopted to absorb the carbon dioxide in the smoke of the medium-temperature anaerobic heating system to form the sodium carbonate solution, the absorption rate of the carbon dioxide is improved by the pH automatic control system, the pH value of the wastewater treatment process is convenient to control, the alkali is reduced, and the acid amount for adjusting the pH value is reduced.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a process and a device for reducing the treatment cost of drilling wastewater.
Background
The waste water treatment is to treat waste water by physical, chemical and biological methods, so that the waste water is purified, the pollution is reduced, the waste water is recycled and reused, water resources are fully utilized, the waste water generated in the process of drilling and production of natural gas in petroleum meeting is required to be treated, and the existing drilling and production waste water treatment equipment has certain defects: 1. the concentration of calcium ions in the drilling wastewater is high, and when the hardness of the wastewater is removed by applying a sodium hydroxide and sodium carbonate method, the adding concentration of sodium carbonate is high, so that the operation cost is high; 2. the carbon dioxide concentration in the boiler flue gas discharged by the medium temperature anaerobic system is high, and the carbon emission of the water treatment system is increased by directly discharging tail gas.
Disclosure of Invention
The invention aims to provide a process and a device for reducing the treatment cost of drilling wastewater, which have the advantage of low treatment cost and solve the problem of high treatment cost of the existing drilling wastewater treatment equipment.
In order to achieve the purpose, the invention provides the following technical scheme: the utility model provides a reduce technology of drilling wastewater treatment cost, includes the waste water treatment process, the waste water treatment process includes absorption treatment process and reaction treatment process, absorption treatment process adopts carbon dioxide absorption tower to handle and the absorption liquid jar of keeping in, reaction treatment process adopts the homogeneity to receive the pond, one section removes hard processing, two-stage section and removes hard processing, sedimentation tank, medium temperature UASB and handles and receive the oxidation pond.
The specific treatment process comprises the following steps:
the method comprises the following steps: the method comprises the following steps of sucking flue gas generated by a gas-fired boiler into a carbon dioxide absorption tower through an induced draft fan, adding alkali liquor into the carbon dioxide absorption tower through an alkali liquor adding pump, and enabling absorption liquid in an absorption liquid temporary storage tank to continuously absorb carbon dioxide in the flue gas through a circulating pump;
step two: adding an absorption liquid into the first-stage hardness removal reactor through an absorption liquid adding pump, conveying water in the homogenizing receiving tank to the first-stage hardness removal reactor through a first static mixer, and injecting a sodium hydroxide solution into the first static mixer at the same time, so that the wastewater is reacted in the first-stage hardness removal reactor;
step three: detecting the calcium ion concentration of the wastewater of the first-stage hardness removal reactor, when the concentration cannot meet the process requirement, transmitting the water obtained in the second step to a second-stage hardness removal and coagulation integrated reactor through a second static mixer, injecting a sodium carbonate solution into the second static mixer, injecting a polyaluminium chloride and polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor in the reaction process of the second-stage hardness removal and coagulation integrated reactor for hardness removal and coagulation treatment, and if the calcium ion concentration of the first-stage hardness removal effluent is less than or equal to 100mg/L, only adding the polyaluminium chloride and the polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor for coagulation treatment;
step four: and (4) enabling the water obtained in the third step to enter a sedimentation tank, a moderate-temperature UASB reactor and a contact oxidation tank in sequence for pollutant treatment.
Preferably, the pH value of the sodium hydroxide solution added into the first static mixer is 11-13, the pH value of the effluent of the first static mixer is 7-7.5, and the moderate temperature UASB reactor adopts a moderate temperature anaerobic process and stably operates at 30-35 ℃.
Preferably, the carbon dioxide absorption tower uses waste water with pH adjusted to 11-13 by adding a sodium hydroxide solution as an absorption liquid to absorb carbon dioxide gas in flue gas, and carbonate is formed for removing calcium hardness of the waste water.
Preferably, the gas boiler uses natural gas as fuel, and simultaneously hot water in the gas boiler is conveyed to the intermediate-temperature UASB reactor.
Preferably, the receiving oxidation tank reduces the concentration of organic pollutants and ammonia nitrogen in the wastewater through aerobic contact reaction, and the absorption liquid added by the first-stage hardness removal reactor needs to be quantitatively added.
The utility model provides a reduce device of brill adopts effluent treatment cost, includes absorbing device and reaction processing apparatus, its characterized in that: absorbing device includes gas boiler, draught fan, carbon dioxide absorption tower and absorption liquid and keeps in the jar, and reaction treatment device includes that the homogeneity receives the pond, one section removes hard reactor, two-stage process and removes hard reactor, sedimentation tank, medium temperature UASB reactor and receives the oxidation pond, the carbon dioxide absorption tower includes tower body and spray plate, the inner wall fixedly connected with anticorrosive coating of jar is kept in to the absorption liquid, one section removes hard reactor and includes first box and first rabbling mechanism, the two-stage process removes hard reactor and includes second box and second rabbling mechanism, medium temperature UASB reactor includes casing, third rabbling mechanism and conveying mechanism.
Preferably, gas boiler, draught fan, carbon dioxide absorption tower and absorption liquid are kept in the jar and are linked to each other in proper order, carbon dioxide absorption tower and absorption liquid are kept in the jar intercommunication and are had the circulating pump, be provided with third static mixer and fourth static mixer between circulating pump and the carbon dioxide absorption tower respectively, one side intercommunication of fourth static mixer has alkali lye to throw and adds the pump.
Preferably, a first static mixer is arranged between the homogeneous receiving tank and the first-stage hardness removal reactor, and a second static mixer is arranged between the first-stage hardness removal reactor and the second-stage hardness removal reactor.
Preferably, sedimentation tank, medium temperature UASB reactor and receiving oxidation pond link to each other in proper order, the intercommunication has the water pipe between gas boiler and the medium temperature UASB reactor, the absorption liquid is kept in the jar and is provided with the absorption liquid between one section except that hard reactor and throws the pump.
Compared with the prior art, the invention has the following beneficial effects:
1. according to the invention, the sodium hydroxide solution is adopted to absorb the carbon dioxide in the smoke of the medium-temperature anaerobic heating system to form the sodium carbonate solution, the absorption rate of the carbon dioxide is improved by the pH automatic control system, the pH value of the wastewater treatment process is convenient to control, the alkali is reduced, and the acid amount for adjusting the pH value is reduced.
2. According to the invention, the draught fan is arranged to compress flue gas of the gas-fired boiler, the flue gas is conveyed to the carbon dioxide absorption tower, absorption reaction power is provided, the circulating pump is arranged to facilitate the recycling of absorption liquid, the alkali liquor feeding pump is arranged to facilitate the injection of alkali liquor into the fourth static mixer, and the absorption liquid feeding pump is arranged to facilitate the injection of the absorption liquid into the first-stage hardness removal reactor.
Drawings
FIG. 1 is a schematic view of a processing apparatus according to the present invention;
FIG. 2 is a process flow diagram of the present invention;
FIG. 3 is a schematic view in partial cross section of a carbon dioxide absorption tower of the present invention;
FIG. 4 is a schematic view, partly in section, of an absorption liquid temporary storage tank according to the invention;
FIG. 5 is a schematic cross-sectional view of a segment of a hardness removal reactor according to the present invention;
FIG. 6 is a schematic cross-sectional view of a two-stage defluxing reactor of the present invention;
FIG. 7 is a schematic sectional view of the moderate temperature UASB reactor of the present invention.
In the figure: 1. a gas boiler; 2. an induced draft fan; 3. a carbon dioxide absorption tower; 4. a temporary absorption liquid storage tank; 5. a homogenizing receiving tank; 6. a first stage of hardness removal reactor; 7. a second stage hardness removal reactor; 8. a sedimentation tank; 9. a moderate temperature UASB reactor; 10. receiving an oxidation pond; 11. a circulation pump; 12. a third static mixer; 13. a fourth static mixer; 14. an alkali liquor feeding pump; 15. a first static mixer; 16. a second static mixer; 17. and (4) feeding an absorption liquid into a pump.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1-7, a process for reducing the treatment cost of drilling wastewater comprises a wastewater treatment process, wherein the wastewater treatment process comprises an absorption treatment process and a reaction treatment process, the absorption treatment process adopts a carbon dioxide absorption tower and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogenizing receiving tank, a first-stage hardness removal treatment, a second-stage hardness removal treatment, a sedimentation tank, a medium-temperature UASB treatment and a receiving oxidation tank.
The specific treatment process comprises the following steps:
the method comprises the following steps: the method comprises the following steps of sucking flue gas generated by a gas-fired boiler into a carbon dioxide absorption tower through a draught fan, adding alkali liquor into the carbon dioxide absorption tower through an alkali liquor adding pump, and enabling absorption liquid in an absorption liquid temporary storage tank to continuously absorb carbon dioxide in the flue gas through a circulating pump;
step two: adding an absorption liquid into the first-stage hardness removal reactor through an absorption liquid adding pump, conveying water in the homogenizing receiving tank to the first-stage hardness removal reactor through a first static mixer, and injecting a sodium hydroxide solution into the first static mixer at the same time, so that the wastewater is reacted in the first-stage hardness removal reactor;
step three: detecting the calcium ion concentration of the wastewater of the first-stage hardness removal reactor, when the concentration cannot meet the process requirement, transmitting the water obtained in the second step to a second-stage hardness removal and coagulation integrated reactor through a second static mixer, injecting a sodium carbonate solution into the second static mixer, injecting a polyaluminium chloride and polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor in the reaction process of the second-stage hardness removal and coagulation integrated reactor for hardness removal and coagulation treatment, and if the calcium ion concentration of the first-stage hardness removal effluent is less than or equal to 100mg/L, only adding the polyaluminium chloride and the polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor for coagulation treatment;
step four: and (2) enabling the water obtained in the third step to sequentially enter a sedimentation tank, a medium-temperature UASB reactor and a contact oxidation tank for pollutant treatment, wherein the pH value of a sodium hydroxide solution added into a first static mixer is 11-13, the pH value of the effluent of the first static mixer is 7-7.5, the medium-temperature UASB reactor adopts a medium-temperature anaerobic process, the operation is stable at 30-35 ℃, a carbon dioxide absorption tower uses waste water obtained by adding the sodium hydroxide solution to adjust the pH value to 11-13 as absorption liquid to absorb carbon dioxide gas in flue gas to form carbonate for removing calcium hardness of the waste water, a gas boiler uses natural gas as fuel, meanwhile, hot water in the gas boiler is conveyed to the medium-temperature UASB reactor, the concentration of organic pollutants and ammonia nitrogen in the waste water is reduced by an aerobic contact reaction in a receiving oxidation tank, and the absorption liquid added by a first-stage hardness removal reactor needs to be quantitatively added.
The utility model provides a reduce device of brill adopts effluent treatment cost, includes absorbing device and reaction processing apparatus, its characterized in that: the absorption device comprises a gas boiler 1, an induced draft fan 2, a carbon dioxide absorption tower 3 and an absorption liquid temporary storage tank 4, the reaction treatment device comprises a homogeneous receiving tank 5, a first-stage hardening removal reactor 6, a second-stage hardening removal reactor 7, a sedimentation tank 8, a medium-temperature UASB reactor 9 and a receiving oxidation tank 10, the carbon dioxide absorption tower 3 comprises a tower body and a spray plate, the inner wall of the absorption liquid temporary storage tank 4 is fixedly connected with an anticorrosive coating, the first-stage hardening removal reactor 6 comprises a first box body and a first stirring mechanism, the second-stage hardening removal reactor 7 comprises a second box body and a second stirring mechanism, the medium-temperature UASB reactor 9 comprises a shell, a third stirring mechanism and a conveying mechanism, the gas boiler 1, the induced draft fan 2, the carbon dioxide absorption tower 3 and the absorption liquid temporary storage tank 4 are sequentially connected, the carbon dioxide absorption tower 3 and the absorption liquid temporary storage tank 4 are communicated with a circulating pump 11, a third static mixer 12 and a fourth static mixer 13 are respectively arranged between the circulating pump 11 and the carbon dioxide absorption tower 3, an alkali liquor adding pump 14 is communicated with one side of a fourth static mixer 13, a first static mixer 15 is arranged between the homogenizing receiving pool 5 and the first-stage hardness removal reactor 6, a second static mixer 16 is arranged between the first-stage hardness removal reactor 6 and the second-stage hardness removal reactor 7, the sedimentation pool 8, the intermediate-temperature UASB reactor 9 and the receiving oxidation pool 10 are sequentially connected, a water pipe is communicated between the gas-fired boiler 1 and the intermediate-temperature UASB reactor 9, an absorption liquid adding pump 17 is arranged between the absorption liquid temporary storage tank 4 and the first-stage hardness removal reactor 6, the flue gas of the gas-fired boiler 1 can be compressed by arranging a draught fan 2, the flue gas is conveyed to a carbon dioxide absorption tower 3, absorption reaction power is provided, the recycling of the absorption liquid can be facilitated by arranging a circulating pump 11, the alkali liquor adding pump 14 can be conveniently injected into the fourth static mixer 13, the absorption liquid adding pump 17 is arranged, can conveniently inject the absorption liquid into one section reactor 6 that removes hard, carbon dioxide through adopting sodium hydroxide solution to absorb in the medium temperature anaerobic heating system flue gas forms sodium carbonate solution, improve the absorptivity of carbon dioxide through pH automatic control system simultaneously, the control of the waste water treatment flow pH value of also being convenient for simultaneously, reduce alkali and the acid content for the callback pH value, use this technology to carry out the processing that removes hard of high calcium ion concentration drilling wastewater, reduce waste water treatment running cost on the one hand, reducible greenhouse gas's emission simultaneously, and simultaneously, the system adopts two segmentation modes that remove hard, can compensate the demand that waste water removes hard when high temperature season flue gas volume is not enough.
The treatment method provided by the invention is adopted for treatment: the flue gas generated by a gas boiler 1 is sucked by a draught fan 2, blown out by a perforated aerator pipe arranged at the bottom of a carbon dioxide absorption tower 3 and contacted with absorption liquid in the absorption tower, the carbon dioxide in the flue gas is absorbed by the absorption liquid, the absorption liquid used in the process is effluent from a sedimentation tank 8 which is added with sodium hydroxide solution and has a pH value of 11-13, the absorption liquid circularly and continuously absorbs the carbon dioxide in the flue gas by a circulating pump 11, a fourth static mixer 13 is arranged on a water inlet pipe line of the carbon dioxide absorption tower 3, a pH detection and control system is arranged at the outlet end of the fourth static mixer 13, the metering pump is controlled by pH data detected on line to feed the sodium hydroxide solution into a first static mixer 15, the pH value of wastewater in the absorption tower is controlled to be kept at 11-13 all the time, the absorption liquid which fully absorbs the carbon dioxide is fed into a section of hardness removal reactor 6 by the metering pump, and when the liquid level of an absorption liquid temporary storage tank 4 is lower than a set value, adding water from a sedimentation tank 8 to a carbon dioxide absorption device through a metering pump, adding a sodium hydroxide solution into wastewater to adjust the pH value to 7-7.5, then carrying out a hardness removal reaction in a first-stage hardness removal reactor 6, detecting the calcium ion concentration of the wastewater in the first-stage hardness removal reactor 6, adding a sodium carbonate solution in a second-stage hardness removal stage if the hardness removal capability of an absorption liquid cannot meet the process requirement, simultaneously adding polyaluminum chloride and polyacrylamide solutions for hardness removal and coagulation treatment, if the calcium ion concentration of the first-stage hardness removal effluent is less than or equal to 100mg/L, only adding the polyaluminum chloride and polyacrylamide solutions in the sedimentation tank to carry out coagulation treatment in the second-stage hardness removal reactor 7, and enabling the effluent of the second-stage hardness removal reactor 7 to sequentially enter the sedimentation tank 8, a medium-temperature UASB reactor 9 and a receiving oxidation tank 10 for pollutant treatment.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. A process for reducing the treatment cost of drilling wastewater comprises a wastewater treatment process and is characterized in that: the wastewater treatment process comprises an absorption treatment process and a reaction treatment process, wherein the absorption treatment process adopts a carbon dioxide absorption tower to treat and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogeneous receiving tank, one-section hardness removal treatment, two-section hardness removal treatment, a sedimentation tank, intermediate temperature UASB treatment and a receiving oxidation tank.
2. The process for reducing the treatment cost of drilling and production wastewater according to claim 1, characterized in that: the specific treatment process comprises the following steps:
the method comprises the following steps: the method comprises the following steps of sucking flue gas generated by a gas-fired boiler into a carbon dioxide absorption tower through a draught fan, adding alkali liquor into the carbon dioxide absorption tower through an alkali liquor adding pump, and enabling absorption liquid in an absorption liquid temporary storage tank to continuously absorb carbon dioxide in the flue gas through a circulating pump;
step two: adding an absorption liquid into the first-stage hardness removal reactor through an absorption liquid adding pump, conveying water in the homogenizing receiving tank to the first-stage hardness removal reactor through a first static mixer, and injecting a sodium hydroxide solution into the first static mixer at the same time, so that the wastewater is reacted in the first-stage hardness removal reactor;
step three: detecting the calcium ion concentration of the wastewater of the first-stage hardness removal reactor, when the concentration cannot meet the process requirement, transmitting the water obtained in the second step to a second-stage hardness removal and coagulation integrated reactor through a second static mixer, injecting a sodium carbonate solution into the second static mixer, injecting a polyaluminium chloride and polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor in the reaction process of the second-stage hardness removal and coagulation integrated reactor for hardness removal and coagulation treatment, and if the calcium ion concentration of the first-stage hardness removal effluent is less than or equal to 100mg/L, only adding the polyaluminium chloride and the polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor for coagulation treatment;
step four: and (3) enabling the water obtained in the third step to sequentially enter a sedimentation tank, a moderate temperature UASB reactor and a contact oxidation tank for pollutant treatment.
3. The process for reducing the treatment cost of drilling and production wastewater according to claim 2, characterized in that: the pH value of the sodium hydroxide solution added into the first static mixer is 11-13, the pH value of the effluent of the first static mixer is 7-7.5, and the moderate temperature UASB reactor adopts a moderate temperature anaerobic process and stably operates at 30-35 ℃.
4. The process for reducing the treatment cost of drilling and production wastewater according to claim 3, characterized in that: the carbon dioxide absorption tower uses waste water which is added with sodium hydroxide solution and has the pH value of 11-13 as absorption liquid to absorb carbon dioxide gas in flue gas, and carbonate is formed and used for removing calcium hardness from the waste water.
5. The process for reducing the treatment cost of drilling and production wastewater according to claim 4, characterized in that: the gas boiler adopts natural gas as fuel, and simultaneously hot water in the gas boiler is conveyed to the intermediate-temperature UASB reactor.
6. The process for reducing the treatment cost of drilling and production wastewater according to claim 5, characterized in that: the receiving oxidation tank reduces the concentration of organic pollutants and ammonia nitrogen in the wastewater through aerobic contact reaction, and the absorption liquid added by the first-stage hardness removal reactor needs to be quantitatively added.
7. The device for reducing the treatment cost of drilling and production wastewater for the process according to any one of claims 1 to 6, which comprises an absorption device and a reaction treatment device, and is characterized in that: absorbing device includes that gas boiler (1), draught fan (2), carbon dioxide absorption tower (3) and absorption liquid keep in jar (4), and reaction treatment device includes that the homogeneity receives pond (5), one section removes hard reactor (6), two-section and removes hard reactor (7), sedimentation tank (8), medium temperature UASB reactor (9) and receive oxidation pond (10), carbon dioxide absorption tower (3) are including the tower body and spray the board, the inner wall fixedly connected with anticorrosive coating of absorption liquid jar (4) of keeping in, one section removes hard reactor (6) and includes first box and first rabbling mechanism, two-section removes hard reactor (7) and includes second box and second rabbling mechanism, medium temperature UASB reactor (9) include casing, third rabbling mechanism and conveying mechanism.
8. The device for reducing the treatment cost of drilling and production wastewater for the process according to claim 7, is characterized in that: gas boiler (1), draught fan (2), carbon dioxide absorption tower (3) and absorption liquid are kept in storage tank (4) and are linked to each other in proper order, carbon dioxide absorption tower (3) and absorption liquid are kept in storage tank (4) intercommunication and are had circulating pump (11), be provided with third static mixer (12) and fourth static mixer (13) between circulating pump (11) and carbon dioxide absorption tower (3) respectively, one side intercommunication of fourth static mixer (13) has alkali lye to throw and adds pump (14).
9. The device for reducing the treatment cost of drilling and production wastewater for the process according to claim 7, is characterized in that: a first static mixer (15) is arranged between the homogeneous receiving pool (5) and the first-stage hardness removal reactor (6), and a second static mixer (16) is arranged between the first-stage hardness removal reactor (6) and the second-stage hardness removal reactor (7).
10. The device for reducing the treatment cost of drilling and production wastewater for the process according to claim 7, is characterized in that: sedimentation tank (8), medium temperature UASB reactor (9) and receive oxidation pond (10) and link to each other in proper order, the intercommunication has the water pipe between gas boiler (1) and medium temperature UASB reactor (9), absorption liquid is kept in jar (4) and is provided with absorption liquid between one section except that hard reactor (6) and throws with pump (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210691957.XA CN115057582B (en) | 2022-06-19 | 2022-06-19 | Process and device for reducing drilling and production wastewater treatment cost |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210691957.XA CN115057582B (en) | 2022-06-19 | 2022-06-19 | Process and device for reducing drilling and production wastewater treatment cost |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115057582A true CN115057582A (en) | 2022-09-16 |
| CN115057582B CN115057582B (en) | 2024-03-05 |
Family
ID=83202759
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210691957.XA Active CN115057582B (en) | 2022-06-19 | 2022-06-19 | Process and device for reducing drilling and production wastewater treatment cost |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115057582B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201292300Y (en) * | 2008-11-07 | 2009-08-19 | 中国石油天然气集团公司 | Water producing and desalting integrated treatment apparatus for oil field |
| CN103449685A (en) * | 2013-09-26 | 2013-12-18 | 中国海洋石油总公司 | Method for disposing high-salt high-polymer wastewater through Fenton oxidation and biology combined technology |
| CN110028188A (en) * | 2019-05-06 | 2019-07-19 | 徐州工程学院 | A kind of processing method of sea oil drilling and production waste water |
| CN110482587A (en) * | 2019-09-24 | 2019-11-22 | 河南心连心化学工业集团股份有限公司 | A kind of device and recovery method of gasification ash water classification recycling precipitated calcium carbonate |
| CN111875180A (en) * | 2020-08-06 | 2020-11-03 | 清华大学 | Coal chemical industry wastewater zero-discharge integrated treatment system and method |
| CN213506212U (en) * | 2020-08-27 | 2021-06-22 | 山西国际能源裕光煤电有限责任公司 | Wastewater hardness removal device and desulfurization wastewater zero-discharge treatment system |
| CN113582399A (en) * | 2021-08-18 | 2021-11-02 | 陕西金禹科技发展有限公司 | By using waste gas CO2Method for removing hardness |
| CN216336975U (en) * | 2021-10-22 | 2022-04-19 | 青岛太平洋化工装备有限公司 | Alkaline waste water removes hard equipment |
-
2022
- 2022-06-19 CN CN202210691957.XA patent/CN115057582B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201292300Y (en) * | 2008-11-07 | 2009-08-19 | 中国石油天然气集团公司 | Water producing and desalting integrated treatment apparatus for oil field |
| CN103449685A (en) * | 2013-09-26 | 2013-12-18 | 中国海洋石油总公司 | Method for disposing high-salt high-polymer wastewater through Fenton oxidation and biology combined technology |
| CN110028188A (en) * | 2019-05-06 | 2019-07-19 | 徐州工程学院 | A kind of processing method of sea oil drilling and production waste water |
| CN110482587A (en) * | 2019-09-24 | 2019-11-22 | 河南心连心化学工业集团股份有限公司 | A kind of device and recovery method of gasification ash water classification recycling precipitated calcium carbonate |
| CN111875180A (en) * | 2020-08-06 | 2020-11-03 | 清华大学 | Coal chemical industry wastewater zero-discharge integrated treatment system and method |
| CN213506212U (en) * | 2020-08-27 | 2021-06-22 | 山西国际能源裕光煤电有限责任公司 | Wastewater hardness removal device and desulfurization wastewater zero-discharge treatment system |
| CN113582399A (en) * | 2021-08-18 | 2021-11-02 | 陕西金禹科技发展有限公司 | By using waste gas CO2Method for removing hardness |
| CN216336975U (en) * | 2021-10-22 | 2022-04-19 | 青岛太平洋化工装备有限公司 | Alkaline waste water removes hard equipment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115057582B (en) | 2024-03-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107399876B (en) | A kind of processing method of high ammonia-nitrogen wastewater | |
| CN102942973B (en) | Method and system for combined air stripping biogas slurry depth treatment and biogas purification and desulfurization | |
| KR20130003522A (en) | Treatment system for waste water | |
| CN103755096A (en) | Coupled Fenton oxidation and anaerobic digestion reactor for treating surplus sludge | |
| CN105693030B (en) | A kind of bamboo wood carbonized waste water treatment system and method | |
| CN110372143A (en) | Landfill leachate physicochemical deamination pretreatment method and device | |
| CN110304779A (en) | Materialization deamination method and treatment system for anaerobic effluent of landfill leachate | |
| CN206407915U (en) | The device of high-purity ammoniacal liquor is produced from ammonia nitrogen waste water | |
| CN110862182A (en) | Landfill leachate treatment device and method | |
| CN215947043U (en) | DMF wastewater treatment system | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN104150729B (en) | The sludge treating system of a kind of high efficient resourcing and low pollution emission and method | |
| CN115057582A (en) | Process and device for reducing drilling wastewater treatment cost | |
| JP4893647B2 (en) | Method and apparatus for treating water containing organic matter | |
| CN217868418U (en) | Ammonia nitrogen wastewater treatment system | |
| CN207002529U (en) | Pyrazolone production wastewater treatment device | |
| CN205077017U (en) | Biogas biological desulfurization system | |
| CN107188378A (en) | Pyrazolone production wastewater treatment device and its handling process | |
| CN218130999U (en) | Integrative device of tail gas treatment and waste water treatment | |
| CN210656543U (en) | Materialization deamination processing system of landfill leachate anaerobism play water | |
| KR101269379B1 (en) | Treatment method for wastewater | |
| CN203382549U (en) | High-concentration ammonia-nitrogen wastewater treatment device | |
| CN208136037U (en) | A kind of new bio nitrogen fixation process processing high ammonia-nitrogen wastewater complexes | |
| CN106608673B (en) | Method for reducing content of soluble impurities in wastewater by utilizing gas-liquid impact mixing reaction system | |
| CN214735046U (en) | Acid-making wastewater treatment and recovery system applied to activated carbon dry-method flue gas treatment device |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |