CN115057582B - Process and device for reducing drilling and production wastewater treatment cost - Google Patents
Process and device for reducing drilling and production wastewater treatment cost Download PDFInfo
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- CN115057582B CN115057582B CN202210691957.XA CN202210691957A CN115057582B CN 115057582 B CN115057582 B CN 115057582B CN 202210691957 A CN202210691957 A CN 202210691957A CN 115057582 B CN115057582 B CN 115057582B
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- 238000000034 method Methods 0.000 title claims abstract description 57
- 230000008569 process Effects 0.000 title claims abstract description 55
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 32
- 238000005553 drilling Methods 0.000 title claims abstract description 22
- 238000004519 manufacturing process 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 100
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 50
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 50
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 47
- 239000002351 wastewater Substances 0.000 claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003546 flue gas Substances 0.000 claims abstract description 18
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 16
- 239000003513 alkali Substances 0.000 claims abstract description 15
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 12
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 8
- 230000003068 static effect Effects 0.000 claims description 42
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 230000015271 coagulation Effects 0.000 claims description 20
- 238000005345 coagulation Methods 0.000 claims description 20
- 230000003647 oxidation Effects 0.000 claims description 17
- 238000007254 oxidation reaction Methods 0.000 claims description 17
- 238000004062 sedimentation Methods 0.000 claims description 16
- 230000007246 mechanism Effects 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- 229920002401 polyacrylamide Polymers 0.000 claims description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 7
- 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
- 239000000446 fuel Substances 0.000 claims description 3
- 239000002957 persistent organic pollutant Substances 0.000 claims description 3
- 239000011248 coating agent Substances 0.000 claims description 2
- 238000000576 coating method Methods 0.000 claims description 2
- 239000007921 spray Substances 0.000 claims description 2
- 239000000779 smoke Substances 0.000 abstract description 4
- 239000002253 acid Substances 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 239000005431 greenhouse gas Substances 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 22
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 238000010586 diagram 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
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000005273 aeration 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
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 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
-
- 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
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- 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 drilling and production wastewater treatment cost, which 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 treatment and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogeneous receiving pool and a section of hard removal treatment. According to the invention, the sodium hydroxide solution is adopted to absorb carbon dioxide in the flue gas of the medium-temperature anaerobic heating system to form the sodium carbonate solution, meanwhile, the pH value of the wastewater treatment process is conveniently controlled by the pH automatic control system, the alkali consumption and the acid consumption for adjusting back the pH value are reduced, the process is used for carrying out the hardness removal treatment of the drilling and production wastewater with high calcium ion concentration, on one hand, the wastewater treatment operation cost is reduced, the emission of greenhouse gases is reduced, and meanwhile, the system adopts a two-stage hardness removal mode, so that the requirement of wastewater hardness removal when the smoke volume in high-temperature seasons is insufficient can be made up.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a process and a device for reducing drilling and production wastewater treatment cost.
Background
The wastewater treatment is to treat wastewater by using physical, chemical and biological methods, so that the wastewater is purified, pollution is reduced, so that the wastewater is recovered and reused, water resources are fully utilized, the generated wastewater is required to be treated in the drilling and production process of petroleum and natural gas, and the existing drilling and production wastewater treatment equipment has certain defects: 1. the content of calcium ions in drilling and production wastewater is high, and when the hardness of the wastewater is removed by using 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 and production wastewater, which have the advantage of low treatment cost and solve the problem of high treatment cost of the existing drilling and production wastewater treatment equipment.
In order to achieve the above purpose, the present invention provides the following technical solutions: the process for reducing the drilling and production wastewater treatment cost 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 treatment and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogeneous receiving tank, a primary hard removal treatment, a secondary hard removal treatment, a sedimentation tank, a medium-temperature UASB treatment and a receiving oxidation tank.
The specific treatment process comprises the following steps:
step one: sucking the flue gas generated by the gas boiler into a carbon dioxide absorption tower through a draught fan, then adding alkali liquor into the carbon dioxide absorption tower through an alkali liquor adding pump, and simultaneously enabling the absorption liquor in the absorption liquor temporary storage tank to continuously absorb carbon dioxide in the flue gas through a circulating pump;
step two: adding the absorption liquid into a first-stage hardness removal reactor through an absorption liquid adding pump, then conveying water in a homogeneous receiving pool to the first-stage hardness removal reactor through a first static mixer, and simultaneously injecting sodium hydroxide solution into the first static mixer, so that wastewater reacts in the first-stage hardness removal reactor;
step three: detecting the concentration of calcium ions in wastewater of the first-stage hardness removal reactor, transmitting the water obtained in the second step to a second-stage hardness removal and coagulation integrated reactor through a second static mixer when the concentration cannot meet the process requirement, injecting sodium carbonate solution into the second static mixer, injecting 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 performing hardness removal and coagulation treatment, and adding polyaluminium chloride and polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor for performing coagulation treatment if the concentration of calcium ions in the water discharged from the first-stage hardness removal is less than or equal to 100 mg/L;
step four: and (3) enabling the water obtained in the step three to sequentially enter a sedimentation tank, a medium-temperature UASB reactor and a contact oxidation tank 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, the medium-temperature UASB reactor adopts a medium-temperature anaerobic process, and the operation is stable at 30-35 ℃.
Preferably, the carbon dioxide absorption tower uses waste water with pH value of 11-13 adjusted by adding sodium hydroxide solution as absorption liquid to absorb carbon dioxide gas in flue gas, so as to form carbonate for removing calcium in the waste water.
Preferably, the gas boiler uses natural gas as fuel, and hot water in the gas boiler is conveyed to the medium-temperature UASB reactor.
Preferably, the receiving oxidation pond reduces the concentration of organic pollutants and ammonia nitrogen in the wastewater through aerobic contact reaction, and the absorption liquid added into the first-stage hardness removal reactor needs to be quantitatively added.
The utility model provides a reduce device of drilling wastewater treatment cost, includes absorbing device and reaction treatment device, its characterized in that: the absorption device comprises a gas boiler, an induced draft fan, a carbon dioxide absorption tower and an absorption liquid temporary storage tank, wherein the reaction treatment device comprises a homogenizing receiving tank, a first-stage hardness removal reactor, a second-stage hardness removal reactor, a sedimentation tank, a medium-temperature UASB reactor and a receiving oxidation tank, the carbon dioxide absorption tower comprises a tower body and a spraying plate, the inner wall of the absorption liquid temporary storage tank is fixedly connected with an anti-corrosion layer, the first-stage hardness removal reactor comprises a first box body and a first stirring mechanism, the second-stage hardness removal reactor comprises a second box body and a second stirring mechanism, and the medium-temperature UASB reactor comprises a shell, a third stirring mechanism and a conveying mechanism.
Preferably, the gas boiler, the induced draft fan, the carbon dioxide absorption tower and the absorption liquid temporary storage tank are sequentially connected, the carbon dioxide absorption tower and the absorption liquid temporary storage tank are communicated with a circulating pump, a third static mixer and a fourth static mixer are respectively arranged between the circulating pump and the carbon dioxide absorption tower, and one side of the fourth static mixer is communicated with an alkali liquor feeding pump.
Preferably, a first static mixer is arranged between the homogenizing receiving pool and the primary hardness removal reactor, and a second static mixer is arranged between the primary hardness removal reactor and the secondary hardness removal reactor.
Preferably, the sedimentation tank, the medium-temperature UASB reactor and the receiving oxidation tank are connected in sequence, a water pipe is communicated between the gas boiler and the medium-temperature UASB reactor, and an absorption liquid feeding pump is arranged between the absorption liquid temporary storage tank and the first-stage hardness removal reactor.
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 carbon dioxide in the flue gas of the medium-temperature anaerobic heating system to form the sodium carbonate solution, meanwhile, the pH value of the wastewater treatment process is conveniently controlled by the pH automatic control system, the alkali consumption and the acid consumption for adjusting back the pH value are reduced, the process is used for carrying out the hardness removal treatment of the drilling and production wastewater with high calcium ion concentration, on one hand, the wastewater treatment operation cost is reduced, the emission of greenhouse gases is reduced, and meanwhile, the system adopts a two-stage hardness removal mode, so that the requirement of wastewater hardness removal when the smoke volume in high-temperature seasons is insufficient can be made up.
2. The invention can compress the flue gas of the gas-fired boiler by arranging the induced air blower, convey the flue gas to the carbon dioxide absorption tower, provide absorption reaction power, facilitate the recycling of the absorption liquid by arranging the circulating pump, facilitate the injection of the alkaline liquid into the fourth static mixer by arranging the alkaline liquid feeding pump, and facilitate the injection of the absorption liquid into the first-stage hardness removal reactor by arranging the absorption liquid feeding pump.
Drawings
FIG. 1 is a schematic diagram 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 absorber of the present invention;
FIG. 4 is a schematic view in partial cross-section of an absorbent temporary storage tank of the present invention;
FIG. 5 is a schematic cross-sectional view of a one-stage hardness removal reactor according to the present invention;
FIG. 6 is a schematic cross-sectional view of a two-stage hardness removal reactor according to the present invention;
FIG. 7 is a schematic cross-sectional view of a medium temperature UASB reactor according to the invention.
In the figure: 1. a gas-fired boiler; 2. an induced draft fan; 3. a carbon dioxide absorption tower; 4. an absorption liquid temporary storage tank; 5. a homogenizing receiving pool; 6. a first-stage hardness removal reactor; 7. a two-stage hardness removal reactor; 8. a sedimentation tank; 9. a medium temperature UASB reactor; 10. receiving an oxidation pond; 11. a circulation pump; 12. a third static mixer; 13. a fourth static mixer; 14. adding alkali liquor into a pump; 15. a first static mixer; 16. a second static mixer; 17. and adding a pump into the absorption liquid.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Referring to fig. 1-7, a process for reducing drilling and production wastewater treatment cost includes a wastewater treatment process, wherein the wastewater treatment process includes an absorption treatment process and a reaction treatment process, the absorption treatment process adopts a carbon dioxide absorption tower treatment and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogeneous receiving tank, a primary hard removal treatment, a secondary hard removal treatment, a sedimentation tank, a medium-temperature UASB treatment and a receiving oxidation tank.
The specific treatment process comprises the following steps:
step one: sucking the flue gas generated by the gas boiler into a carbon dioxide absorption tower through a draught fan, then adding alkali liquor into the carbon dioxide absorption tower through an alkali liquor adding pump, and simultaneously enabling the absorption liquor in the absorption liquor temporary storage tank to continuously absorb carbon dioxide in the flue gas through a circulating pump;
step two: adding the absorption liquid into a first-stage hardness removal reactor through an absorption liquid adding pump, then conveying water in a homogeneous receiving pool to the first-stage hardness removal reactor through a first static mixer, and simultaneously injecting sodium hydroxide solution into the first static mixer, so that wastewater reacts in the first-stage hardness removal reactor;
step three: detecting the concentration of calcium ions in wastewater of the first-stage hardness removal reactor, transmitting the water obtained in the second step to a second-stage hardness removal and coagulation integrated reactor through a second static mixer when the concentration cannot meet the process requirement, injecting sodium carbonate solution into the second static mixer, injecting 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 performing hardness removal and coagulation treatment, and adding polyaluminium chloride and polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor for performing coagulation treatment if the concentration of calcium ions in the water discharged from the first-stage hardness removal is less than or equal to 100 mg/L;
step four: and (3) sequentially feeding water obtained in the step (III) into a sedimentation tank, an intermediate-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 effluent of the first static mixer is 7-7.5, the intermediate-temperature UASB reactor adopts an intermediate-temperature anaerobic process, the operation is stabilized at 30-35 ℃, a carbon dioxide absorption tower is used for absorbing carbon dioxide gas in flue gas by taking waste water with pH value of 11-13 adjusted by adding the sodium hydroxide solution as absorption liquid, carbonate is formed and is used for removing calcium hardness of the waste water, a gas boiler is used for taking natural gas as fuel, meanwhile, hot water in the gas boiler is conveyed to the intermediate-temperature UASB reactor, the concentration of organic pollutants and ammonia nitrogen in the waste water is reduced by aerobic contact reaction of the receiving oxidation tank, and the absorption liquid fed by the first-stage hardness removal reactor needs quantitative feeding.
The utility model provides a reduce device of drilling wastewater treatment cost, includes absorbing device and reaction treatment device, 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 homogenizing receiving tank 5, a first-stage hardness removal reactor 6, a second-stage hardness 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 hardness removal reactor 6 comprises a first box body and a first stirring mechanism, the second-stage hardness 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, one side of the fourth static mixer 13 is communicated with an alkali liquor adding pump 14, a first static mixer 15 is arranged between the homogenizing receiving tank 5 and the first-section hardness removal reactor 6, a second static mixer 16 is arranged between the first-section hardness removal reactor 6 and the second-section hardness removal reactor 7, the sedimentation tank 8, the middle-temperature UASB reactor 9 and the receiving oxidation tank 10 are sequentially connected, a water pipe is communicated between the gas boiler 1 and the middle-temperature UASB reactor 9, an absorption liquor adding pump 17 is arranged between the absorption liquor temporary storage tank 4 and the first-section hardness removal reactor 6, the smoke of the gas boiler 1 can be compressed by arranging the induced draft fan 2, the smoke is conveyed to the carbon dioxide absorption tower 3, absorption reaction power is provided, the recycling of the absorption liquor can be facilitated by arranging the circulating pump 11, the alkali liquor adding pump 14 is arranged, the method can conveniently inject alkali liquor into the fourth static mixer 13, and can conveniently inject the absorption liquor into the one-stage hardness removal reactor 6 by arranging the absorption liquor adding pump 17, and can simultaneously improve the absorption rate of carbon dioxide by adopting a sodium hydroxide solution to absorb carbon dioxide in flue gas of the medium-temperature anaerobic heating system, and simultaneously improve the absorption rate of the carbon dioxide by a pH automatic control system, and simultaneously facilitate the control of pH value of a wastewater treatment flow, reduce the acid consumption of alkali and a pH value of the wastewater, and perform the hardness removal treatment of high calcium ion concentration drilling and mining wastewater by using the process.
The processing method provided by the invention is adopted for processing: the flue gas generated by the gas boiler 1 is pumped by a draught fan 2, is blown out by a perforated aeration pipe arranged at the bottom of a carbon dioxide absorption tower 3 and contacts with absorption liquid in the absorption tower, carbon dioxide in the flue gas is absorbed by the absorption liquid, the absorption liquid used in the process is sedimentation tank 8 effluent water with pH value adjusted to 11-13 by adding sodium hydroxide solution, the absorption liquid continuously absorbs carbon dioxide in the flue gas by circulating pump 11, a fourth static mixer 13 is arranged on a water inlet pipe of the carbon dioxide absorption tower 3, a pH value detection and control system is arranged at the outlet end of the fourth static mixer 13, a metering pump is controlled to add sodium hydroxide solution to a first static mixer 15 by pH value data detected on line, waste water in the absorption tower is controlled to always keep pH value 11-13, the absorption liquid which fully absorbs carbon dioxide is added into a section of hardness removal reactor 6 by the metering pump, when the liquid level of the absorption liquid temporary storage tank 4 is lower than a set value, supplementing water to a carbon dioxide absorption device from a sedimentation tank 8 through a metering pump, adding a sodium hydroxide solution to adjust the pH value of waste water 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 waste water of the first-stage hardness removal reactor 6, adding a sodium carbonate solution in a second-stage hardness removal stage if the hardness removal capacity of the absorption liquid cannot meet the process requirement, simultaneously adding a polyaluminium chloride and a polyacrylamide solution 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 an aluminum chloride and a polyacrylamide solution in the first-stage hardness removal reactor 7 for coagulation treatment, and sequentially feeding the effluent of the second-stage hardness removal reactor 7 into 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 understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. The process for reducing the drilling and production wastewater treatment cost 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 treatment and an absorption liquid temporary storage tank, and the reaction treatment process adopts a homogeneous receiving tank, a primary hard removal treatment, a secondary hard removal treatment, a sedimentation tank, a medium-temperature UASB treatment and a receiving oxidation tank;
the wastewater treatment process comprises the following steps:
step one: sucking the flue gas generated by the gas boiler into a carbon dioxide absorption tower through a draught fan, then adding alkali liquor into the carbon dioxide absorption tower through an alkali liquor adding pump, and simultaneously enabling the absorption liquor in the absorption liquor temporary storage tank to continuously absorb carbon dioxide in the flue gas through a circulating pump;
step two: adding the absorption liquid into a first-stage hardness removal reactor through an absorption liquid adding pump, then conveying water in a homogeneous receiving pool to the first-stage hardness removal reactor through a first static mixer, and simultaneously injecting sodium hydroxide solution into the first static mixer, so that wastewater reacts in the first-stage hardness removal reactor;
step three: detecting the concentration of calcium ions in wastewater of the first-stage hardness removal reactor, transmitting the water obtained in the second step to a second-stage hardness removal and coagulation integrated reactor through a second static mixer when the concentration cannot meet the process requirement, injecting sodium carbonate solution into the second static mixer, injecting 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 performing hardness removal and coagulation treatment, and adding polyaluminium chloride and polyacrylamide solution into the second-stage hardness removal and coagulation integrated reactor for performing coagulation treatment if the concentration of calcium ions in the water discharged from the first-stage hardness removal is less than or equal to 100 mg/L;
step four: 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;
the carbon dioxide absorption tower is used for absorbing carbon dioxide gas in the flue gas by a waste water absorption liquid with pH value of 11-13 adjusted by adding sodium hydroxide solution, so that carbonate is formed for removing calcium in the waste water;
the receiving oxidation pond reduces the concentration of organic pollutants and ammonia nitrogen in the wastewater through aerobic contact reaction, and the absorption liquid added in the first-stage hardness removal reactor needs to be quantitatively added.
2. The process for reducing the cost of drilling and production wastewater treatment according to claim 1, wherein the process comprises the following steps: 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, the medium-temperature UASB reactor adopts a medium-temperature anaerobic process, and the operation is stabilized at 30-35 ℃.
3. The process for reducing the cost of drilling and production wastewater treatment according to claim 2, wherein: the gas boiler adopts natural gas as fuel, and hot water in the gas boiler is conveyed to the medium-temperature UASB reactor.
4. A process unit for reducing the cost of drilling and production wastewater treatment according to any one of claims 1-3, comprising an absorption unit and a reaction treatment unit, 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 homogenizing receiving tank (5), a first-stage hardness removal reactor (6), a second-stage hardness 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 hardness removal reactor (6) comprises a first box body and a first stirring mechanism, the second-stage hardness removal reactor (7) comprises a second box body and a second stirring mechanism, and the medium-temperature UASB reactor (9) comprises a shell, a third stirring mechanism and a conveying mechanism;
the gas boiler is characterized in that 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), and one side of the fourth static mixer (13) is communicated with an alkali liquor feeding pump (14).
5. The process device for reducing the cost of drilling and production wastewater treatment according to claim 4, wherein: a first static mixer (15) is arranged between the homogenizing receiving pool (5) and the primary hardness removal reactor (6), and a second static mixer (16) is arranged between the primary hardness removal reactor (6) and the secondary hardness removal reactor (7).
6. The process device for reducing the cost of drilling and production wastewater treatment according to claim 5, wherein: sedimentation tank (8), medium temperature UASB reactor (9) and receive oxidation pond (10) link to each other in proper order, the intercommunication has the water pipe between gas boiler (1) and medium temperature UASB reactor (9), be provided with absorption liquid between absorption liquid temporary storage tank (4) and the one section except that hard reactor (6) and throw pump (17).
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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 |
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