CN104591496A - Decrement consumption-reduction device used for oil refinery acidic wastewater stripping process - Google Patents
Decrement consumption-reduction device used for oil refinery acidic wastewater stripping process Download PDFInfo
- Publication number
- CN104591496A CN104591496A CN201510016213.8A CN201510016213A CN104591496A CN 104591496 A CN104591496 A CN 104591496A CN 201510016213 A CN201510016213 A CN 201510016213A CN 104591496 A CN104591496 A CN 104591496A
- Authority
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- China
- Prior art keywords
- membrane module
- waste water
- pipeline
- acid waste
- stripping tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 28
- 230000008569 process Effects 0.000 title claims abstract description 28
- 230000002378 acidificating effect Effects 0.000 title abstract 5
- 239000012528 membrane Substances 0.000 claims abstract description 58
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 4
- 239000002253 acid Substances 0.000 claims description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- 239000007789 gas Substances 0.000 claims description 16
- 238000005070 sampling Methods 0.000 claims description 12
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 7
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 7
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a decrement consumption-reduction device used for an oil refinery acidic wastewater stripping process. The device comprises a security filter, a membrane module, a biochemical tank and a stripping tower, wherein the upstream workshop section and a downstream workshop section of acidic wastewater are sequentially the security filter and the membrane module and the membrane module is respectively connected with the biochemical tank for treating clear liquid and the stripping tower for treating concentrated liquid. To-be-treated acidic wastewater is firstly collected in an adjusting tank and then enters the membrane module, the clear liquid of the membrane module is sent to a biochemical workshop section and the concentrated liquid of the membrane module is sent to the stripping workshop section. By the device, the content of pollutants in the oil refinery acidic wastewater is reduced, the load of the biochemical system is relieved, the moisture amount entering the stripping tower is decreased, the load of the stripping tower is relieved so that the purposes of energy conservation and environmental friendliness are finally achieved.
Description
Technical field
The present invention relates to a kind of technical field of wastewater treatment, be specifically related to the decrement consumption reducing device of refinery acid waste water gas stripping process that a kind of membrane sepn of proposing for refinery sour water and air lift, biochemistry combine.
Background technology
Refinery multiple links in process of production, as atmospheric and vacuum distillation, catalytic cracking, hydrogen manufacturing, hydrogenation, delayed coking, gas fractionation etc. all can produce sour water, although these waste water water yields are not etc., but pollutant kind is similar, all containing oil, ammonia nitrogen, sulfide, volatile phenol and salt etc., COD (chemical oxygen demand (COD)) is general between 3000-10000mg/L, and volatile phenol is less than 1500mg/L, does not possess the basis of individual curing and Resource recovery.Refinery generally adopts the mode process of air lift, and the waste water after air lift enters biochemical workshop section of plant area again.Gas stripping process processing cost is high, and often has the waste water after process can not reach the influent quality requirement of biochemical workshop section permission.
Summary of the invention
For the problems referred to above, main purpose of the present invention is the decrement consumption reducing device of the refinery acid waste water gas stripping process providing a kind of membrane sepn for the proposition of refinery sour water and air lift, biochemistry to combine.
The present invention solves above-mentioned technical problem by following technical proposals: a kind of decrement consumption reducing device of refinery acid waste water gas stripping process, described device comprises: cartridge filter, membrane module, biochemistry pool and stripping tower, be followed successively by cartridge filter and membrane module from the upstream workshop section of acid waste water to downstream section, membrane module is the biochemistry pool of connection handling clear liquid and the stripping tower of process dope respectively.
In specific embodiments of the invention, need acid waste water to be processed to be contained in acid waste water equalizing tank, the pipeline between acid waste water equalizing tank and cartridge filter is provided with successively former water feed valve, former water topping-up pump, vacuum breaker, former water feed pressure table, former water feed flow meter and cartridge filter early gate.
Linked together by pipeline between cartridge filter and membrane module, the pipeline between cartridge filter and membrane module is provided with successively cartridge filter late gate, high-pressure pump, enter film wastewater pressure table, membrane module early gate.
Linked together by pipeline between membrane module and biochemistry pool, the pipeline between membrane module and biochemistry pool is provided with successively film clear liquid discharge valve, film clear liquid tensimeter, film clear liquid sampling valve, film clear liquid enter biochemistry pool valve and film clear liquid under meter.
Linked together by pipeline between membrane module and stripping tower, the pipeline between membrane module and stripping tower is provided with successively film dope discharge valve, film dope tensimeter, film dope stopping valve, film dope admission stripper valve, film dope under meter and film dope sampling valve.
Stripping tower is provided with the pipeline that saturation steam enters, the pipeline that saturation steam enters is provided with saturated vapour pressure table, saturation steam under meter and saturation steam feed valve.
Stripping tower is also provided with the air lift product transport pipe of conveying air lift product.
Stripping tower discharging is also installed between stripping tower and biochemistry pool and enters biochemistry pool pipeline, this pipeline is provided with stripping tower discharging and enters biochemistry pool valve.
In specific embodiments of the invention, the pipeline between described acid waste water equalizing tank and cartridge filter is also provided with acid waste water water inlet sampling valve.
In specific embodiments of the invention, described acid waste water water inlet sampling valve is arranged on the pipeline between vacuum breaker and former water feed pressure table.
In specific embodiments of the invention, described membrane module is disc tube reverse osmosis (dt-ro) membrane module.
In specific embodiments of the invention, the cartridge filter of cartridge filter to be filtering accuracy be 1-10um.
In specific embodiments of the invention, high pressure pump lift is 400m-800m.
In specific embodiments of the invention, the permission water inlet petroleum-type concentration entering biochemistry pool is 50-120mg/L, influent ammonium concentration is 500-800mg/L, water inlet sulfide concentration is 200-600mg/L, water inlet volatile phenol concentration is 40-80mg/L, the concentration of water inlet chemical oxygen demand (COD) is 500-1500mg/L, and total salt concentration is 100-1000mg/L.
Positive progressive effect of the present invention is: the decrement consumption reducing device of refinery acid waste water gas stripping process provided by the invention has the following advantages: need acid waste water to be processed to be first collected in equalizing tank in the present invention, enter membrane module subsequently, biochemical workshop section delivered to by the clear liquid of membrane module, and the dope of membrane module enters air lift workshop section.The present invention not only reduces the pollutant load of refinery acid waste water, alleviates the load of biochemical system, and reduces the water yield entering stripping tower, alleviates the load of stripping tower, finally achieves the target of energy saving standard.
Accompanying drawing explanation
Fig. 1 is the FB(flow block) of overall schematic of the present invention.
Fig. 2 is one-piece construction schematic diagram of the present invention.
Embodiment
Present pre-ferred embodiments is provided, to describe technical scheme of the present invention in detail below in conjunction with accompanying drawing.
Fig. 1 is the FB(flow block) of overall schematic of the present invention.As shown in Figure 1, the decrement consumption reducing device of refinery acid waste water gas stripping process provided by the invention, flow process comprises acid waste water and is first collected in equalizing tank, enters membrane module subsequently, biochemical workshop section delivered to by the clear liquid of membrane module, and the dope of membrane module enters air lift workshop section.
Fig. 2 is one-piece construction schematic diagram of the present invention, this concrete device of the present invention comprises: cartridge filter 8, membrane module 14, biochemistry pool 28 and stripping tower 26, be followed successively by cartridge filter 8 and membrane module 14 from the upstream workshop section of acid waste water to downstream section, membrane module 14 is the biochemistry pool 28 of connection handling clear liquid and the stripping tower 26 of process dope respectively.
Need acid waste water to be processed to be contained in acid waste water equalizing tank 1, the pipeline between acid waste water equalizing tank 1 and cartridge filter 8 is provided with successively former water feed valve 2, former water topping-up pump 3, vacuum breaker 4, former water feed pressure table 5, former water feed flow meter 6 and cartridge filter early gate 7.
Linked together by pipeline between cartridge filter 8 and membrane module 14, the pipeline between cartridge filter 8 and membrane module 14 is provided with successively cartridge filter late gate 9, high-pressure pump 10, enter film wastewater pressure table 11, membrane module early gate 12.
Linked together by pipeline between membrane module 14 and biochemistry pool 28, the pipeline between membrane module 14 and biochemistry pool 28 is provided with successively film clear liquid discharge valve 15, film clear liquid tensimeter 16, film clear liquid sampling valve 17, film clear liquid enter biochemistry pool valve 18 and film clear liquid under meter 19.
Linked together by pipeline between membrane module 14 and stripping tower 26, the pipeline between membrane module 14 and stripping tower 26 is provided with successively film dope discharge valve 13, film dope tensimeter 20, film dope stopping valve 21, film dope admission stripper valve 22, film dope under meter 23 and film dope sampling valve 24.
Stripping tower 26 is provided with the pipeline that saturation steam enters, the pipeline that saturation steam enters is provided with saturated vapour pressure table 29, saturation steam under meter 30 and saturation steam feed valve 25.
Stripping tower 26 is also provided with the air lift product transport pipe of conveying air lift product.
Stripping tower discharging is also installed between stripping tower 26 and biochemistry pool 28 and enters biochemistry pool pipeline, this pipeline is provided with stripping tower discharging and enters biochemistry pool valve 27, the part clear liquid in stripping tower 26 is conveyed in biochemistry pool 28 and processes or the part dope in biochemistry pool 28 is sent into process in stripping tower 26.
Pipeline between acid waste water equalizing tank 1 and cartridge filter 8 is also provided with acid waste water water inlet sampling valve 31, acid waste water water inlet sampling valve 31 is arranged on the pipeline between vacuum breaker 4 and former water feed pressure table 5.
Membrane module 14 in the present invention is disc tube reverse osmosis (dt-ro) membrane module, cartridge filter 8 for filtering accuracy be the cartridge filter of 1-10um, the lift of high-pressure pump 10 is 400m-800m.
The permission water inlet petroleum-type concentration entering biochemistry pool 28 is in the present invention 50-120mg/L, influent ammonium concentration is 500-800mg/L, water inlet sulfide concentration is 200-600mg/L, water inlet volatile phenol concentration is 40-80mg/L, the concentration of water inlet chemical oxygen demand (COD) is 500-1500mg/L, and total salt concentration is 100-1000mg/L.
Require in the present invention in acid waste water not containing the organic solvent caused serious harm to film.
Here is 1 specific embodiment:
Embodiment 1:
Process waste water is the acid waste water after certain refinery merges, flow 10m
3/ h, oil-contg is 120mg/L, and ammonia-nitrogen content is 12500mg/L, and sulfide content is 10000mg/L, and volatile phenol content is 600mg/L, COD
crcontent is 22000mg/L.Membrane module coupling high pressure pump lift is 700m, and membrane module concentrated stream amount is 4m
3/ h, membrane module clear liquid flow is 6m
3/ h, the rate of recovery of membrane module is 60%, and the dense water after membrane module process enters stripping tower, clear liquid enters biochemistry pool, and clear liquid effluent quality is: oil-contg is 85mg/L, and ammonia-nitrogen content is 652mg/L, sulfide content is 448mg/L, and volatile phenol content is 47mg/L, COD
crcontent is 1020mg/L.
Need acid waste water to be processed to be first collected in equalizing tank in the present invention, enter membrane module subsequently, biochemical workshop section delivered to by the clear liquid of membrane module, and the dope of membrane module enters air lift workshop section.The present invention not only reduces the pollutant load of refinery acid waste water, alleviates the load of biochemical system, and reduces the water yield entering stripping tower, alleviates the load of stripping tower, finally achieves the target of energy saving standard.
More than show and describe ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications; these changes and improvements all fall in the claimed scope of the invention, and application claims protection domain is defined by appending claims and equivalent thereof.
Claims (8)
1. the decrement consumption reducing device of a refinery acid waste water gas stripping process, it is characterized in that: described device comprises: cartridge filter, membrane module, biochemistry pool and stripping tower, be followed successively by cartridge filter and membrane module from the upstream workshop section of acid waste water to downstream section, membrane module is the biochemistry pool of connection handling clear liquid and the stripping tower of process dope respectively.
2. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 1, it is characterized in that: need acid waste water to be processed to be contained in acid waste water equalizing tank, the pipeline between acid waste water equalizing tank and cartridge filter is provided with successively former water feed valve, former water topping-up pump, vacuum breaker, former water feed pressure table, former water feed flow meter and cartridge filter early gate;
Linked together by pipeline between cartridge filter and membrane module, the pipeline between cartridge filter and membrane module is provided with successively cartridge filter late gate, high-pressure pump, enter film wastewater pressure table, membrane module early gate;
Linked together by pipeline between membrane module and biochemistry pool, the pipeline between membrane module and biochemistry pool is provided with successively film clear liquid discharge valve, film clear liquid tensimeter, film clear liquid sampling valve, film clear liquid enter biochemistry pool valve and film clear liquid under meter;
Linked together by pipeline between membrane module and stripping tower, the pipeline between membrane module and stripping tower is provided with successively film dope discharge valve, film dope tensimeter, film dope stopping valve, film dope admission stripper valve, film dope under meter and film dope sampling valve;
Stripping tower is provided with the pipeline that saturation steam enters, the pipeline that saturation steam enters is provided with saturated vapour pressure table, saturation steam under meter and saturation steam feed valve;
Stripping tower is also provided with the air lift product transport pipe of conveying air lift product;
Stripping tower discharging is also installed between stripping tower and biochemistry pool and enters biochemistry pool pipeline, this pipeline is provided with stripping tower discharging and enters biochemistry pool valve.
3. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 1, is characterized in that: the pipeline between described acid waste water equalizing tank and cartridge filter is also provided with acid waste water water inlet sampling valve.
4. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 3, is characterized in that: described acid waste water water inlet sampling valve is arranged on the pipeline between vacuum breaker and former water feed pressure table.
5. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 1 and 2, is characterized in that: described membrane module is disc tube reverse osmosis (dt-ro) membrane module.
6. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 1 and 2, is characterized in that: the cartridge filter of cartridge filter to be filtering accuracy be 1-10um.
7. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 2, is characterized in that: high pressure pump lift is 400m-800m.
8. the decrement consumption reducing device of refinery acid waste water gas stripping process according to claim 1 and 2, it is characterized in that: the permission water inlet petroleum-type concentration entering biochemistry pool is 50-120mg/L, influent ammonium concentration is 500-800mg/L, water inlet sulfide concentration is 200-600mg/L, water inlet volatile phenol concentration is 40-80mg/L, the concentration of water inlet chemical oxygen demand (COD) is 500-1500mg/L, and total salt concentration is 100-1000mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510016213.8A CN104591496A (en) | 2015-01-13 | 2015-01-13 | Decrement consumption-reduction device used for oil refinery acidic wastewater stripping process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510016213.8A CN104591496A (en) | 2015-01-13 | 2015-01-13 | Decrement consumption-reduction device used for oil refinery acidic wastewater stripping process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104591496A true CN104591496A (en) | 2015-05-06 |
Family
ID=53117612
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510016213.8A Pending CN104591496A (en) | 2015-01-13 | 2015-01-13 | Decrement consumption-reduction device used for oil refinery acidic wastewater stripping process |
Country Status (1)
| Country | Link |
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| CN (1) | CN104591496A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108231230A (en) * | 2016-12-14 | 2018-06-29 | 中核四0四有限公司 | A kind of high salinity low level waste water processing system and method |
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|---|---|---|---|---|
| CN1331053A (en) * | 2000-06-28 | 2002-01-16 | 中国石油化工集团公司 | Process for reclaiming ammonia-contained sewage |
| CN101723512A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Ammonia-contained waste water high-efficiency biochemical processing method |
| CN102874965A (en) * | 2012-10-16 | 2013-01-16 | 广州市鹏凯水处理设备有限公司 | System for recycling waste water containing oil and washing water |
| CN203904132U (en) * | 2014-06-11 | 2014-10-29 | 中国石油化工股份有限公司 | Device for treating wastewater generated in production of butadiene by virtue of oxidative dehydrogenation of industrial butene |
| CN204644044U (en) * | 2015-01-13 | 2015-09-16 | 上海安赐机械设备有限公司 | A kind of decrement consumption reducing device of refinery acid waste water gas stripping process |
-
2015
- 2015-01-13 CN CN201510016213.8A patent/CN104591496A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1331053A (en) * | 2000-06-28 | 2002-01-16 | 中国石油化工集团公司 | Process for reclaiming ammonia-contained sewage |
| CN101723512A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Ammonia-contained waste water high-efficiency biochemical processing method |
| CN102874965A (en) * | 2012-10-16 | 2013-01-16 | 广州市鹏凯水处理设备有限公司 | System for recycling waste water containing oil and washing water |
| CN203904132U (en) * | 2014-06-11 | 2014-10-29 | 中国石油化工股份有限公司 | Device for treating wastewater generated in production of butadiene by virtue of oxidative dehydrogenation of industrial butene |
| CN204644044U (en) * | 2015-01-13 | 2015-09-16 | 上海安赐机械设备有限公司 | A kind of decrement consumption reducing device of refinery acid waste water gas stripping process |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108231230A (en) * | 2016-12-14 | 2018-06-29 | 中核四0四有限公司 | A kind of high salinity low level waste water processing system and method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 201201 Shanghai, Pudong New Area Jin Tang Road, No. 2, block B, 145 Applicant after: SHANGHAI ANHORN ENVIRONMENTAL TECHNOLOGY CO., LTD. Address before: 201201 Shanghai, Pudong New Area Jin Tang Road, No. 2, block B, 145 Applicant before: Shanghai Anhorn Mechanical Equipment Co., Ltd. |
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| COR | Change of bibliographic data | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20150506 |