CN104628212B - A kind of refinery(waste) water high-efficient treatment method - Google Patents
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- CN104628212B CN104628212B CN201310545170.3A CN201310545170A CN104628212B CN 104628212 B CN104628212 B CN 104628212B CN 201310545170 A CN201310545170 A CN 201310545170A CN 104628212 B CN104628212 B CN 104628212B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 239000002699 waste material Substances 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000011282 treatment Methods 0.000 title claims abstract description 22
- 239000002351 wastewater Substances 0.000 claims abstract description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000000605 extraction Methods 0.000 claims abstract description 26
- 230000001112 coagulating effect Effects 0.000 claims abstract description 22
- 238000005189 flocculation Methods 0.000 claims abstract description 13
- 230000016615 flocculation Effects 0.000 claims abstract description 13
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 11
- 230000003197 catalytic effect Effects 0.000 claims abstract description 11
- 230000003647 oxidation Effects 0.000 claims abstract description 11
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 11
- 238000003860 storage Methods 0.000 claims abstract description 11
- 238000009833 condensation Methods 0.000 claims abstract description 6
- 230000005494 condensation Effects 0.000 claims abstract description 6
- 238000003672 processing method Methods 0.000 claims abstract description 6
- 235000012239 silicon dioxide Nutrition 0.000 claims abstract description 6
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 6
- 238000003756 stirring Methods 0.000 claims abstract description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 32
- 229910021529 ammonia Inorganic materials 0.000 claims description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000005868 electrolysis reaction Methods 0.000 claims description 15
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 10
- 238000001179 sorption measurement Methods 0.000 claims description 10
- 238000004062 sedimentation Methods 0.000 claims description 7
- 238000005188 flotation Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 5
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 3
- 239000010842 industrial wastewater Substances 0.000 abstract description 10
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000010521 absorption reaction Methods 0.000 abstract 2
- WAKTWVHWRCNIKU-UHFFFAOYSA-N S(=O)(=O)(O)O.[AlH3] Chemical compound S(=O)(=O)(O)O.[AlH3] WAKTWVHWRCNIKU-UHFFFAOYSA-N 0.000 abstract 1
- 238000002156 mixing Methods 0.000 abstract 1
- 238000006467 substitution reaction Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 17
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 229920000592 inorganic polymer Polymers 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 239000003513 alkali Substances 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
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Abstract
The invention discloses a kind of refinery(waste) water high-efficient treatment methods, which is characterized in that the processing method after mixing evenly, carries out oil removal processing the following steps are included: (1) terra silicea purificata is added into oil extraction waste water；(2) coagulating basin impeller is opened to carry out after coagulating (3) are filtered to storage pool, sulfuric acid aluminum flocculation (4) are added and pass through catalytic oxidation device, in the case where steam-water ratio 1:20, compressed air stirring (5) low pressure depickling deammoniation tower processing (6) high pressure deammoniation tower is further processed after (7) multistage fractional condensation device is concentrated, pH=3-4 is adjusted, active carbon and iron powder are added, PH=8-9 is adjusted in absorption (8), ultrafiltration, absorption obtains that treated industrial wastewater.After the present invention removes the polluter in waste water to the greatest extent, greatly the middle pressure steam valuable with low-pressure steam substitution more than needed, can be recycled and be utilized to industrial wastewater, have good economy and environmental benefit.
Description
Technical field
The invention belongs to industrial waste water treatments, and in particular to a kind of refinery(waste) water high-efficient treatment method.
Background technique
Refinery(waste) water is mainly formed by oily waste water and containing alkali waste water, and water is in alkalinity, and pH is between 7-8, and oil-containing is in 120-
200mg/L.Carry out refinery(waste) water and be processed into oil field with the research of water filling, the former is only pressed into technical requirements inside refinery, is utilized
Existing utility makees simple pretreatment, then defeated to underground is injected behind oilfield sewage station, with recovered water mixed processing, will both have warp
Ji benefit, and there is social benefit.
With the fast development of oil exploration industry, oil extraction waste water is increasingly severe to the pollution level of ground and underground,
People's lives and living environment are threaten through different degrees of.In current water resource, there is a serious shortage of, the whole society, and energy conservation to be mobilized to subtract
Under the big situation of row, extremely it is unfavorable for making full use of for resource, does not meet the requirement of circular economy.Currently, petroleum wastewater treatment
Technology cannot effectively remove the harmful substance in waste water, and treatment effect is unobvious；Biochemical method oil extraction waste water is individually used,
Since oil extraction waste water temperature is high, variation water quality is big, and containing there are many polymer to the toxic effect of strain, makes
The adaptability of strain is deteriorated, and in addition various oil recovery auxiliary agents are various in style, and oil extraction waste water organic components are complicated, and salt content is high, difficult
To reach target by biochemical treatment.
The present invention on the basis of existing technology, proposes a kind of heat coupled method processing acid gas-containing and ammonia waste water
Steam consumption can be greatly lowered in technical matters.The steam consumption of ton water can be reduced to 140-150kg.In oil refining and coal
Chemical company, since many pressure of by-product are the low-pressure steams of 0.5Mpa or so in production process, thus low-pressure steam is more than needed
It is more, it is forced the purposes as some low values.And the middle pressure steam of 1.0Mpa or more is insufficient.Thus, if proposed a kind of new
Depickling deamination technique, as far as possible using low-pressure steam more than needed, reduce middle pressure steam consumption, for improving Business Economic Benefit,
Promoting industry technology level has greater significance.
Summary of the invention
The object of the present invention is to provide a kind of refinery(waste) water high-efficient treatment methods, and it is poor to solve prior art Biochemical Treatment
The problem of, it realizes the Optimized Matching for using energy demand, can significantly save the consumption of middle pressure steam, and can guarantee and preferably locate
Manage effect.
The technical scheme adopted by the invention is that:
A kind of refinery(waste) water high-efficient treatment method, which is characterized in that the processing method the following steps are included:
(1) 0.5-0.8kg terra silicea purificata is added into oil extraction waste water raw water per ton, is stirred using compressed air paddling process
After uniformly, it is sent into oil separator, carries out oil removal processing；
(2) waste water after oil removal enters coagulating basin, opens coagulating basin impeller and carries out coagulating, reaction time 40-
50min；
(3) inorganic polymer flocculant aluminum sulfate 25-30g/ is added after filtering to storage pool in the waste water after coagulating
L is stirred evenly, the flocculation time 80-100min in reaction tank；
(4) upper clear supernate through flocculation sedimentation is sent into catalytic oxidation device, in the case where steam-water ratio 1:20, compression is empty
Gas agitating, catalytic oxidation 4-5h；
(5) refinery(waste) water is made to be divided to hot and cold two strands to distinguish from the low pressure depickling deammoniation tower top with lateral line withdrawal function and middle and upper part
Into in tower, adjusting low pressure depickling deammoniation tower tower top pressure respectively is 0.2MPa, and 45 DEG C of tower top temperature, tower bottom pressure is
0.22MPa, 120 DEG C of column bottom temperature, after going out sour gas in refinery(waste) water from stripped overhead, into incinerator；
(6) middle and upper part for entering high pressure deammoniation tower by the kettle liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, adjusts control
The tower top pressure of deammoniation tower processed is 0.6Mpa, and tower top temperature is 145 DEG C, tower bottom pressure 0.65Mpa, and column bottom temperature is 165 DEG C；
(7) being concentrated into subsequent multistage fractional condensation device containing ammonia vapor from the overhead extraction of high pressure deammoniation tower
Afterwards, the PH value of water in micro-electrolysis reactor is adjusted with hydrochloric acid, is controlled between 3-4；It is added simultaneously into micro-electrolysis reactor
Active carbon and iron powder adsorb 30-40min；
(8) micro-electrolysis reactor water outlet enter flotation tank, with sodium hydroxide by air bearing pool inner water PH value be adjusted to 8-9 it
Between, then ultrafiltration is carried out, the water after hyperfiltration treatment enters discharge bay after activated carbon adsorption, is handled into activated carbon adsorption tank
Industrial wastewater afterwards.
Above-mentioned step (5) mesolow depickling deammoniation tower makees heat source using the low-pressure steam of 0.6-0.7Mpa.
Above-mentioned step (6) mesohigh deammoniation tower makees heat source using the middle pressure steam of 1.2-1.5Mpa or more.
Active carbon and iron powder dosage are the 0.03-0.05% of waste water total amount in above-mentioned step (7).
It is condensed from the overhead extraction of low pressure deammoniation tower containing ammonia vapor to after 115 DEG C in above-mentioned step (5), into gas-liquid
Gas phase and liquid phase are separated in knockout drum, liquid-phase reflux returns in tower, and gas phase enters second level condenser, is all condensed into weak aqua ammonia
Afterwards, high pressure deammoniation tower is pumped into through storage tank.
Advantageous effect of the invention:
The characteristics of specific surface area of super large of the present invention and easy flocculation sedimentation, the organic matter in oil extraction waste water is adsorbed,
And then under the action of inorganic salts or high polymer coagulant, flocculation sedimentation is effectively carried out, the polluter in waste water is maximum
After the removal of degree, industrial wastewater can be recycled and be utilized, treated, and industrial wastewater can be re-used as recycling water
It uses, has saved water resource, there is good economy and environmental benefit.Acid gas-containing is handled using heat coupled method and ammonia is useless
The technical matters of water can greatly substitute valuable middle pressure steam with low-pressure steam more than needed, and equipment therefor is all
General chemical separation device, mature and reliable, obtaining that treated, industrial wastewater is widely used, can be applied to industrial production
Links in, for promoted industry technology level have greater significance.
Specific embodiment
Embodiment 1
A kind of refinery(waste) water high-efficient treatment method, which is characterized in that the processing method the following steps are included:
(1) 0.5kg terra silicea purificata is added into oil extraction waste water raw water per ton, is stirred evenly using compressed air paddling process
Afterwards, it is sent into oil separator, carries out oil removal processing；
(2) waste water after oil removal enters coagulating basin, opens coagulating basin impeller and carries out coagulating, reaction time 40min；
(3) inorganic polymer flocculant aluminum sulfate 25g/L is added after filtering to storage pool in the waste water after coagulating,
It stirs evenly, the flocculation time 80min in reaction tank；
(4) upper clear supernate through flocculation sedimentation is sent into catalytic oxidation device, in the case where steam-water ratio 1:20, compression is empty
Gas agitating, catalytic oxidation 4h；
(5) refinery(waste) water is made to be divided to hot and cold two strands to distinguish from the low pressure depickling deammoniation tower top with lateral line withdrawal function and middle and upper part
Into in tower, adjusting low pressure depickling deammoniation tower tower top pressure respectively is 0.2MPa, and low pressure depickling deammoniation tower is low using 0.6Mpa's
Pressure steam makees heat source, and 45 DEG C of tower top temperature, tower bottom pressure 0.22MPa, makes the acidity in refinery(waste) water by 120 DEG C of column bottom temperature
After gas goes out from stripped overhead, into incinerator, condense from the overhead extraction of low pressure deammoniation tower containing ammonia vapor to 115 DEG C
Afterwards, into separation gas phase and liquid phase in knockout drum, liquid-phase reflux is returned in tower, and gas phase enters second level condenser, all cold
After congealing into weak aqua ammonia, high pressure deammoniation tower is pumped into through storage tank；
(6) enter the middle and upper part of high pressure deammoniation tower, high pressure-off by the kettle liquid of pump extraction from low pressure depickling deammoniation tower tower reactor
Ammonia tower makees heat source using the middle pressure steam of 1.2Mpa or more, and the tower top pressure for adjusting control deammoniation tower is 0.6Mpa, tower top temperature
It is 145 DEG C, tower bottom pressure 0.65Mpa, column bottom temperature is 165 DEG C；
(7) being concentrated into subsequent multistage fractional condensation device containing ammonia vapor from the overhead extraction of high pressure deammoniation tower
Afterwards, the PH value of water in micro-electrolysis reactor is adjusted with hydrochloric acid, is controlled between 3-4；It is added simultaneously into micro-electrolysis reactor
Active carbon and iron powder, active carbon and iron powder dosage are the 0.03% of waste water total amount, adsorb 30min；
(8) micro-electrolysis reactor water outlet enter flotation tank, with sodium hydroxide by air bearing pool inner water PH value be adjusted to 8-9 it
Between, then ultrafiltration is carried out, the water after hyperfiltration treatment enters discharge bay after activated carbon adsorption, is handled into activated carbon adsorption tank
Industrial wastewater afterwards.
Embodiment 2
A kind of refinery(waste) water high-efficient treatment method, which is characterized in that the processing method the following steps are included:
(1) 0.8kg terra silicea purificata is added into oil extraction waste water raw water per ton, is stirred evenly using compressed air paddling process
Afterwards, it is sent into oil separator, carries out oil removal processing；
(2) waste water after oil removal enters coagulating basin, opens coagulating basin impeller and carries out coagulating, reaction time 50min；
(3) inorganic polymer flocculant aluminum sulfate 30g/L is added after filtering to storage pool in the waste water after coagulating,
It stirs evenly, the flocculation time 100min in reaction tank；
(4) upper clear supernate through flocculation sedimentation is sent into catalytic oxidation device, in the case where steam-water ratio 1:20, compression is empty
Gas agitating, catalytic oxidation 5h；
(5) refinery(waste) water is made to be divided to hot and cold two strands to distinguish from the low pressure depickling deammoniation tower top with lateral line withdrawal function and middle and upper part
Into in tower, adjusting low pressure depickling deammoniation tower tower top pressure respectively is 0.2MPa, and low pressure depickling deammoniation tower is low using 0.7Mpa's
Pressure steam makees heat source, and 45 DEG C of tower top temperature, tower bottom pressure 0.22MPa, makes the acidity in refinery(waste) water by 120 DEG C of column bottom temperature
After gas goes out from stripped overhead, into incinerator, condense from the overhead extraction of low pressure deammoniation tower containing ammonia vapor to 115 DEG C
Afterwards, into separation gas phase and liquid phase in knockout drum, liquid-phase reflux is returned in tower, and gas phase enters second level condenser, all cold
After congealing into weak aqua ammonia, high pressure deammoniation tower is pumped into through storage tank；
(6) enter the middle and upper part of high pressure deammoniation tower, high pressure-off by the kettle liquid of pump extraction from low pressure depickling deammoniation tower tower reactor
Ammonia tower makees heat source using the middle pressure steam of 1.5Mpa or more, and the tower top pressure for adjusting control deammoniation tower is 0.6Mpa, tower top temperature
It is 145 DEG C, tower bottom pressure 0.65Mpa, column bottom temperature is 165 DEG C；
(7) being concentrated into subsequent multistage fractional condensation device containing ammonia vapor from the overhead extraction of high pressure deammoniation tower
Afterwards, the PH value of water in micro-electrolysis reactor is adjusted with hydrochloric acid, is controlled between 3-4；It is added simultaneously into micro-electrolysis reactor
Active carbon and iron powder, active carbon and iron powder dosage are the 0.05% of waste water total amount, adsorb 40min；
(8) micro-electrolysis reactor water outlet enter flotation tank, with sodium hydroxide by air bearing pool inner water PH value be adjusted to 8-9 it
Between, then ultrafiltration is carried out, the water after hyperfiltration treatment enters discharge bay after activated carbon adsorption, is handled into activated carbon adsorption tank
Industrial wastewater afterwards.
Embodiment 3
A kind of refinery(waste) water high-efficient treatment method, which is characterized in that the processing method the following steps are included:
(1) 0.6kg terra silicea purificata is added into oil extraction waste water raw water per ton, is stirred evenly using compressed air paddling process
Afterwards, it is sent into oil separator, carries out oil removal processing；
(2) waste water after oil removal enters coagulating basin, opens coagulating basin impeller and carries out coagulating, reaction time 45min；
(3) inorganic polymer flocculant aluminum sulfate 28g/L is added after filtering to storage pool in the waste water after coagulating,
It stirs evenly, the flocculation time 90min in reaction tank；
(4) upper clear supernate through flocculation sedimentation is sent into catalytic oxidation device, in the case where steam-water ratio 1:20, compression is empty
Gas agitating, catalytic oxidation 4.5h；
(5) refinery(waste) water is made to be divided to hot and cold two strands to distinguish from the low pressure depickling deammoniation tower top with lateral line withdrawal function and middle and upper part
Into in tower, adjusting low pressure depickling deammoniation tower tower top pressure respectively is 0.2MPa, and low pressure depickling deammoniation tower is low using 0.7Mpa's
Pressure steam makees heat source, and 45 DEG C of tower top temperature, tower bottom pressure 0.22MPa, makes the acidity in refinery(waste) water by 120 DEG C of column bottom temperature
After gas goes out from stripped overhead, into incinerator, condense from the overhead extraction of low pressure deammoniation tower containing ammonia vapor to 115 DEG C
Afterwards, into separation gas phase and liquid phase in knockout drum, liquid-phase reflux is returned in tower, and gas phase enters second level condenser, all cold
After congealing into weak aqua ammonia, high pressure deammoniation tower is pumped into through storage tank；
(6) enter the middle and upper part of high pressure deammoniation tower, high pressure-off by the kettle liquid of pump extraction from low pressure depickling deammoniation tower tower reactor
Ammonia tower makees heat source using the middle pressure steam of 1.3Mpa or more, and the tower top pressure for adjusting control deammoniation tower is 0.6Mpa, tower top temperature
It is 145 DEG C, tower bottom pressure 0.65Mpa, column bottom temperature is 165 DEG C；
(7) being concentrated into subsequent multistage fractional condensation device containing ammonia vapor from the overhead extraction of high pressure deammoniation tower
Afterwards, the PH value of water in micro-electrolysis reactor is adjusted with hydrochloric acid, is controlled between 3-4；It is added simultaneously into micro-electrolysis reactor
Active carbon and iron powder, active carbon and iron powder dosage are the 0.05% of waste water total amount, adsorb 35min；
(8) micro-electrolysis reactor water outlet enter flotation tank, with sodium hydroxide by air bearing pool inner water PH value be adjusted to 8-9 it
Between, then ultrafiltration is carried out, the water after hyperfiltration treatment enters discharge bay after activated carbon adsorption, is handled into activated carbon adsorption tank
Industrial wastewater afterwards.
The residual quantity of its treated waste water hydrogen sulfide and carbon dioxide is far below 50mg/L, and ammon amount 45mg/L meets
Required standard.
By 25 yuan of low-pressure steam price per ton, 120 yuan of 1.5Mpa steam price calculating, using the present invention to waste water at
Reason, the steam cost of ton water is only 5.7 yuan, and to take original technique, and the steam cost of ton water is about 15-22 member.Benefit is non-
Chang Xianzhu.
Claims (5)
1. a kind of refinery(waste) water high-efficient treatment method, which is characterized in that the processing method the following steps are included:
(1) 0.5-0.8kg terra silicea purificata is added into oil extraction waste water raw water per ton, is stirred evenly using compressed air paddling process
Afterwards, it is sent into oil separator, carries out oil removal processing；
(2) waste water after oil removal enters coagulating basin, opens coagulating basin impeller and carries out coagulating, reaction time 40-50min；
(3) waste water after coagulating is added flocculant aluminum sulfate 25-30g/L, stirs evenly after filtering to storage pool,
Flocculation time 80-100min in reaction tank；
(4) upper clear supernate through flocculation sedimentation is sent into catalytic oxidation device, in the case where steam-water ratio 1:20, compressed air is stirred
It mixes, catalytic oxidation 4-5h；
(5) refinery(waste) water is made to be divided to hot and cold two strands to respectively enter from the low pressure depickling deammoniation tower top with lateral line withdrawal function and middle and upper part
In tower, respectively adjust low pressure depickling deammoniation tower tower top pressure be 0.2MPa, 45 DEG C of tower top temperature, tower bottom pressure 0.22MPa, tower
120 DEG C of bottom temperature, after going out sour gas in refinery(waste) water from stripped overhead, into incinerator；
(6) middle and upper part for entering high pressure deammoniation tower by the kettle liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, it is de- to adjust control
The tower top pressure of ammonia tower is 0.6MPa, and tower top temperature is 145 DEG C, tower bottom pressure 0.65MPa, and column bottom temperature is 165 DEG C；
(7) enter from the overhead extraction of high pressure deammoniation tower containing ammonia vapor after subsequent multistage fractional condensation device is concentrated, use
Hydrochloric acid adjusts the pH value of water in micro-electrolysis reactor, controls between 3-4；Simultaneously into micro-electrolysis reactor add active carbon and
Iron powder adsorbs 30-40min；
(8) micro-electrolysis reactor water outlet enters flotation tank, and water ph value in flotation tank is adjusted between 8-9 with sodium hydroxide, then into
Row ultrafiltration, the water after hyperfiltration treatment enter activated carbon adsorption tank, and discharge bay is entered after activated carbon adsorption, the work that obtains that treated
Industry waste water.
2. a kind of refinery(waste) water high-efficient treatment method according to claim 1, which is characterized in that in the step (5)
Low pressure depickling deammoniation tower makees heat source using the low-pressure steam of 0.6-0.7MPa.
3. a kind of refinery(waste) water high-efficient treatment method according to claim 1, which is characterized in that in the step (6)
High pressure deammoniation tower makees heat source using the middle pressure steam of 1.2-1.5MPa.
4. a kind of refinery(waste) water high-efficient treatment method according to claim 1, which is characterized in that in the step (7)
Active carbon and iron powder dosage are the 0.03-0.05% of waste water total amount.
5. a kind of refinery(waste) water high-efficient treatment method according to claim 1, which is characterized in that in the step (5)
It condenses from the overhead extraction of low pressure deammoniation tower containing ammonia vapor to after 115 DEG C, into separating gas phase and liquid phase in knockout drum,
Liquid-phase reflux returns in tower, and gas phase enters second level condenser, after being all condensed into weak aqua ammonia, is pumped into high pressure deammoniation tower through storage tank.
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