CN104628212A - High-efficiency treatment method for oil refining wastewater - Google Patents
High-efficiency treatment method for oil refining wastewater Download PDFInfo
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- CN104628212A CN104628212A CN201310545170.3A CN201310545170A CN104628212A CN 104628212 A CN104628212 A CN 104628212A CN 201310545170 A CN201310545170 A CN 201310545170A CN 104628212 A CN104628212 A CN 104628212A
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- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000002351 wastewater Substances 0.000 title claims abstract description 37
- 238000011282 treatment Methods 0.000 title claims abstract description 26
- 238000007670 refining Methods 0.000 title abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 66
- 238000000605 extraction Methods 0.000 claims abstract description 26
- 238000003756 stirring Methods 0.000 claims abstract description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000005345 coagulation Methods 0.000 claims abstract description 12
- 230000015271 coagulation Effects 0.000 claims abstract description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 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
- 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 abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims abstract description 6
- 238000009833 condensation Methods 0.000 claims abstract description 6
- 230000005494 condensation Effects 0.000 claims abstract description 6
- 238000001914 filtration Methods 0.000 claims abstract description 6
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 36
- 229910021529 ammonia Inorganic materials 0.000 claims description 18
- 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
- 238000005189 flocculation Methods 0.000 claims description 12
- 230000016615 flocculation Effects 0.000 claims description 12
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 10
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 230000003197 catalytic effect Effects 0.000 claims description 10
- 230000001112 coagulating effect Effects 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 10
- 239000013049 sediment Substances 0.000 claims description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 6
- 239000003610 charcoal Substances 0.000 claims description 5
- 238000005188 flotation Methods 0.000 claims description 5
- 229920000592 inorganic polymer Polymers 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 235000012239 silicon dioxide Nutrition 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 5
- 230000009615 deamination Effects 0.000 abstract description 3
- 238000006481 deamination reaction Methods 0.000 abstract description 3
- 239000010842 industrial wastewater Substances 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- 239000003344 environmental pollutant Substances 0.000 abstract 1
- 230000003311 flocculating effect Effects 0.000 abstract 1
- 231100000719 pollutant Toxicity 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000001580 bacterial effect Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000011284 combination treatment Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 235000019600 saltiness Nutrition 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
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Abstract
The invention discloses a high-efficiency treatment method for oil refining wastewater, and is characterized in that the treatment method comprises the following steps: (1) adding refined diatomite into oil extraction wastewater, stirring evenly, and then carrying out oil separation treatment; (2) starting a plug-flow device of a coagulation pool, and carrying out a coagulation reaction; (3) after filtering, sending to a storage pool, adding aluminum sulfate, and flocculating; (4) through a contact oxidation device, under a condition of the steam-water ratio of 1:20, compressing air and stirring; (5) treating with a low-pressure deacidification deamination tower; (6) further treating with a high-pressure deamination tower; (7) after concentrating with a multistage fractional condensation device, adjusting the pH to 3-4, adding activated carbon and an iron powder, and adsorbing; and (8) adjusting the pH to 8-9, carrying out ultrafiltration, and adsorbing to obtain treated industrial wastewater. After pollutants in the wastewater are removed to the greatest extent, extra low-pressure steam is relatively greatly used for replacing valuable medium-pressure steam, the industrial wastewater can be recycled and used, and the method has good economic and environmental benefits.
Description
Technical field
The invention belongs to industrial waste water treatment, be specifically related to a kind of refinery water high-efficient treatment method.
Background technology
Refinery water mainly contains oily(waste)water and containing alkali waste water composition, water is in alkalescence, and pH is between 7-8, and oil-containing is at 120-200mg/L.Carry out refinery water and be processed into the research of oil field with water filling, the former is only pressed technical requirements in inside, refinery, utilizes existing utility to do simple pre-treatment, then oilfield sewage station is passed to, inject underground with after recovered water combination treatment, both will have economic benefit, and again there is social benefit.
Along with the fast development of oil exploration industry, oil extraction waste water on the ground and the pollution level of underground more and more serious, the life that threaten people in various degree and living environment.Under current water resources famine, the whole society mobilize the large situation of energy-saving and emission-reduction, be extremely unfavorable for making full use of of resource, do not meet the requirement of recycling economy.At present, the Treatment Techniques of Petroleum Wastewater effectively can not remove the objectionable impurities in waste water, and treatment effect is not obvious; Independent employing Biochemical method oil extraction waste water, because oil extraction waste water temperature is high, variation water quality is large, and containing many polymers to the toxic effect of bacterial classification, the adaptability of bacterial classification is deteriorated, and various oil recovery auxiliary agent is various in style in addition, and oil extraction waste water organic components is complicated, saltiness is high, is difficult to reach re-set target by biochemical treatment.
The present invention on the basis of existing technology, proposes the technical matters of a kind of thermal coupling method process acid gas-containing and ammonia waste water, significantly can reduce steam consumption.The steam consumption of ton water can be reduced to 140-150kg.In oil refining and coal chemical industry enterprises, due to by-product in production process, a lot of pressure is the low-pressure steam of about 0.5Mpa, and thus low-pressure steam is had more than needed more, is forced to the purposes being used as some low values.And the middle pressure steam of more than 1.0Mpa is not enough.Thus, if propose a kind of new depickling deamination technique, adopt low-pressure steam more than needed as far as possible, reduce middle pressure steam consumption, for improving Business Economic Benefit, promoting industry technology level and there is greater significance.
Summary of the invention
The object of this invention is to provide a kind of refinery water high-efficient treatment method, solve the problem of prior art Biochemical Treatment difference, realize, with the Optimized Matching of energy demand, significantly to save the consumption of middle pressure steam, and preferably treatment effect being ensured.
The technical solution adopted in the present invention is:
A kind of refinery water high-efficient treatment method, it is characterized in that, described treatment process comprises the following steps:
(1) in oil extraction waste water former water per ton, add 0.5-0.8kg terra silicea purificata, after adopting pressurized air paddling process to stir, send into oil trap, carry out oil removal process;
(2) waste water after oil removal enters coagulation basin, opens coagulation basin impeller and carries out coagulating, reaction times 40-50min;
(3) waste water after coagulating, after filtering to storage pool, adds inorganic polymer flocculant Tai-Ace S 150 25-30g/L, stirs, flocculation time 80-100min in reaction tank;
(4) upper clear supernate through flocculation sediment is sent into catalytic oxidation device, when steam-water ratio 1:20, pressurized air stirs, catalytic oxidation 4-5h;
(5) refinery water is made to divide hot and cold two bursts of low pressure depickling deammoniation tower tops from band lateral line withdrawal function and middle and upper part to enter respectively in tower, low pressure depickling deammoniation tower tower top pressure is regulated to be 0.2MPa respectively, tower top temperature 45 DEG C, tower bottom pressure is 0.22MPa, column bottom temperature 120 DEG C, after sour gas in refinery water is gone out from stripped overhead, enter incinerator;
(6) entered the middle and upper part of high pressure deammoniation tower by the still liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, the tower top pressure of regulable control deammoniation tower is 0.6Mpa, and tower top temperature is 145 DEG C, and tower bottom pressure is 0.65Mpa, and column bottom temperature is 165 DEG C;
(7) from the overhead extraction of high pressure deammoniation tower containing ammonia vapor enter follow-up multistage fractional condensation device carry out concentrated after, regulate the PH value of water in micro-electrolysis reactor with hydrochloric acid, control between 3-4; In micro-electrolysis reactor, add gac and iron powder, absorption 30-40min simultaneously;
(8) micro-electrolysis reactor water outlet enters air flotation pool, and air supporting pool inner water PH value be adjusted between 8-9 with sodium hydroxide, then carry out ultrafiltration, the water after uf processing enters activated carbon adsorption tank, after charcoal absorption, enter outlet sump, obtains the trade effluent after processing.
Above-mentioned step (5) mesolow depickling deammoniation tower adopts the low-pressure steam of 0.6-0.7Mpa to make thermal source.
Above-mentioned step (6) mesohigh deammoniation tower adopts the middle pressure steam of more than 1.2-1.5Mpa to make thermal source.
In above-mentioned step (7), gac and iron powder consumption are the 0.03-0.05% of waste water total amount.
After being condensed to 115 DEG C from the overhead extraction of low pressure deammoniation tower containing ammonia vapor in above-mentioned step (5), enter in knockout drum and be separated gas phase and liquid phase, liquid-phase reflux returns in tower, and gas phase enters second stage condenser, after being all condensed into weak ammonia, pump into high pressure deammoniation tower through storage tank.
The beneficial effect of the invention:
The specific surface area of super large of the present invention and the feature of easy flocculation sediment, organism in oil extraction waste water is adsorbed, and then under the effect of inorganic salt or polymeric flocculant, effectively carry out flocculation sediment, after farthest being removed by pollution substance in waste water, can reclaim trade effluent and utilize, the trade effluent after process can use as recovery water again, save water resources, there is good economy and environment benefit.Adopt the technical matters of thermal coupling method process acid gas-containing and ammonia waste water, valuable middle pressure steam can be substituted greatly by low-pressure steam more than needed, and equipment therefor is all general chemical separation device, mature and reliable, trade effluent after the process obtained is of many uses, can be applied in industrial links, for lifting industry technology level, there is greater significance.
Embodiment
Embodiment 1
A kind of refinery water high-efficient treatment method, it is characterized in that, described treatment process comprises the following steps:
(1) in oil extraction waste water former water per ton, add 0.5kg terra silicea purificata, after adopting pressurized air paddling process to stir, send into oil trap, carry out oil removal process;
(2) waste water after oil removal enters coagulation basin, opens coagulation basin impeller and carries out coagulating, reaction times 40min;
(3) waste water after coagulating, after filtering to storage pool, adds inorganic polymer flocculant Tai-Ace S 150 25g/L, stirs, flocculation time 80min in reaction tank;
(4) upper clear supernate through flocculation sediment is sent into catalytic oxidation device, when steam-water ratio 1:20, pressurized air stirs, catalytic oxidation 4h;
(5) refinery water is divided cold, heat two strands enters in tower respectively from the low pressure depickling deammoniation tower top and middle and upper part of being with lateral line withdrawal function, low pressure depickling deammoniation tower tower top pressure is regulated to be 0.2MPa respectively, low pressure depickling deammoniation tower adopts the low-pressure steam of 0.6Mpa to make thermal source, tower top temperature 45 DEG C, tower bottom pressure is 0.22MPa, column bottom temperature 120 DEG C, after sour gas in refinery water is gone out from stripped overhead, enter incinerator, after being condensed to 115 DEG C from the overhead extraction of low pressure deammoniation tower containing ammonia vapor, enter in knockout drum and be separated gas phase and liquid phase, liquid-phase reflux returns in tower, gas phase enters second stage condenser, after being all condensed into weak ammonia, high pressure deammoniation tower is pumped into through storage tank,
(6) entered the middle and upper part of high pressure deammoniation tower by the still liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, high pressure deammoniation tower adopts the middle pressure steam of more than 1.2Mpa to make thermal source, the tower top pressure of regulable control deammoniation tower is 0.6Mpa, tower top temperature is 145 DEG C, tower bottom pressure is 0.65Mpa, and column bottom temperature is 165 DEG C;
(7) from the overhead extraction of high pressure deammoniation tower containing ammonia vapor enter follow-up multistage fractional condensation device carry out concentrated after, regulate the PH value of water in micro-electrolysis reactor with hydrochloric acid, control between 3-4; In micro-electrolysis reactor, add gac and iron powder, gac and iron powder consumption are 0.03% of waste water total amount simultaneously, absorption 30min;
(8) micro-electrolysis reactor water outlet enters air flotation pool, and air supporting pool inner water PH value be adjusted between 8-9 with sodium hydroxide, then carry out ultrafiltration, the water after uf processing enters activated carbon adsorption tank, after charcoal absorption, enter outlet sump, obtains the trade effluent after processing.
Embodiment 2
A kind of refinery water high-efficient treatment method, it is characterized in that, described treatment process comprises the following steps:
(1) in oil extraction waste water former water per ton, add 0.8kg terra silicea purificata, after adopting pressurized air paddling process to stir, send into oil trap, carry out oil removal process;
(2) waste water after oil removal enters coagulation basin, opens coagulation basin impeller and carries out coagulating, reaction times 50min;
(3) waste water after coagulating, after filtering to storage pool, adds inorganic polymer flocculant Tai-Ace S 150 30g/L, stirs, flocculation time 100min in reaction tank;
(4) upper clear supernate through flocculation sediment is sent into catalytic oxidation device, when steam-water ratio 1:20, pressurized air stirs, catalytic oxidation 5h;
(5) refinery water is divided cold, heat two strands enters in tower respectively from the low pressure depickling deammoniation tower top and middle and upper part of being with lateral line withdrawal function, low pressure depickling deammoniation tower tower top pressure is regulated to be 0.2MPa respectively, low pressure depickling deammoniation tower adopts the low-pressure steam of 0.7Mpa to make thermal source, tower top temperature 45 DEG C, tower bottom pressure is 0.22MPa, column bottom temperature 120 DEG C, after sour gas in refinery water is gone out from stripped overhead, enter incinerator, after being condensed to 115 DEG C from the overhead extraction of low pressure deammoniation tower containing ammonia vapor, enter in knockout drum and be separated gas phase and liquid phase, liquid-phase reflux returns in tower, gas phase enters second stage condenser, after being all condensed into weak ammonia, high pressure deammoniation tower is pumped into through storage tank,
(6) entered the middle and upper part of high pressure deammoniation tower by the still liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, high pressure deammoniation tower adopts the middle pressure steam of more than 1.5Mpa to make thermal source, the tower top pressure of regulable control deammoniation tower is 0.6Mpa, tower top temperature is 145 DEG C, tower bottom pressure is 0.65Mpa, and column bottom temperature is 165 DEG C;
(7) from the overhead extraction of high pressure deammoniation tower containing ammonia vapor enter follow-up multistage fractional condensation device carry out concentrated after, regulate the PH value of water in micro-electrolysis reactor with hydrochloric acid, control between 3-4; In micro-electrolysis reactor, add gac and iron powder, gac and iron powder consumption are 0.05% of waste water total amount simultaneously, absorption 40min;
(8) micro-electrolysis reactor water outlet enters air flotation pool, and air supporting pool inner water PH value be adjusted between 8-9 with sodium hydroxide, then carry out ultrafiltration, the water after uf processing enters activated carbon adsorption tank, after charcoal absorption, enter outlet sump, obtains the trade effluent after processing.
Embodiment 3
A kind of refinery water high-efficient treatment method, it is characterized in that, described treatment process comprises the following steps:
(1) in oil extraction waste water former water per ton, add 0.6kg terra silicea purificata, after adopting pressurized air paddling process to stir, send into oil trap, carry out oil removal process;
(2) waste water after oil removal enters coagulation basin, opens coagulation basin impeller and carries out coagulating, reaction times 45min;
(3) waste water after coagulating, after filtering to storage pool, adds inorganic polymer flocculant Tai-Ace S 150 28g/L, stirs, flocculation time 90min in reaction tank;
(4) upper clear supernate through flocculation sediment is sent into catalytic oxidation device, when steam-water ratio 1:20, pressurized air stirs, catalytic oxidation 4.5h;
(5) refinery water is divided cold, heat two strands enters in tower respectively from the low pressure depickling deammoniation tower top and middle and upper part of being with lateral line withdrawal function, low pressure depickling deammoniation tower tower top pressure is regulated to be 0.2MPa respectively, low pressure depickling deammoniation tower adopts the low-pressure steam of 0.7Mpa to make thermal source, tower top temperature 45 DEG C, tower bottom pressure is 0.22MPa, column bottom temperature 120 DEG C, after sour gas in refinery water is gone out from stripped overhead, enter incinerator, after being condensed to 115 DEG C from the overhead extraction of low pressure deammoniation tower containing ammonia vapor, enter in knockout drum and be separated gas phase and liquid phase, liquid-phase reflux returns in tower, gas phase enters second stage condenser, after being all condensed into weak ammonia, high pressure deammoniation tower is pumped into through storage tank,
(6) entered the middle and upper part of high pressure deammoniation tower by the still liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, high pressure deammoniation tower adopts the middle pressure steam of more than 1.3Mpa to make thermal source, the tower top pressure of regulable control deammoniation tower is 0.6Mpa, tower top temperature is 145 DEG C, tower bottom pressure is 0.65Mpa, and column bottom temperature is 165 DEG C;
(7) from the overhead extraction of high pressure deammoniation tower containing ammonia vapor enter follow-up multistage fractional condensation device carry out concentrated after, regulate the PH value of water in micro-electrolysis reactor with hydrochloric acid, control between 3-4; In micro-electrolysis reactor, add gac and iron powder, gac and iron powder consumption are 0.05% of waste water total amount simultaneously, absorption 35min;
(8) micro-electrolysis reactor water outlet enters air flotation pool, and air supporting pool inner water PH value be adjusted between 8-9 with sodium hydroxide, then carry out ultrafiltration, the water after uf processing enters activated carbon adsorption tank, after charcoal absorption, enter outlet sump, obtains the trade effluent after processing.
Waste water hydrogen sulfide after its process and the residual quantity of carbonic acid gas are far below 50mg/L, and ammonia quantity 45mg/L, conform with the regulations standard.
By low-pressure steam price per ton 25 yuan, 1.5Mpa steam price 120 yuan calculating, adopt the present invention to process waste water, the steam cost of ton water is only 5.7 yuan, and will take original technique, and the steam cost of ton water is about 15-22 unit.Benefit highly significant.
Claims (5)
1. a refinery water high-efficient treatment method, is characterized in that, described treatment process comprises the following steps:
(1) in oil extraction waste water former water per ton, add 0.5-0.8kg terra silicea purificata, after adopting pressurized air paddling process to stir, send into oil trap, carry out oil removal process;
(2) waste water after oil removal enters coagulation basin, opens coagulation basin impeller and carries out coagulating, reaction times 40-50min;
(3) waste water after coagulating, after filtering to storage pool, adds inorganic polymer flocculant Tai-Ace S 150 25-30g/L, stirs, flocculation time 80-100min in reaction tank;
(4) upper clear supernate through flocculation sediment is sent into catalytic oxidation device, when steam-water ratio 1:20, pressurized air stirs, catalytic oxidation 4-5h;
(5) refinery water is made to divide hot and cold two bursts of low pressure depickling deammoniation tower tops from band lateral line withdrawal function and middle and upper part to enter respectively in tower, low pressure depickling deammoniation tower tower top pressure is regulated to be 0.2MPa respectively, tower top temperature 45 DEG C, tower bottom pressure is 0.22MPa, column bottom temperature 120 DEG C, after sour gas in refinery water is gone out from stripped overhead, enter incinerator;
(6) entered the middle and upper part of high pressure deammoniation tower by the still liquid of pump extraction from low pressure depickling deammoniation tower tower reactor, the tower top pressure of regulable control deammoniation tower is 0.6Mpa, and tower top temperature is 145 DEG C, and tower bottom pressure is 0.65Mpa, and column bottom temperature is 165 DEG C;
(7) from the overhead extraction of high pressure deammoniation tower containing ammonia vapor enter follow-up multistage fractional condensation device carry out concentrated after, regulate the PH value of water in micro-electrolysis reactor with hydrochloric acid, control between 3-4; In micro-electrolysis reactor, add gac and iron powder, absorption 30-40min simultaneously;
(8) micro-electrolysis reactor water outlet enters air flotation pool, and air supporting pool inner water PH value be adjusted between 8-9 with sodium hydroxide, then carry out ultrafiltration, the water after uf processing enters activated carbon adsorption tank, after charcoal absorption, enter outlet sump, obtains the trade effluent after processing.
2. a kind of refinery water high-efficient treatment method according to claim 1, is characterized in that, described step (5) mesolow depickling deammoniation tower adopts the low-pressure steam of 0.6-0.7Mpa to make thermal source.
3. a kind of refinery water high-efficient treatment method according to claim 1, is characterized in that, described step (6) mesohigh deammoniation tower adopts the middle pressure steam of more than 1.2-1.5Mpa to make thermal source.
4. a kind of refinery water high-efficient treatment method according to claim 1, is characterized in that, in described step (7), gac and iron powder consumption are the 0.03-0.05% of waste water total amount.
5. a kind of refinery water high-efficient treatment method according to claim 1, it is characterized in that, after being condensed to 115 DEG C from the overhead extraction of low pressure deammoniation tower containing ammonia vapor in described step (5), enter in knockout drum and be separated gas phase and liquid phase, liquid-phase reflux returns in tower, gas phase enters second stage condenser, after being all condensed into weak ammonia, pumps into high pressure deammoniation tower through storage tank.
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| CN104628212B (en) | 2018-12-28 |
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