CN106477792A - A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure - Google Patents
A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure Download PDFInfo
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- CN106477792A CN106477792A CN201610851727.XA CN201610851727A CN106477792A CN 106477792 A CN106477792 A CN 106477792A CN 201610851727 A CN201610851727 A CN 201610851727A CN 106477792 A CN106477792 A CN 106477792A
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- 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
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- 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
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- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- 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
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- 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)
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- 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)
- Physical Water Treatments (AREA)
- Degasification And Air Bubble Elimination (AREA)
Abstract
The invention belongs to petro-chemical waste water treatment technical field, and in particular to a kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure, the method are concretely comprised the following steps：Sulfur-bearing, ammonia sour water is degassed, enter stripper ground floor column plate after oil removing, the gaseous mixture gone out from stripped overhead is through fractional condensation, gained sour gas is delivered to sulfur recovery facility with the gaseous mixture of ammonia, gained Acidic Liquid is back to stripper, is delivered to each device reuse from the purified water of stripper bottom of towe extraction.In the present invention, stripper operating pressure is 0.03 0.07MPa, and column bottom temperature is reduced to 95 DEG C.Compared to existing technologies, the hot and cold load of package unit reduces, due to need not consider the recovery of ammonia thus flow process greatly shorten, reduce equipment investment and floor space and operation, maintenance cost.
Description
Technical field
The present invention relates to petro-chemical waste water treatment technical field, and in particular to a kind of nothing the process of side line single column negative pressure stripping
The method and device of petrochemical industry sour water.
Background technology
Petroleum chemical enterprise can supervene some acid waters in oil refining process, such as heavy oil catalytically cracking equipment point
Evaporate overhead condensation water, the tower top acid water of atmospheric and vacuum distillation unit, the fractionating column acid water of reformation hydrogenation plant, the rich gas of coking plant
Acid water of washings and hydrocracking unit etc..All containing the higher hydrogen sulfide of concentration and ammonia in these acid waters, if not
Removing just pollutes the environment.
Soul water stripper is the main sulfur-bearing equipment containing AMMONIA TREATMENT of oil plant.With the raising of environmental requirement, how
Optimize soul water stripper, while requiring indices satisfaction, reduce investment and operating cost is particularly important.At present
The effective treating method of sour water is to be stripped using double tower or the high pressure with side line or normal pressure Single-tower stripping, such as United States Patent (USP)
US3,335,071 and US3, double tower gas stripping process disclosed in 404,072, the method need to be stripped twice to sewage, and energy consumption is relatively
Height, investment and operating cost are higher；Chinese patent CN1249274 proposes the side that Single-tower stripping lateral line withdrawal function processes sour water
Method, but this method desirable pressure is big, and technological process is complicated, and equipment investment is big, and operating cost is high, and easily causes equipment
Corrosion and environmental pollution.
For problem above, the present invention proposes a kind of single column and does not take out side line atmospheric stripping process petrochemical industry sulfuric acid
The method of sewage, the method can overcome the defect of both the above method, technological process is relatively simple, energy consumption and operating cost relatively
Low.
Content of the invention
It is an object of the invention to overcoming the shortcomings of that existing petrochemical industry sour water processing method is present, a kind of nothing is provided
Side line single column negative pressure stripping processes the method and device of petrochemical industry sour water, and the method has substantially compared to prior art
Investment is little, the advantage such as energy consumption is low, simple to operate, gained purified water quality is higher.For achieving the above object, the present invention is adopted
Technical scheme as follows：
A kind of method for stripping process petrochemical industry sour water nothing side line single column negative pressure, it is characterised in that by following sides
Method is carried out：
A sour water initially enters raw material degassing tank (1) degassing de-oiling, and subsequently entering raw material water tank (2), to carry out sedimentation de-
Oil, is finally pumped in raw water oil expeller (3) further oil removing；
Step a gained sour water to predetermined temperature, is then input into by b by raw water-purification water- to-water heat exchanger (6) heat exchange
Ground floor column plate to Sulfur-containing Sewage Stripping Tower (4) is stripped, and tower top gaseous mixture enters return tank of top of the tower (5) after heat exchange and enters
Row gas-liquid separation, the sour gas that separates are delivered to sulfur recovery facility, and the Acidic Liquid that separates pumps into sulfur-bearing again
Wastewater Stripping Tower (4) top is flowed back；Bottom of towe liquid returns to sour water stripping after being delivered to bottom reboiler (8) heat exchange
In tower (4), in tower, the purified water of condensation is discharged from bottom of towe outlet, is sent after raw water-purification water- to-water heat exchanger (6) heat exchange, boosting
To each device reuse.
In such scheme, Sulfur-containing Sewage Stripping Tower (4) are divided into top packing section and lower tray section, top packing section
Filling random packing, the theoretical cam curve of lower tray section is 30-40, and the ratio of the tower diameter of top packing section and lower tray section is
0.1-1:1.
In such scheme, the operating pressure of Sulfur-containing Sewage Stripping Tower (4) is 0.03-0.07MPa, and tower top temperature is 80 DEG C,
Column bottom temperature is 95 DEG C.
In such scheme, the sour water after the deoiling treatment that deaerates is through raw water-purification water- to-water heat exchanger (6) heat exchange to 95-
The ground floor column plate of Sulfur-containing Sewage Stripping Tower (4) is entered after 105 DEG C.
In such scheme, the gaseous mixture gone out from stripped overhead is through sour gas-low-temperature water heating heat exchanger (7) heat exchange to 85-95
Return tank of top of the tower (5) is entered after DEG C.
In such scheme, bottom of towe liquid returns to sour water stripping through bottom reboiler (8) heat exchange to after 120-135 DEG C
In tower (4), described bottom reboiler (8) are using 1.0MPa stripped vapor as thermal source.
In such scheme, in tower the purified water of condensation through raw water-purification water- to-water heat exchanger (6) heat exchange to after 55-65 DEG C, by
Pump boosts, and purified water-air cooling device (9), purification water cooler (10) are cooled to 40 DEG C and deliver to each device reuse.
Preferably, in such scheme, the operating pressure of Sulfur-containing Sewage Stripping Tower (4) is 0.05MPa, the tower of lower tray section
Plate number is 36, and the sour water after the deoiling treatment that deaerates is entered to after 100 DEG C through raw water-purification water- to-water heat exchanger (6) heat exchange and contained
Sulphur Wastewater Stripping Tower (4) ground floor column plate, the gaseous mixture gone out from stripped overhead is through sour gas-low-temperature water heating heat exchanger (7) heat exchange
Return tank of top of the tower (5) is entered to after 90 DEG C, and bottom of towe liquid returns to sour water stripping through reboiler (8) heat exchange to after 128 DEG C
In tower (4), in tower, the purified water of condensation boosts to after 60 DEG C through raw water-purification water- to-water heat exchanger (6) heat exchange and cools back use.
The above-mentioned device for stripping process petrochemical industry sour water nothing side line single column negative pressure, including raw material degassing tank (1), original
Material water pot (2), raw water oil expeller (3), Sulfur-containing Sewage Stripping Tower (4), return tank of top of the tower (5), raw water-purification water- to-water heat exchanger
(6), sour gas-low-temperature water heating heat exchanger (7), bottom reboiler (8), purified water air cooler (9) and purification water cooler
(10), described Sulfur-containing Sewage Stripping Tower (4) be divided into top packing section and lower tray section, top packing section fills random packing,
The theoretical cam curve of lower tray section is 30-40, and the ratio of the tower diameter of top packing section and lower tray section is 0.1-1:1；Wherein
Raw material degassing tank (1), raw material water tank (2), raw water oil expeller (3), Sulfur-containing Sewage Stripping Tower (4) are sequentially connected by pipeline；
Sour gas-low-temperature water heating heat exchanger (7) is exported with Sulfur-containing Sewage Stripping Tower (4) overhead vapor by pipeline respectively and tower top is returned
Stream tank (5) air inlet is connected, and the gas vent of return tank of top of the tower (5) leads to sulfur recovery facility, and it is dirty that liquid outlet leads to sulfur-bearing
Water stripper (4) top；Sulfur-containing Sewage Stripping Tower (4) bottom is provided with liquid entrance and discharge outlet, the liquid entrance
Be connected with bottom reboiler (8), discharge outlet by pipeline successively with raw water-purification water- to-water heat exchanger (6), force (forcing) pump, purified water
Air cooler (9), purification water cooler (10) are connected.
In the inventive method, raw material sour water is flowed in Sulfur-containing Sewage Stripping Tower (4) from top to bottom, through bottom of towe reboiling
H after device (8) stripping2S and NH3Component is escaped from acid water and is from bottom to top separated from tower top, and bottom of towe extraction purifies Water circulation.Tower
Top sour gas condensation cooling takes the flow process of heat using low-temperature water heating, and the 1.0Mpa stripped vapor that bottom reboiler is adopted is from system
Pipe network.Pump used in the present invention using energy-saving chemical flow-process pump and is equipped with energy-saving electrical machine, can improve pump and motor
Efficiency, bottom of towe air cooler (9) adopts converter technique, saved the consumption of electric energy, and other each equipment, each pipeline are strictly by relevant
Standard regulation is incubated, and reduces heat loss.
The present invention compared with prior art, has the advantage that：
(1) under the conditions of other situation identicals, the steam stripped hot and cold load of negative pressure is all few than low pressure, saving energy consumption.
(2) stripper adopts negative-pressure operation, reduces column bottom temperature, and therefore the steam using low temperature position is used as reboiler
Thermal source, further energy saving.
(3) due to considering the recovery of ammonia, thus the multistage fractional condensation of ammonia, ammonia purifier need not be set, flow process is significantly
Shorten, reduce equipment investment and floor space, and operation, maintenance cost.
(4) due to simultaneously by ammonia and acid gas removal and flow process shortening, the fractional condensation phegma of ammonia in a stripper
Greatly reduce, thus the steam total amount needed for depickling deamination can be greatly lowered, and can be using low-pressure steam as heat
Source.
Description of the drawings
Fig. 1 processes petrochemical industry sour water device and process schematic representation for of the present invention stripping nothing side line single column negative pressure.
1- raw material degassing tank, 2- raw material water tank, 3- raw water oil expeller, 4- Sulfur-containing Sewage Stripping Tower, 5- return tank of top of the tower,
6- raw water-purification water- to-water heat exchanger, 7- sour gas-low-temperature water heating heat exchanger, 8- bottom reboiler, 9- purified water air cooler, 10-
Purify water cooler.
Specific embodiment
For making those of ordinary skill in the art fully understand technical scheme and beneficial effect, below in conjunction with concrete
Embodiment is further described, but the present invention is not limited in following examples.
Embodiment 1
The high sulfur-bearing of certain petrochemical plant and the sour water of ammonia, in charging, the raw material water yield is 12000Kg/h, wherein vulcanizes
Hydrogen concentration is 80000ppm, and ammonia density is 40000ppm.After raw water is filtered, initially enters raw material degassing tank 1 and enter
Row degassing de-oiling, to low pressure gas pipe network, sump oil enters slop tank to the light oil pneumatic transmission of abjection.Raw water after degassing de-oiling is through liquid
Position enters raw material water tank 2 after adjusting control and carries out sedimentation de-oiling, and the sump oil of abjection enters slop tank, and the raw water after de-oiling is through original
Material water pump boosting, then tiny oil droplets in water are removed further through raw water oil expeller 3.
Sour water after degassing oil removing is with raw water -6 heat exchange of purification water- to-water heat exchanger to 100 DEG C after Flow-rate adjustment control
Sulfur-containing Sewage Stripping Tower 4 ground floor column plate is entered afterwards.The raw water tank deck tail gas of water seal is broken through after tail gas absorber deodorization
High altitude discharge.
Sulfur-containing Sewage Stripping Tower 4 sets one section of high random packing of 6m and 36 layers of column plate, top packing section and lower tray section
Tower diameter ratio be 0.1-1:1.The operating pressure of stripper is 0.05MPa, and tower top temperature is 80 DEG C, and column bottom temperature is 95 DEG C.
Raw water is flowed in Sulfur-containing Sewage Stripping Tower 4 from top to bottom, H after being stripped by stripper bottom reboiler 82S and NH3Component is certainly
Escape in acid water, from bottom to top separate from tower top.Tower top sour gas is cooled to through tower top sour gas-low-temperature water heating heat exchanger 7
Entering return tank of top of the tower 5 after 90 DEG C carries out gas-liquid separation, and the sour gas after separating is separated to sulfur recovery facility after voltage-controlled valve
Acidic Liquid afterwards is then flowed back by 4 top of overhead reflux pumped back Sulfur-containing Sewage Stripping Tower.
Bottom of towe liquid is heated to 128 DEG C through bottom reboiler 8 and is back to stripper, and the process carries out heat exchange using steam,
Steam used is the 1.0Mpa stripped vapor come from system pipe network, does the thermal source of reboiler after flow control and regulation, its condensation
Water then enters condensation water pot, then drains into condensate pipe network.Gas participates in mass transfer, the fluid purification water that tower bottom is obtained in tower
Through raw water -6 heat exchange of purification water- to-water heat exchanger to 60 DEG C, boosted by clarified water pump, then purified water-air cooling device 9, purification water cooling
Device 10 is cooled to 40 DEG C, is delivered to each device reuse after adjusting through flow control valve.After above-mentioned process, sulphur in gained purified water
The concentration for changing hydrogen and ammonia is respectively lower than 50mg/L and 40mg/L.
Claims (9)
1. a kind of nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that in the steps below
Carry out：
A sour water initially enters raw material degassing tank (1) degassing de-oiling, and subsequently entering raw material water tank (2) carries out sedimentation de-oiling, most
After be pumped in raw water oil expeller (3) further oil removing；
B is then input to contain by step a gained sour water by raw water-purification water- to-water heat exchanger (6) heat exchange to predetermined temperature
The ground floor column plate of sulphur Wastewater Stripping Tower (4) is stripped, and tower top gaseous mixture enters return tank of top of the tower (5) after heat exchange and enters promoting the circulation of qi
Liquid is separated, and the sour gas that separates is delivered to sulfur recovery facility, and the Acidic Liquid that separates pumps into sour water again
Stripper (4) top is flowed back；Bottom of towe liquid returns to Sulfur-containing Sewage Stripping Tower after being delivered to bottom reboiler (8) heat exchange
(4) in, in tower, the purified water of condensation is discharged from bottom of towe outlet, is delivered to after raw water-purification water- to-water heat exchanger (6) heat exchange, boosting
Each device reuse.
2. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
Sulfur-containing Sewage Stripping Tower (4) are divided into top packing section and lower tray section, and top packing section fills random packing, lower tower
The theoretical cam curve of plate section is 30-40, and the ratio of the tower diameter of top packing section and lower tray section is 0.1-1:1.
3. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
The operating pressure of Sulfur-containing Sewage Stripping Tower (4) is 0.03-0.07MPa, and tower top temperature is 80 DEG C, and column bottom temperature is 95 DEG C.
4. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
Sour water after degassing deoiling treatment enters sour water through raw water-purification water- to-water heat exchanger (6) heat exchange to after 95-105 DEG C
The ground floor column plate of stripper (4).
5. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
Return tank of top of the tower is entered from the gaseous mixture that stripped overhead goes out to after 85-95 DEG C through sour gas-low-temperature water heating heat exchanger (7) heat exchange
(5).
6. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
Bottom of towe liquid is returned to after 120-135 DEG C through bottom reboiler (8) heat exchange in Sulfur-containing Sewage Stripping Tower (4), the bottom of towe weight
Boiling device (8) is using 1.0MPa stripped vapor as thermal source.
7. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
In tower, the purified water of condensation, is boosted by pump through raw water-purification water- to-water heat exchanger (6) heat exchange to after 55-65 DEG C, purified water-air cooling
Device (9), purification water cooler (10) are cooled to 40 DEG C and deliver to each device reuse.
8. as claimed in claim 1 nothing side line single column negative pressure strip process petrochemical industry sour water method, it is characterised in that：
The operating pressure of Sulfur-containing Sewage Stripping Tower (4) is 0.05MPa, and the number of plates of lower tray section is 36, after degassing deoiling treatment
Sour water enters the ground floor tower of Sulfur-containing Sewage Stripping Tower (4) to after 100 DEG C through raw water-purification water- to-water heat exchanger (6) heat exchange
Plate, enters return tank of top of the tower from the gaseous mixture that stripped overhead goes out through sour gas-low-temperature water heating heat exchanger (7) heat exchange to after 90 DEG C
(5), bottom of towe liquid is returned to after 128 DEG C through bottom reboiler (8) heat exchange in Sulfur-containing Sewage Stripping Tower (4), condensation in tower
Purified water boosts to after 60 DEG C through raw water-purification water- to-water heat exchanger (6) heat exchange and cools back use.
9. a kind of nothing side line single column negative pressure strip process petrochemical industry sour water device, it is characterised in that including raw material deaerate
Tank (1), raw material water tank (2), raw water oil expeller (3), Sulfur-containing Sewage Stripping Tower (4), return tank of top of the tower (5), raw water-purification
Water- to-water heat exchanger (6), sour gas-low-temperature water heating heat exchanger (7), bottom reboiler (8), purified water air cooler (9) and purified water
Cooler (10), Sulfur-containing Sewage Stripping Tower (4) are divided into top packing section and lower tray section, and packing section filling in top dissipates heap
Filler, the theoretical cam curve of lower tray section is 30-40, and the ratio of the tower diameter of top packing section and lower tray section is 0.1-1:1；
Wherein raw material degassing tank (1), raw material water tank (2), raw water oil expeller (3), Sulfur-containing Sewage Stripping Tower (4) pass through pipeline sequentially phase
Even；Sour gas-low-temperature water heating heat exchanger (7) is exported with Sulfur-containing Sewage Stripping Tower (4) overhead vapor respectively by pipeline and tower
Top return tank (5) air inlet is connected, and the gas vent of return tank of top of the tower (5) leads to sulfur recovery facility, and liquid outlet leads to and contains
Sulphur Wastewater Stripping Tower (4) top；Sulfur-containing Sewage Stripping Tower (4) bottom is provided with liquid entrance and discharge outlet, and the liquid enters
Outlet is connected with bottom reboiler (8), discharge outlet pass through pipeline successively with raw water-purification water- to-water heat exchanger (6), force (forcing) pump, only
Change water-air cooling device (9), purification water cooler (10) to be connected.
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| CN201610851727.XA CN106477792A (en) | 2016-09-26 | 2016-09-26 | A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure |
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| CN107754368A (en) * | 2017-10-17 | 2018-03-06 | 杭州富如德科技有限公司 | The anti-corrosion method and its anti-corrosive apparatus of a kind of soul water stripper |
| CN108911345A (en) * | 2018-09-17 | 2018-11-30 | 陕西黑猫焦化股份有限公司 | The cleaning treatment system of gas liquor after a kind of Coal Gasification |
| CN109248564A (en) * | 2018-11-15 | 2019-01-22 | 山东海科化工集团有限公司 | A kind of recycle device and technique of the ammonia liquor that petrochemical industry refinery acidity water treatment facilities generates |
| CN110215729A (en) * | 2018-03-01 | 2019-09-10 | 无锡科伦达化工热力装备有限公司 | A kind of plate distillation column |
| CN111079350A (en) * | 2019-12-31 | 2020-04-28 | 湖州同润汇海科技有限公司 | Modeling method and device for operating performance of single-tower low-pressure acidic water stripping device |
| CN112551832A (en) * | 2020-12-30 | 2021-03-26 | 福建联合石油化工有限公司 | Treatment method of high-concentration overhaul sewage |
| CN115215460A (en) * | 2022-08-11 | 2022-10-21 | 华东理工大学 | Water-saving method and device for hydrocracking device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107754368A (en) * | 2017-10-17 | 2018-03-06 | 杭州富如德科技有限公司 | The anti-corrosion method and its anti-corrosive apparatus of a kind of soul water stripper |
| CN107754368B (en) * | 2017-10-17 | 2022-12-02 | 杭州富如德科技有限公司 | Corrosion prevention method and device for acidic water stripper |
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| CN109248564A (en) * | 2018-11-15 | 2019-01-22 | 山东海科化工集团有限公司 | A kind of recycle device and technique of the ammonia liquor that petrochemical industry refinery acidity water treatment facilities generates |
| CN111079350A (en) * | 2019-12-31 | 2020-04-28 | 湖州同润汇海科技有限公司 | Modeling method and device for operating performance of single-tower low-pressure acidic water stripping device |
| CN112551832A (en) * | 2020-12-30 | 2021-03-26 | 福建联合石油化工有限公司 | Treatment method of high-concentration overhaul sewage |
| CN115215460A (en) * | 2022-08-11 | 2022-10-21 | 华东理工大学 | Water-saving method and device for hydrocracking device |
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Application publication date: 20170308 |