WO2024239595A1 - 石油炼制汽提净化水污水资源化利用方法及系统 - Google Patents

石油炼制汽提净化水污水资源化利用方法及系统 Download PDF

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Publication number
WO2024239595A1
WO2024239595A1 PCT/CN2023/136431 CN2023136431W WO2024239595A1 WO 2024239595 A1 WO2024239595 A1 WO 2024239595A1 CN 2023136431 W CN2023136431 W CN 2023136431W WO 2024239595 A1 WO2024239595 A1 WO 2024239595A1
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Prior art keywords
phenol
water
stripping
purified water
low
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PCT/CN2023/136431
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English (en)
French (fr)
Inventor
王梓先
谢加才
刘玉龙
张晓飞
吴百春
李嫣宁
刘振雷
柳津
孟斌
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Petrochina Co Ltd
CNPC Research Institute of Safety and Environmental Technology Co Ltd
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Petrochina Co Ltd
CNPC Research Institute of Safety and Environmental Technology Co Ltd
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Publication of WO2024239595A1 publication Critical patent/WO2024239595A1/zh
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Classifications

    • 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
    • C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • 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
    • 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
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/001—Upstream control, i.e. monitoring for predictive control

Definitions

  • the invention relates to the technical field of sewage treatment, and in particular to a method and system for resource utilization of petroleum refining steam stripping purified water.
  • Acidic water accounts for the highest proportion of the total process wastewater discharged from refineries, which can reach more than 60% of the total process wastewater discharged from refineries.
  • Most oil refineries in my country use the stripping method to treat acidic water.
  • the hydrogen sulfide and ammonia in the wastewater are removed and recovered by stripping.
  • the recovered hydrogen sulfide is recovered by sulfur recovery equipment.
  • the sulfur and nitrogen loads of pollutants such as the acidic water before treatment have been greatly reduced in the stripping purified water obtained after stripping treatment, and it has the advantages of low hardness and low salinity, and it is feasible to achieve water saving and emission reduction through cascade utilization and reuse process units.
  • the stripping purified water contains pollutants such as phenols, sulfides, and ammonia nitrogen, it still belongs to refining wastewater.
  • Stripping purified water is the largest point source wastewater in the oil refining process, with a unit discharge of about 0.2m3 /t crude oil. Stripping purified water needs special attention due to its large volume, and The green enterprise evaluation specification specifically sets up water efficiency performance indicators for the reuse rate of sulfur-containing wastewater for assessment, and special work on wastewater resource utilization must be carried out to ensure that the standard is met.
  • the reuse rate of sulfur-containing wastewater depends on the amount of water that the stripping purified water reuses in the oil refining process unit, while the stripping purified water that is not reused and directly discharged into the sewage treatment plant by the process unit has no contribution to the water efficiency performance of the reuse rate of sulfur-containing wastewater. Therefore, the efficiency of wastewater resource utilization of stripping purified water depends entirely on the amount of water that the stripping purified water reuses in the oil refining process unit.
  • the wastewater resource utilization method of stripping purified water used in refinery projects at home and abroad is only direct reuse, which is mainly used for water supply in the electro-desalting process.
  • the reuse rate of stripping purified water is usually difficult to exceed 50%.
  • the purpose of the present invention is to overcome the problem of low reuse rate of stripping purified water in the prior art, and to provide a method and system for resource utilization of petroleum refining stripping purified water.
  • the present invention collects the stripping purified water from the source according to the difference in volatile phenol concentration, and constructs a plant-wide stripping purified water resource utilization system based on the dual stripping towers equipped in the refinery, realizing quality-based collection, parallel treatment of the dual stripping devices, and direct reuse of the quality-based water, which can optimize and improve the wastewater resource utilization rate of the stripping purified water in the whole plant, reduce the risk of scaling and blockage of process pipelines and devices, and ensure the long-term stable operation of the process equipment.
  • the first aspect of the present invention provides a petroleum refining steam stripping purification A method for recycling water and sewage, the method comprising the following steps:
  • the sulfur-containing and amino-acidic water in the refinery is divided into high-phenolic acid water and low-phenolic acid water according to the concentration of volatile phenols contained;
  • the high-phenol acidic water is subjected to a first stripping treatment to obtain high-phenol stripping purified water;
  • the low-phenol acidic water is subjected to a second stripping treatment to obtain low-phenol stripping purified water;
  • the high-phenol stripping purified water and the low-phenol stripping purified water are reused respectively.
  • the second aspect of the present invention provides a system for resource utilization of petroleum refining steam stripping purified water and wastewater, the system comprising: a low-phenol acidic water collection network, a high-phenol acidic water collection network, an acidic water stripping tower I, an acidic water stripping tower II, a low-phenol steam stripping purified water reuse network and a high-phenol steam stripping purified water reuse network;
  • the low-phenol acidic water collection pipe network is connected to at least one oil refining process device that produces low-phenol acidic water, and is used to collect low-phenol acidic water;
  • the acidic water stripping tower I is connected to the low-phenol acidic water collection pipe network, and is used to perform stripping treatment on the collected low-phenol acidic water to obtain low-phenol stripping purified water;
  • the low-phenol stripping purified water reuse pipe network is connected to the acidic water stripping tower I, and is used to directly reuse the low-phenol stripping purified water to at least one oil refining process device among a catalytic cracking flue gas desulfurization device, a residual oil hydrogenation device, a diesel hydrogenation device and a wax oil hydrogenation device, and the water seal of the acidic water stripping tower I, and the excess low-phenol stripping purified water is reused into a sewage treatment plant;
  • the high-phenol acidic water collection network is connected to at least one oil refining process device that produces high-phenol acidic water, and is used to collect high-phenol acidic water;
  • the acidic water stripping tower II is connected to the high-phenol acidic water collection network, and is used to perform stripping treatment on the collected high-phenol acidic water to obtain high-phenol stripping purified water;
  • the high-phenol stripping purified water reuse network is connected to the acidic water stripping tower II.
  • Tower II is connected to directly reuse the high-phenol stripping purified water in at least one of the oil refining process units including the atmospheric and vacuum unit, the catalytic cracking unit, the catalytic reforming unit and the solvent regeneration unit and the water seal of the acid water stripping tower II, and reuse the excess high-phenol stripping purified water into the sewage treatment plant.
  • the present invention utilizes the difference characteristics of volatile phenol concentrations in sulfur-containing and amino-acid-containing water generated by the process equipment of the refinery, and matches the water quality control index requirements for volatile phenol organic pollution in the production water of the process equipment using steam stripping purified water as production water, adopts high-phenol steam stripping purified water and low-phenol steam stripping purified water, and collects the steam stripping purified water source separately and treats it separately in a double-tower device, thereby realizing the direct reuse of steam stripping purified water with high water use and low water use, strengthening and improving the overall reuse efficiency of steam stripping purified water, which accounts for the majority of the refinery wastewater, and can optimize and improve the wastewater resource utilization rate of the whole plant's steam stripping purified water, and can also make full use of the advantage of low hardness of steam stripping purified water, reduce the risk of scaling and blockage of process pipelines and equipment, ensure the long-term stable operation of the process equipment, and realize the maximum wastewater resource utilization of refinery stripping purified water.
  • Oil hydrogenation, diesel hydrogenation, wax oil hydrogenation and other hydrogen production process units while high-phenol stripping purified water is preferentially reused in electro-desalting, atmospheric pressure reduction, catalytic cracking and other process units with relatively low water quality requirements, and when the high-phenol stripping purified water is fully reused and still cannot meet the reuse water volume requirements of the process units, the low-phenol stripping purified water with better water quality will be reused for the process units with lower water quality requirements, further improving the overall resource utilization efficiency of the stripping purified water, and systematically optimizing the production and resource utilization system of the whole plant's stripping purified water from the source, intermediate processing and terminal reuse, to maximize the resource utilization of the whole plant's stripping purified water in the refinery, and achieve water saving, emission reduction and green development.
  • the present invention makes full use of the existing facilities of two stripping towers conventionally configured in large-scale refineries. No additional investment is required in the construction of stripping purified water treatment and reuse projects. It only needs to realize the separation and collection of high-phenol stripping purified water and low-phenol stripping purified water during system construction and operation.
  • the two stripping devices run in parallel and are directly reused by separation, which can optimize the wastewater resource utilization rate of the stripping purified water in the whole plant.
  • the operation of the entire system only requires one conventional unit operation of the acid water stripping process.
  • the process flow is short, the operation control is simple and reliable, the required amount of drugs is small, and no secondary pollution is caused to the stripping purified water.
  • the present invention can also guide refineries with only a single stripping tower to design and build a second stripping tower, and realize the separate collection of high-phenol stripping purified water and low-phenol stripping purified water during system construction and operation.
  • the dual stripping devices can operate in parallel and directly reuse the separated water, which can significantly improve the wastewater resource utilization rate of the stripping purified water in the entire plant.
  • FIG1 is a process flow chart of resource utilization of petroleum refining steam stripping purified water provided by one embodiment of the present invention.
  • the present invention provides a method for resource utilization of petroleum refining steam stripping purified water and sewage, the method comprising the following steps:
  • the sulfur-containing and amino-acidic water in the refinery is divided into high-phenolic acid water and low-phenolic acid water according to the concentration of volatile phenols contained;
  • the high-phenol acidic water is subjected to a first stripping treatment to obtain high-phenol stripping purified water;
  • the low-phenol acidic water is subjected to a second stripping treatment to obtain low-phenol stripping purified water;
  • the high-phenol stripping purified water and the low-phenol stripping purified water are reused respectively.
  • the present invention utilizes the process equipment of the oil refinery to produce volatile phenol concentration in sulfur-containing and amino acid-containing water.
  • the process equipment using stripping purified water as production water has different requirements for the control indicators of volatile phenol organic pollution in the production water quality
  • the whole process system of stripping purified water generation source and reuse terminal of petroleum refining enterprises is optimized, and the technical methods of source quality separation collection, double stripping parallel operation and quality separation direct reuse of stripping purified water with high phenol hardness and low water hardness are adopted.
  • the quality separation direct reuse mode of high water for high use and low water for low use is realized, which systematically improves the resource utilization efficiency of stripping purified water wastewater in the refinery, strengthens and improves the overall reuse efficiency of stripping purified water which accounts for the majority of refinery wastewater volume, can optimize and improve the wastewater resource utilization rate of stripping purified water in the whole plant, and can also make full use of the advantage of low hardness of stripping purified water, reduce the risk of scaling and blockage of process pipelines and equipment, and ensure the long-term stable operation of process equipment.
  • the method for resource utilization of stripping purified water in an oil refinery is to collect sulfur-containing and amino acid-containing water discharged from the source of stripping purified water, i.e., the operation and production of the refining process unit, according to the different concentrations of volatile phenols in the acidic water, and send them to two stripping units for treatment respectively, and then match the water quality of the stripping purified water with the water quality control requirements of the refinery process unit for process water injection or production water replenishment for phenolic pollutant concentration, and directly reuse the stripping purified water by quality, so as to maximize the resource utilization rate of the stripping purified water in the whole plant.
  • the present invention can make full use of the existing facilities of the two stripping towers conventionally configured in the built large-scale refinery, and does not require additional investment in the construction of stripping purified water treatment and reuse projects. It only needs to realize the quality collection of high-phenol stripping purified water and low-phenol stripping purified water in the system construction and operation, and the two stripping units are operated in parallel and directly reused by quality, so as to optimize the wastewater resource utilization rate of the stripping purified water in the whole plant.
  • the operation of the entire system only requires one conventional unit operation, the acid water stripping process.
  • the process flow is short, the operation control is simple and reliable, the amount of chemicals required is small, and no secondary pollution is caused to the stripping purified water.
  • the invention can reduce the fresh water consumption per unit crude oil of the refinery and the sewage discharge, and reduce the hydraulic load and pollution load of the sewage treatment facilities. It provides strong technical support for reducing the cost of feed water treatment and sewage treatment reuse in refineries and improving the water performance compliance rate of refineries.
  • the invention can also guide refineries with only a single stripping tower to design and build a second stripping tower, and realize the separate collection of high-phenol stripping purified water and low-phenol stripping purified water during system construction and operation.
  • the dual stripping units can operate in parallel and directly reuse the separated water, which can significantly improve the wastewater resource utilization rate of the stripping purified water in the entire plant.
  • the sulfur-containing and amino-acidic acid water of the present invention mainly comes from the acidic water produced by the atmospheric and vacuum decompression, catalytic cracking, catalytic reforming, solvent regeneration, residual oil hydrogenation, diesel hydrogenation, wax oil hydrogenation and other process units of the refinery.
  • the sulfur-containing and amino-acidic acid water produced by the atmospheric and vacuum decompression unit, catalytic cracking unit, catalytic reforming unit, and solvent regeneration unit has a high concentration of volatile phenols
  • the sulfur-containing and amino-acidic acid water produced by the hydrogenation units such as residual oil hydrogenation, diesel hydrogenation, and wax oil hydrogenation has a low concentration of volatile phenols.
  • the concentration of volatile phenols contained in the high-phenolic acidic water is greater than 10 mg/L; and the concentration of volatile phenols contained in the low-phenolic acidic water is not greater than 10 mg/L.
  • the acidic water stripping device generally cannot remove volatile phenols, and the volatile phenol concentration of the stripping purified water reused by the catalytic cracking desulfurization device of the refinery's major water user cannot be greater than 10 mg/L, otherwise the desulfurization device will foam and cannot operate normally.
  • Reusing the stripping purified water with a volatile phenol concentration lower than 10 mg/L can not only allow the device to operate normally and achieve water collection and emission reduction, but also due to the low salt and low hardness characteristics of the stripping purified water, the scaling phenomenon of the device is obvious. Due to the use of fresh water with higher hardness, the device can operate stably for a long period of time.
  • the acidic water is divided into high phenol and low phenol from the source, and a method of quality collection is adopted. According to the dividing point of 10 mg/L, the volatile phenol concentration in the acidic water is divided, and the reuse rate of the stripping purified water can be achieved to the greatest extent.
  • the method for resource utilization of stripping purified water in petroleum refining enterprises proposed in the present invention follows the principle of reasonable matching of water quality and quantity of "water source” and "water sink” in wastewater resource utilization work, and adjusts the volatile phenol organic content of production water according to the different concentrations of volatile phenols in sulfur-containing and amino acid-containing water produced by the process equipment of the refinery and the process equipment using stripping purified water as production water. Different rules are followed for pollution control indicators with high and low requirements.
  • the concentration of volatile phenols in acidic water is set at 10 mg/L as the dividing point between high-phenolic acidic water and low-phenolic acidic water.
  • the whole process system of the production source and reuse terminal of stripping purified water in petroleum refining enterprises is optimized.
  • the present invention collects stripping purified water by quality from the source according to the difference in volatile phenol concentration, and constructs a plant-wide stripping purified water wastewater resource utilization system based on the dual stripping towers equipped in the refinery.
  • the method of quality collection, parallel treatment and direct reuse of stripping purified water is adopted, and the existing dual stripping device is used to construct a plant-wide stripping purified water treatment and reuse system.
  • the difference characteristics of volatile phenol concentration in sulfur-containing and amino acid-containing water generated by the process equipment of the refinery are matched with the water quality control requirements for volatile phenol organic pollution in production water by the process equipment using stripping purified water as production water.
  • the system optimizes and improves the resource utilization efficiency of stripping purified water, and realizes water saving and emission reduction in the refinery.
  • the highly phenolic acidic water is derived from sulfur- and amino-acidic water produced by at least one oil refining process unit of an oil refinery, including a atmospheric and vacuum unit, a catalytic cracking unit, a catalytic reforming unit, and a solvent regeneration unit.
  • the low-phenolic acidic water is derived from sulfur- and amino-acidic water produced by at least one hydrorefining process unit of an oil refinery.
  • the hydrogenation unit in the present invention includes but is not limited to a residue oil hydrogenation unit, a diesel oil hydrogenation unit and a wax oil hydrogenation unit.
  • the sources of high-phenol acidic water and low-phenol acidic water can be adjusted according to the actual conditions of each refinery.
  • Acidic water containing volatile phenols at a concentration greater than 10 mg/L is used as high-phenol acidic water and subjected to the first stripping treatment; acidic water containing volatile phenols at a concentration not greater than 10 mg/L is used as low-phenol acidic water and subjected to the second stripping treatment, and then they are reused separately according to the conditions of each refinery.
  • the sulfur-containing and amino-acidic acid water of the refinery is divided into two types: high phenolic acidic water and low phenolic acidic water; by constructing two independent acidic water collection systems for high phenolic acidic water and low phenolic acidic water, the sulfur-containing and amino-acidic acid water of the refinery is divided into two types: high phenolic acidic water and low phenolic acidic water.
  • the high-phenol stripping purified water is sent to the collection pipe network and sent to two stripping purification units respectively; the two stripping purification units treat high-phenol acidic water and low-phenol acidic water respectively, and produce high-phenol stripping purified water and low-phenol stripping purified water respectively; the high-phenol stripping purified water and low-phenol stripping purified water enter the high-phenol stripping purified water reuse pipe network and the low-phenol stripping purified water reuse pipe network respectively.
  • the high-phenol stripping purified water reuse pipe network sends the high-phenol stripping purified water to the process units such as atmospheric vacuum reduction, catalytic cracking, catalytic reforming, solvent regeneration, etc.
  • the low-phenol stripping purified water reuse pipe network sends the low-phenol stripping purified water to the process units such as catalytic cracking flue gas non-regeneration wet scrubbing desulfurization, residual oil hydrogenation, diesel hydrogenation, wax oil hydrogenation, etc. that can directly reuse the low-phenol stripping purified water.
  • the two acidic water collection pipelines used do not have special technical requirements due to the different concentrations of volatile phenols contained in the acidic water that needs to be stripped. It is necessary to ensure that the high-phenol acidic water collection pipeline and the low-phenol acidic water collection pipeline are physically separated, collect high-phenol acidic water and low-phenol acidic water respectively, and ensure that the two collection pipelines operate independently.
  • the two stripping purified water reuse pipelines used collect and transport the stripping purified water that meets the control requirements of hydrogen sulfide and ammonia nitrogen produced by the two stripping devices. There are no special technical requirements due to the different concentrations of volatile phenols contained in the stripping purified water. It is necessary to ensure that the high-phenol stripping purified water reuse pipeline and the low-phenol stripping purified water reuse pipeline are physically separated and operate independently.
  • the adopted steam stripping purification device has no changing technical requirements due to the different concentrations of volatile phenols contained in the acidic water to be stripped, and there is no technical requirement for the steam stripping process to remove volatile phenols. It only needs to meet the control requirements of hydrogen sulfide and ammonia nitrogen in the steam stripping purified water (hydrogen sulfide ⁇ 20 mg/L, ammonia nitrogen (as N) ⁇ 50 mg/L).
  • the high-phenol stripping purified water is directly recycled to at least one oil refining process unit among a atmospheric and vacuum unit, a catalytic cracking unit, a catalytic reforming unit and a solvent regeneration unit.
  • the water injection in the electric desalting process of the atmospheric and vacuum unit is given priority to directly reusing the high-phenol stripping purified water, and using crude oil to extract volatile phenol, which can reduce the phenol pollution emissions of the entire plant.
  • low-phenol stripping purified water when the amount of high-phenol stripping purified water is insufficient, low-phenol stripping purified water, fresh water or demineralized water is used to supplement it, preferably low-phenol stripping purified water is used to supplement it.
  • the high-phenol stripping purified water and/or low-phenol stripping purified water used for the atmospheric and vacuum electro-desalting water injection is monitored for water quality to ensure that the pH value of the water is 6.5-8.5, the suspended matter does not exceed 5 mg/L, and the total hardness as CaCO3 does not exceed 140 mg/L.
  • the low-phenol stripping purified water is directly recycled to at least one oil refining process unit of a catalytic cracking flue gas non-regenerative wet scrubbing desulfurization unit, a residual oil hydrogenation unit, a diesel hydrogenation unit and a wax oil hydrogenation unit.
  • the catalytic cracking flue gas non-regenerative wet scrubbing desulfurization device uses low-phenol stripping purified water as the scrubbing circulating liquid make-up water.
  • the water quality of the low-phenol stripping purified water used in the catalytic cracking flue gas non-regenerative wet scrubbing desulfurization unit is monitored to ensure that the concentration of volatile phenols contained in the low-phenol stripping purified water does not exceed 10 mg/L, the concentration of TOC does not exceed 10 mg/L, and the concentration of oil does not exceed 1 mg/L.
  • the catalytic cracking flue gas non-regeneration wet scrubbing desulfurization unit and the hydrogenation units such as residual oil hydrogenation, diesel hydrogenation, and wax oil hydrogenation can only directly reuse the low-phenol stripping purified water, and it is not allowed to directly reuse the high-phenol stripping purified water under any conditions. In the case of insufficient water volume of the low-phenol stripping purified water, low-hardness fresh water is used to supplement it.
  • the present invention reuses the low-phenol stripping purified water with better water quality for the catalyst with higher water quality requirements.
  • the high-phenol stripping purified water is preferentially reused in the process units with relatively low water quality requirements, such as electro-desalting, atmospheric pressure reduction, catalytic cracking, etc.; and when the high-phenol stripping purified water is fully reused and still cannot meet the reuse water volume requirements of the process units, the low-phenol stripping purified water with better water quality will be reused in the process units with lower water quality requirements, so as to further improve the overall resource utilization efficiency of the stripping purified water, and systematically optimize the production and resource utilization system of the stripping purified water in the whole plant from the source, intermediate processing and terminal reuse, so as to maximize the resource utilization of the stripping purified water in the whole refinery and achieve water saving, emission reduction and green development.
  • the present invention has no special restrictions on the first stripping treatment and the second stripping treatment.
  • the conventional stripping method and conventional stripping tower can be used. It is only necessary to ensure that the stripping purified water produced by the stripping process meets the water quality control requirements for hydrogen sulfide and ammonia nitrogen (hydrogen sulfide ⁇ 20 mg/L, ammonia nitrogen (as N) ⁇ 50 mg/L).
  • the hydrogen sulfide contained in the high-phenol stripping purified water is ⁇ 20 mg/L, and the ammonia nitrogen calculated as N is ⁇ 50 mg/L; the hydrogen sulfide contained in the low-phenol stripping purified water is ⁇ 20 mg/L, and the ammonia nitrogen calculated as N is ⁇ 50 mg/L.
  • the second aspect of the present invention provides a system for resource utilization of petroleum refining steam stripping purified water and wastewater, the system comprising: a low-phenol acidic water collection network, a high-phenol acidic water collection network, an acidic water stripping tower I, an acidic water stripping tower II, a low-phenol steam stripping purified water reuse network and a high-phenol steam stripping purified water reuse network;
  • the low-phenol acidic water collection network is connected to at least one oil refining process device that produces low-phenol acidic water, and is used to collect low-phenol acidic water;
  • the acidic water stripping tower I is connected to the low-phenol acidic water collection network, and is used to perform stripping treatment on the collected low-phenol acidic water to obtain low-phenol stripping purified water;
  • the low-phenol stripping purified water reuse network is connected to the acidic water stripping tower I, and is used to directly reuse the low-phenol stripping purified water for catalytic cracking flue gas desulfurization equipment, At least one of the oil refining process units among the residue oil hydrogenation unit, the diesel oil hydrogenation unit and the wax oil hydrogenation unit and the water seal of the acid water stripping tower I, and the excess low-phenol stripping purified water is recycled into the sewage treatment plant;
  • the high-phenol acidic water collection network is connected to at least one oil refining process device that produces high-phenol acidic water, and is used to collect high-phenol acidic water;
  • the acidic water stripping tower II is connected to the high-phenol acidic water collection network, and is used to perform stripping treatment on the collected high-phenol acidic water to obtain high-phenol stripping purified water;
  • the high-phenol stripping purified water reuse network is connected to the acidic water stripping tower II, and is used to directly reuse the high-phenol stripping purified water to at least one oil refining process device among the atmospheric and vacuum pressure unit, the catalytic cracking unit, the catalytic reforming unit and the solvent regeneration unit, and the water seal of the acidic water stripping tower II, and reuse the excess high-phenol stripping purified water into the sewage treatment plant.
  • the oil refinery process unit that produces low-phenol acidic water includes a residue oil hydrogenation unit, a diesel hydrogenation unit, and a wax oil hydrogenation unit of an oil refinery.
  • the oil refinery process unit that produces highly phenolic acidic water includes an atmospheric and vacuum unit, a catalytic cracking unit, a catalytic reforming unit, and a solvent regeneration unit of an oil refinery.
  • the concentration of volatile phenols contained in the low-phenolic acidic water produced by the oil refining process unit that produces low-phenolic acidic water is no more than 10 mg/L.
  • the concentration of volatile phenols contained in the high phenolic acidic water produced by the oil refinery process unit that produces high phenolic acidic water is greater than 10 mg/L.
  • the method specifically comprises the following steps:
  • the high-phenolic acidic water collected by the high-phenolic acidic water collection network is subjected to a first stripping treatment through the first stripping purification device to obtain high-phenolic stripping purified water, and then the high-phenolic stripping purified water is reused through the high-phenolic stripping purified water reuse network;
  • the low-phenolic acidic water collected by the low-phenolic acidic water collection network is subjected to a second stripping treatment through the second stripping purification device to obtain low-phenolic stripping purified water, and then the low-phenolic stripping purified water is reused through the low-phenolic stripping purified water reuse network.
  • the high-phenol stripping purified water recycling pipeline network can be connected to a constant pressure reduction unit, a catalytic cracking unit, a catalytic reforming unit, a solvent regeneration unit and the like to realize the recycling of the high-phenol stripping purified water.
  • a constant pressure reduction unit a catalytic cracking unit, a catalytic reforming unit, a solvent regeneration unit and the like.
  • the low-phenol stripping purified water recycling pipeline network can be connected to a catalytic cracking flue gas non-regeneration wet scrubbing desulfurization unit, a residual oil hydrogenation unit, a diesel hydrogenation unit, a wax oil hydrogenation unit and other units to achieve the recycling of low-phenol stripping purified water.
  • a catalytic cracking flue gas non-regeneration wet scrubbing desulfurization unit a residual oil hydrogenation unit
  • a diesel hydrogenation unit a wax oil hydrogenation unit and other units to achieve the recycling of low-phenol stripping purified water.
  • the concentration of volatile phenols contained in the sulfur-containing and amino-acidic water of each device in the refinery can be monitored to determine whether it enters the high-phenolic acid water collection network or the low-phenolic acid water collection network.
  • Each refinery can make adjustments based on its actual situation.
  • the present invention is based on the double stripping towers equipped in the refinery to construct a wastewater resource utilization system for the whole plant's stripping purified water, realizes quality-based collection, and parallel treatment of the double stripping devices, and direct reuse of quality-based wastewater, which can optimize and improve the wastewater resource utilization rate of the whole plant's stripping purified water.
  • the entire stripping purified water resource utilization system does not require additional investment in the construction of stripping purified water treatment and reuse projects, and the industry The process flow is short, and the operation and control are simple and reliable.
  • a large oil refinery was designed and equipped with two sets of sulfur-containing and amino acid-containing water stripping units. After mixing and treating the sulfur-containing and amino acid-containing water produced by various process units in the plant, part of the stripping purified water was directly reused in the process units to realize the resource utilization of stripping purified water and wastewater, and the stripping purified water that could not be reused was discharged into the sewage treatment plant.
  • the stripping purified water reuse efficiency of the whole plant was less than 60%.
  • the method of the present invention is used to optimize the large-scale refinery in the prior art, as shown in FIG1 , and the specific steps are as follows:
  • a low-phenol acidic water collection network is specially set up for the low-phenol acidic water produced by the hydrogenation process units such as residue oil hydrogenation, diesel hydrogenation, and wax oil hydrogenation, and sent to the acidic water stripping tower I. After the first stripping treatment, it is ensured that the sulfide and ammonia nitrogen meet the standards (sulfide ⁇ 20 mg/L and ammonia nitrogen ⁇ 50 mg/L). Obtain low-phenol stripping purified water;
  • the low-phenol stripping purified water is directly reused in various hydrogen production process units such as catalytic cracking flue gas desulfurization, residual oil hydrogenation, diesel hydrogenation, wax oil hydrogenation, and the water seal of the acid water stripping tower I;
  • a special high-phenol acidic water collection network is set up for the high-phenol acidic water produced by the atmospheric and vacuum pressure, catalytic cracking, solvent regeneration and other process units (as shown in Figure 1), and the acidic water is sent to the acidic water stripping tower II. After the second stripping treatment, it is ensured that the sulfide and ammonia nitrogen meet the standards (sulfide ⁇ 20 mg/L and ammonia nitrogen ⁇ 50 mg/L), and high-phenol stripping purified water is obtained.
  • the purified water from high-phenol stripping can be directly reused in production process units such as electric desalination, catalytic cracking, etc. (as shown in Figure 1) and the water seal of the acid water stripping tower II.
  • the purified water from high-phenol stripping that exceeds the amount used in each direct reuse process unit is discharged into a sewage treatment plant for treatment and then meets the discharge standards; among them, the purified water from high-phenol stripping discharged into the sewage treatment plant is not included in the resource utilization of purified water from stripping;
  • the electro-desalting process can utilize crude oil extraction to recover volatile phenols in high-phenol stripping purified water, with a removal rate of more than 90% for volatile phenols.
  • the volatile phenol pollution load that eventually enters the refinery wastewater treatment plant can therefore be reduced by 50 tons per year.
  • the low-phenol stripping purified water can be reused in the process units that give priority to using high-phenol stripping purified water. This can save fresh water and improve the resource utilization rate of stripping purified water in the whole plant.
  • the low-phenol stripping purified water that exceeds the amount used by each direct reuse process unit is discharged into a sewage treatment plant for treatment and then meets the discharge standards.
  • the low-phenol stripping purified water discharged into the sewage treatment plant is not included in the resource utilization of the stripping purified water.
  • the refinery did not consider the different concentrations of volatile phenols in the stripping purified water, did not collect the acidic water by quality, and adopted the mixed collection of the acidic water produced by each process unit, and evenly distributed the two sets of stripping units according to the water volume, resulting in the production of water from the two sets of acidic water stripping units.
  • the phenol content in the water is relatively high.
  • the catalytic cracking flue gas non-regenerative wet scrubbing desulfurization unit and other units with high requirements for production water quality cannot directly reuse the steam stripping purified water.
  • the steam stripping purified water reuse efficiency of the entire plant is less than 60%.
  • the oil refinery has increased the reuse rate of stripping purified water to more than 95% without additional engineering investment, and a total of 1.45 million m3 of stripping purified water is recycled annually, thereby saving about 1.45 million tons of fresh water and desalted water, reducing the amount of sewage generated by 1.45 million m3 , and reducing the emission of volatile phenols by 50 tons.
  • Low-phenol stripping purified water is directly recycled for alkali liquid replenishment of catalytic cracking flue gas desulfurization equipment instead of fresh water, which not only saves 55m3 /h of fresh water, but also significantly reduces the scaling and clogging of equipment and pipelines because the hardness of low-phenol stripping purified water is less than one-tenth of the hardness of local fresh water. Therefore, the method of the present invention realizes the resource utilization of stripping purified water treatment, improves the efficiency of sewage resource utilization, and achieves water saving and emission reduction, and green development.

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Abstract

石油炼制汽提净化水污水资源化利用方法及系统，方法包括如下步骤：将炼油厂含硫含氨酸性水按照所含挥发酚的浓度划分为高酚酸性水和低酚酸性水；将高酚酸性水进行第一汽提处理，得到高酚汽提净化水；将低酚酸性水进行第二汽提处理，得到低酚汽提净化水；将高酚汽提净化水和低酚汽提净化水分别进行回用。采取高酚汽提净化水和低酚汽提净化水汽提净化水源头分质收集和双塔装置分质处理技术，实现了高水高用低水低用的分质直接回用方式，系统提升炼油厂的汽提净化水污水资源化利用效率，实现炼厂汽提净化水的污水资源化最大化利用。

Description

石油炼制汽提净化水污水资源化利用方法及系统
相关申请的交叉引用
本申请要求2023年05月24日提交的中国专利申请202310596060.3的权益，该申请的内容通过引用被合并于本文。
技术领域
本发明涉及污水处理技术领域，具体涉及石油炼制汽提净化水污水资源化利用方法及系统。
背景技术
炼油厂在加工含硫原油时，常减压、催化裂化、延迟焦化、加氢精制等工艺装置都要排出大量酸性水(含硫含氨污水)，酸性水在炼厂工艺废水总排放量占比最高，可达炼厂工艺污水总量的60％以上。我国炼油厂多采用汽提法处理酸性水，污水中的硫化氢、氨通过汽提的方式进行脱除并加以回收，回收的硫化氢通过硫磺回收装置回收硫。经过汽提处理的获得的汽提净化水相比处理前的酸性水，其硫、氮等污染物负荷已经大大降低了，而且具备低硬度低盐度的优点，具有串级利用和回用工艺装置实现节水减排的可行性。但是由于汽提净化水含有酚类、硫化物、氨氮等污染物，仍然属于炼化污水。
汽提净化水是石油炼制生产过程中排水量最大的点源污水，单位排放量约0.2m3/t原油。汽提净化水由于水量大需要重点关注，而且 绿色企业评价规范专门设置了含硫污水回用率水效绩效指标进行考核，必须开展污水资源化专项工作确保达标。含硫污水回用率取决于汽提净化水回用炼油工艺装置的水量，而未能回用工艺装置直接排入污水处理场的汽提净化水对含硫污水回用率水效绩效无贡献。因此，汽提净化水污水资源化利用效率高低完全取决于汽提净化水回用炼油工艺装置的水量多少。
目前，国内外的炼厂工程应用的汽提净化水的污水资源化利用方式只有直接回用单一途径，主要用于电脱盐工艺给水。但是由于电脱盐工艺用水量存在上限，汽提净化水的回用率通常难以超过50％。为了应对不断趋严的取水定额限制和含硫污水回用率提升的需求，炼厂工艺用水水量需求较大的催化裂化烟气脱硫装置能否利用汽提净化水取代新鲜水已实现节水减排正在逐步受到业界关注。
发明内容
本发明的目的是为了克服现有技术存在的汽提净化水回用率低的问题，提供石油炼制汽提净化水污水资源化利用方法及系统，本发明根据挥发酚浓度差异将汽提净化水从源头分质收集，以炼厂装备的双汽提塔为基础，构建全厂汽提净化水污水资源化系统，实现分质收集，双汽提装置平行处理、分质直接回用，能够优化提升全厂汽提净化水的污水资源化利用率，减少工艺管线和装置结垢堵塞的风险，确保了工艺装置的长期稳定运行。
为了实现上述目的，本发明第一方面提供一种石油炼制汽提净化 水污水资源化利用方法，所述方法包括如下步骤：
将炼油厂含硫含氨酸性水按照所含挥发酚的浓度划分为高酚酸性水和低酚酸性水；
将所述高酚酸性水进行第一汽提处理，得到高酚汽提净化水；
将所述低酚酸性水进行第二汽提处理，得到低酚汽提净化水；
将所述高酚汽提净化水和低酚汽提净化水分别进行回用。
本发明第二方面提供一种石油炼制汽提净化水污水资源化利用系统，所述系统包括：低酚酸性水收集管网、高酚酸性水收集管网、酸性水汽提塔I、酸性水汽提塔II、低酚汽提净化水回用管网和高酚汽提净化水回用管网；
所述低酚酸性水收集管网连接至少一种产生低酚酸性水的炼油工艺装置，用于收集低酚酸性水；所述酸性水汽提塔I与所述低酚酸性水收集管网连接，用于将收集到的低酚酸性水进行汽提处理，得到低酚汽提净化水；所述低酚汽提净化水回用管网与所述酸性水汽提塔I连接，用于将低酚汽提净化水直接回用于催化裂化烟气脱硫装置、渣油加氢装置、柴油加氢装置和蜡油加氢装置中的至少一种炼油工艺装置以及酸性水汽提塔I的水封，回用超出的部分低酚汽提净化水进入污水处理场；
所述高酚酸性水收集管网连接至少一种产生高酚酸性水的炼油工艺装置，用于收集高酚酸性水；所述酸性水汽提塔II与所述高酚酸性水收集管网连接，用于将收集到的高酚酸性水进行汽提处理，得到高酚汽提净化水；所述高酚汽提净化水回用管网与所述酸性水汽提 塔II连接，用于将高酚汽提净化水直接回用于常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置以及酸性水汽提塔II的水封，回用超出的部分高酚汽提净化水进入污水处理场。通过上述技术方案，本发明所取得的有益技术效果如下：
(1)本发明利用炼油厂的工艺装置产生含硫含氨酸性水中挥发酚浓度差异特征，并匹配采用汽提净化水作为生产用水的工艺装置对生产用水挥发酚有机污染的水质控制指标要求，采取高酚汽提净化水和低酚汽提净化水汽提净化水源头分质收集和双塔装置分质处理，实现了汽提净化水高水高用低水低用的分质直接回用方式，强化提升了炼厂污水水量占优的汽提净化水的整体回用效率，能够优化提升全厂汽提净化水的污水资源化利用率，并且还能充分利用汽提净化水硬度低的优点，减少工艺管线和装置结垢堵塞的风险，确保了工艺装置的长期稳定运行，能够实现炼厂汽提净化水的污水资源化最大化利用。
(2)采用本发明提出的石油炼制企业汽提净化水污水资源化利用方法及系统，遵循污水资源化工作中“水源”和“水阱”的水质水量合理匹配原理，根据炼油厂工艺装置产生含硫含氨酸性水中挥发酚浓度高低不同和采用汽提净化水作为生产用水的工艺装置对生产用水水质挥发酚有机污染的控制指标高低要求不同的规律，对石油炼制企业汽提净化水的产生源头及回用终端进行全过程系统优化，采取高酚汽提净化水和低酚汽提净化水汽提净化水采取源头分质收集、双汽提装置平行运行、分质直接回用的技术方法，将水质更优的低酚汽提净化水回用于水质要求更高的催化裂化烟气非再生湿法洗涤脱硫装置、渣 油加氢、柴油加氢、蜡油加氢等临氢生产工艺装置，而高酚汽提净化水优先回用于水质要求相对较低的电脱盐、常减压、催化裂化等工艺装置，并在高酚汽提净化水完全回用仍不满足工艺装置回用水水量要求的情况下时将水质更优的低酚汽提净化水回用于对水质要求较低的工艺装置，进一步提升汽提净化水的总体资源化利用效率，对全厂汽提净化水产生及资源化利用系统从源头、中间处理和终端回用全过程进行系统优化，实现炼厂全厂汽提净化水资源化利用最大化，实现节水减排、绿色发展。
(3)本发明充分利用已建大型炼厂常规配置的2个汽提塔的现有设施，不需要额外的汽提净化水处理回用工程建设投资，只需要在系统构建和运行中实现高酚汽提净化水和低酚汽提净化水汽提净化水的分质收集，双汽提装置平行运行、分质直接回用，就能够优化全厂汽提净化水的污水资源化利用率。整个系统运行只需要酸性水汽提工艺一个常规单元操作，工艺流程简短，运行控制简便可靠，所需药剂量少且不会对汽提净化水造成二次污染，能降低炼厂单位原油新鲜水耗和污水排放量，减轻污水处理设施的水力负荷和污染负荷，为降低石油炼制企业给水处理和污水处理回用成本，提高石油炼制企业水绩效达标率，提供了有力技术支撑。本发明也可以指导只有单汽提塔的炼厂设计建设第二汽提塔，并且系统构建和运行中实现高酚汽提净化水和低酚汽提净化水汽提净化水的分质收集，双汽提装置平行运行、分质直接回用，就能够显著提升全厂汽提净化水的污水资源化利用率。
附图说明
图1为本发明一个实施方式提供的石油炼制汽提净化水污水资源化利用的工艺流程图。
具体实施方式
在本文中所披露的范围的端点和任何值都不限于该精确的范围或值，这些范围或值应当理解为包含接近这些范围或值的值。对于数值范围来说，各个范围的端点值之间、各个范围的端点值和单独的点值之间，以及单独的点值之间可以彼此组合而得到一个或多个新的数值范围，这些数值范围应被视为在本文中具体公开。
通过对石油炼制企业开展烟气脱硫装置直接回用汽提净化水的工程探索场试验发现，凡是采用高酚性水汽提净化水回用烟气脱硫装置的试验都无法保证烟气脱硫工艺的正常运行，只有采用低酚酸性水汽提净化水回用烟气脱硫装置才能够实现汽提净化水替代新鲜水且工艺长周期稳定运行。因此，发明人意外发现根据汽提净化水的含酚浓度不同匹配不同炼化工艺生产用水的需求可以提升汽提净化水污水资源化利用效率。
本发明提供一种石油炼制汽提净化水污水资源化利用方法，所述方法包括如下步骤：
将炼油厂含硫含氨酸性水按照所含挥发酚的浓度划分为高酚酸性水和低酚酸性水；
将所述高酚酸性水进行第一汽提处理，得到高酚汽提净化水；
将所述低酚酸性水进行第二汽提处理，得到低酚汽提净化水；
将所述高酚汽提净化水和低酚汽提净化水分别进行回用。
本发明利用炼油厂的工艺装置产生含硫含氨酸性水中挥发酚浓 度高低不同和采用汽提净化水作为生产用水的工艺装置对生产用水水质挥发酚有机污染的控制指标高低要求不同的规律，对石油炼制企业汽提净化水的产生源头及回用终端进行全过程系统优化，采取高酚汽提净化水和低酚汽提净化水汽提净化水采取源头分质收集、双汽提平行运行、分质直接回用的技术方法，实现了高水高用低水低用的分质直接回用方式，系统提升炼油厂的汽提净化水污水资源化利用效率，强化提升了炼厂污水水量占优的汽提净化水的整体回用效率，能够优化提升全厂汽提净化水的污水资源化利用率，并且还能充分利用汽提净化水硬度低的优点，减少工艺管线和装置结垢堵塞的风险，确保了工艺装置的长期稳定运行。
本发明提供的炼油厂汽提净化水分质资源化利用方法，是从汽提净化水产生源头即炼化工艺装置运行生产排出的含硫含氨酸性水，根据酸性水含挥发酚浓度的不同，实行分质收集，分别送2个汽提装置处理，再依据汽提净化水的水质匹配炼油工艺装置对工艺注水或生产补水的用水水质对含酚污染物浓度控制要求，分质直接回用汽提净化水，以最大化提高全厂汽提净化水的资源化利用率。本发明可充分利用已建大型炼厂常规配置的2个汽提塔的现有设施，不需要额外的汽提净化水处理回用工程建设投资，只需要在系统构建和运行中实现高酚汽提净化水和低酚汽提净化水汽提净化水的分质收集，双汽提装置平行运行、分质直接回用，就能够优化全厂汽提净化水的污水资源化利用率。整个系统运行只需要酸性水汽提工艺一个常规单元操作，工艺流程简短，运行控制简便可靠，所需药剂量少且不会对汽提净化水造成二次污染，能降低炼厂单位原油新鲜水耗和污水排放量，减轻污水处理设施的水力负荷和污染负荷，为降低炼油厂给水处理和污水处理回用成本，提高炼油厂水绩效达标率，提供了有力技术支撑。本发 明也可以指导只有单汽提塔的炼厂设计建设第二汽提塔，并且系统构建和运行中实现高酚汽提净化水和低酚汽提净化水汽提净化水的分质收集，双汽提装置平行运行、分质直接回用，就能够显著提升全厂汽提净化水的污水资源化利用率。
经研究发现，本发明的含硫含氨酸性水主要来源于炼油厂的常减压、催化裂化、催化重整、溶剂再生、渣油加氢、柴油加氢、蜡油加氢等工艺装置产生的酸性水，其中，常减压装置、催化裂化装置、催化重整装置、溶剂再生装置产生的含硫含氨酸性水含挥发酚浓度高，渣油加氢、柴油加氢、蜡油加氢等临氢装置产生的含硫含氨酸性水含挥发酚浓度低。
在本发明的一些实施方式中，所述高酚酸性水中所含挥发酚的浓度大于10mg/L；所述低酚酸性水中所含挥发酚的浓度不大于10mg/L。
发明人经过大量的研究发现，酸性水汽提装置一般不能去除挥发酚，而且炼厂的用水大户催化裂化脱硫装置回用汽提净化水的挥发酚浓度不能大于10mg/L，否则会脱硫装置会起泡不能正常运行的情况，而回用挥发酚浓度低于10mg/L的汽提净化水后不仅能让装置正常运行，实现接水减排，而且由于汽提净化水低盐低硬度的特性，装置的结垢现象明显由于使用较高硬度的新鲜水，装置能平稳长周期运行。因此，从源头对酸性水进行了高酚和低酚的划分，采取分质收集的方法。按照10mg/L的分界点来划分酸性水中挥发酚浓度，可以最大程度的实现汽提净化水的回用率。
本发明提出的石油炼制企业汽提净化水污水资源化利用方法，遵循污水资源化工作中“水源”和“水阱”的水质水量合理匹配原理，根据炼油厂工艺装置产生的含硫含氨酸性水中挥发酚浓度高低不同和采用汽提净化水作为生产用水的工艺装置对生产用水水质挥发酚有机 污染的控制指标高低要求不同的规律，以酸性水中所含挥发酚的浓度为10mg/L作为高酚酸性水和低酚酸性水的分界点，对石油炼制企业汽提净化水的产生源头及回用终端进行全过程系统优化。
本发明根据挥发酚浓度差异将汽提净化水从源头分质收集，以炼厂装备的双汽提塔为基础，构建全厂汽提净化水污水资源化系统，采用汽提净化水分质收集、平行处理、分质直接回用的方法，利用现有双汽提装置构建全厂汽提净化水处理回用系统，将炼油厂工艺装置产生的含硫含氨酸性水中挥发酚浓度差异特征，与采用汽提净化水作为生产用水的工艺装置对生产用水挥发酚有机污染的水质控制要求匹配，系统优化提升汽提净化水资源化利用效率，实现炼油厂节水减排。
在本发明的一些实施方式中，所述高酚酸性水来源于炼油厂的常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置产生的含硫含氨酸性水。
在本发明的一些实施方式中，所述低酚酸性水来源于炼油厂的至少一种临氢炼油工艺装置产生的含硫含氨酸性水。
本发明中的临氢装置包括但不限于渣油加氢装置、柴油加氢装置和蜡油加氢装置。
本发明中，高酚酸性水和低酚酸性水的来源可根据各个炼厂的实际情况进行调整。含挥发酚的浓度大于10mg/L的酸性水作为高酚酸性水，进行第一汽提处理；含挥发酚的浓度不大于10mg/L的酸性水作为低酚酸性水，进行第二汽提处理，然后再根据各个炼厂的情况进行分别回用。
本发明根据炼油厂工艺装置产生的含硫含氨酸性水中酚污染浓度含量不同，将炼油厂含硫含氨酸性水划分为高酚酸性水和低酚酸性水两种类型；通过构建高酚酸性水和低酚酸性水两个独立的酸性水收 集管网，并分别送往两个汽提净化装置；两个汽提净化装置分别处理高酚酸性水和低酚酸性水，分别产生高酚汽提净化水和低酚汽提净化水；高酚汽提净化水和低酚汽提净化水分别进入高酚汽提净化水回用管网和低酚汽提净化水回用管网。高酚汽提净化水回用管网将高酚汽提净化水送往常减压、催化裂化、催化重整、溶剂再生等可直接回用高酚汽提净化水的工艺装置，低酚汽提净化水回用管网将低酚汽提净化水送往催化裂化烟气非再生湿法洗涤脱硫、渣油加氢、柴油加氢、蜡油加氢等可以直接回用低酚汽提净化水的工艺装置。采用的两个酸性水收集管网不因为需要汽提处理的酸性水所含挥发酚的浓度高低不同而有特别的技术需求区别，需要确保高含酚酸性水收集管网和低含酚酸性水收集管网实现物理隔断，分别收集高酚酸性水和低酚酸性水，确保两个收集管网各自独立运行。采用的两个汽提净化水回用管网分别收集输送两个汽提装置生产的硫化氢及氨氮的控制要求指标达标的汽提净化水，不因为汽提净化水所含挥发酚的浓度高低不同而有特别的技术需求区别，需要确保高酚汽提净化水回用管网和低酚汽提净化水回用管网实现物理隔断，各自独立运行。
采用的汽提净化装置不因为需要汽提处理的酸性水所含挥发酚的浓度高低不同而有技术需求变化，也没有汽提工艺去除挥发酚的技术要求，只满足汽提净化水的含硫化氢及氨氮的控制要求即可(硫化氢≤20mg/L，氨氮(以N计)≤50mg/L)。
在本发明的一些实施方式中，将所述高酚汽提净化水直接回用于常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置。
常减压装置电脱盐工艺注水优先全部直接回用高酚汽提净化水，利用原油萃取挥发酚，可以降低全厂的酚污染排放。
在本发明的一些实施方式中，在所述高酚汽提净化水的水量不足的情况下，使用低酚汽提净化水、新鲜水或除盐水补足，优选使用低酚汽提净化水补足。
本发明中，在高酚汽提净化水水量不足的情况下，优先使用低酚汽提净化水，尽量不使用新鲜水或除盐水。
在本发明的一些实施方式中，对所述常减压的电脱盐注水采用的高酚汽提净化水和/或低酚汽提净化水进行水质监测，确保水质的pH值为6.5-8.5、悬浮物不超过5mg/L和以CaCO3计的总硬度不超过140mg/L。
在本发明的一些实施方式中，将所述低酚汽提净化水直接回用于催化裂化烟气非再生湿法洗涤脱硫装置、渣油加氢装置、柴油加氢装置和蜡油加氢装置中的至少一种炼油工艺装置。
在本发明的一些实施方式中，所述催化裂化烟气非再生湿法洗涤脱硫装置采用低酚汽提净化水作为洗涤循环液补充水。
在本发明的一些实施方式中，对所述催化裂化烟气非再生湿法洗涤脱硫装置采用的低酚汽提净化水进行水质监测，确保低酚汽提净化水中所含挥发酚的浓度不超过10mg/L、TOC的浓度不超过10mg/L和油的浓度不超过1mg/L。
在本发明的一些实施方式中，在所述低酚汽提净化水的水量不足的情况下，使用低硬度新鲜水补足。
本发明中，催化裂化烟气非再生湿法洗涤脱硫装置以及渣油加氢、柴油加氢、蜡油加氢等临氢装置只能直接回用低酚汽提净化水，在任何条件下都不允许直接回用高酚汽提净化水。在低酚汽提净化水的水量不足的情况下，使用低硬度新鲜水补足。
本发明将水质更优的低酚汽提净化水回用于水质要求更高的催 化裂化烟气非再生湿法洗涤脱硫装置、渣油加氢、柴油加氢、蜡油加氢等临氢生产工艺装置，而高酚汽提净化水优先回用于水质要求相对较低的电脱盐、常减压、催化裂化等工艺装置，并在高酚汽提净化水完全回用仍不满足工艺装置回用水水量要求的情况下时将水质更优的低酚汽提净化水回用于对水质要求较低的工艺装置，进一步提升汽提净化水的总体资源化利用效率，对全厂汽提净化水产生及资源化利用系统从源头、中间处理和终端回用全过程进行系统优化，实现炼厂全厂汽提净化水资源化利用最大化，实现节水减排、绿色发展。
本发明对第一汽提处理和第二汽提处理没有特殊的限制，可采用目前常规的汽提方法，采用常规的汽提塔，只需确保汽提工艺产出的汽提净化水满足汽含硫化氢及氨氮的水质控制要求(硫化氢≤20mg/L，氨氮(以N计)≤50mg/L)即可。
在本发明的一些实施方式中，所述高酚汽提净化水所含的硫化氢≤20mg/L，以N计的氨氮≤50mg/L；所述低酚汽提净化水所含的硫化氢≤20mg/L，以N计的氨氮≤50mg/L。
本发明第二方面提供一种石油炼制汽提净化水污水资源化利用系统，所述系统包括：低酚酸性水收集管网、高酚酸性水收集管网、酸性水汽提塔I、酸性水汽提塔II、低酚汽提净化水回用管网和高酚汽提净化水回用管网；
所述低酚酸性水收集管网连接至少一种产生低酚酸性水的炼油工艺装置，用于收集低酚酸性水；所述酸性水汽提塔I与所述低酚酸性水收集管网连接，用于将收集到的低酚酸性水进行汽提处理，得到低酚汽提净化水；所述低酚汽提净化水回用管网与所述酸性水汽提塔I连接，用于将低酚汽提净化水直接回用于催化裂化烟气脱硫装置、 渣油加氢装置、柴油加氢装置和蜡油加氢装置中的至少一种炼油工艺装置以及酸性水汽提塔I的水封，回用超出的部分低酚汽提净化水进入污水处理场；
所述高酚酸性水收集管网连接至少一种产生高酚酸性水的炼油工艺装置，用于收集高酚酸性水；所述酸性水汽提塔II与所述高酚酸性水收集管网连接，用于将收集到的高酚酸性水进行汽提处理，得到高酚汽提净化水；所述高酚汽提净化水回用管网与所述酸性水汽提塔II连接，用于将高酚汽提净化水直接回用于常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置以及酸性水汽提塔II的水封，回用超出的部分高酚汽提净化水进入污水处理场。
在本发明的一些实施方式中，产生低酚酸性水的炼油工艺装置包括炼油厂的渣油加氢装置、柴油加氢装置和蜡油加氢装置。
在本发明的一些实施方式中，产生高酚酸性水的炼油工艺装置包括炼油厂的常减压装置、催化裂化装置、催化重整装置和溶剂再生装置。
在本发明的一些实施方式中，产生低酚酸性水的炼油工艺装置所产生的低酚酸性水中所含挥发酚的浓度不大于10mg/L。
在本发明的一些实施方式中，产生高酚酸性水的炼油工艺装置所产生的高酚酸性水中所含挥发酚的浓度大于10mg/L。
作为本发明一种优选的实施方式，所述方法具体包括如下步骤：
(1)构建与第一汽提净化装置连接的高酚酸性水收集管网和低酚汽提净化水回用管网；并构建与第二汽提净化装置连接的低酚酸性水收集管网和低酚汽提净化水回用管网；
(2)将炼油厂含硫含氨酸性水按照所含挥发酚的浓度划分为高酚酸性水和低酚酸性水；分别将高酚酸性水和低酚酸性水通过两个独立的酸性水收集管网分别送往用于高酚酸性水汽提的第一汽提净化装置和用于低酚酸性水汽提的第二汽提净化装置；
(3)将所述高酚酸性水收集管网收集到的高酚酸性水经所述第一汽提净化装置进行第一汽提处理，得到高酚汽提净化水，然后经所述高酚汽提净化水回用管网进行高酚汽提净化水的回用；将所述低酚酸性水收集管网收集到的低酚酸性水经所述第二汽提净化装置进行第二汽提处理，得到低酚汽提净化水，然后经所述低酚汽提净化水回用管网进行低酚汽提净化水的回用。
所述高酚汽提净化水回用管网可与常减压装置、催化裂化装置、催化重整装置和溶剂再生装置等装置连接，实现高酚汽提净化水的回用，在所述高酚汽提净化水的水量不足的情况下，使用低酚汽提净化水、新鲜水或除盐水补足，优选使用低酚汽提净化水补足。
所述低酚汽提净化水回用管网可与催化裂化烟气非再生湿法洗涤脱硫装置、渣油加氢装置、柴油加氢装置和蜡油加氢装置等装置连接，实现低酚汽提净化水的回用，在所述低酚汽提净化水的水量不足的情况下，使用低硬度新鲜水补足。
本发明的方法中，可通过监测炼油厂各装置的含硫含氨酸性水所含挥发酚的浓度确定进入高酚酸性水收集管网还是低酚酸性水收集管网，各个炼厂可以根据自己的实际情况进行调节。
本发明以炼厂装备的双汽提塔为基础，构建全厂汽提净化水污水资源化系统，实现分质收集，双汽提装置平行处理、分质直接回用，能够优化提升全厂汽提净化水的污水资源化利用率。整个汽提净化水资源化利用系统不需要额外的汽提净化水处理回用工程建设投资，工 艺流程简短，运行控制简便可靠，能降低炼厂单位原油新鲜水耗和污水排放量，减轻污水处理设施的水力负荷和污染负荷，可降低炼油厂给水处理和污水处理回用成本，提高炼油厂水绩效达标率。
以下将通过实施例对本发明中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
以下实施例和对比例中未注明具体条件者，按照常规条件或制造商建议的条件进行。所用试剂或仪器未注明生产厂商者，均为可以通过市购途径获得的常规产品。
某大型炼油厂设计装备2套含硫含氨酸性水汽提装置，将全厂各工艺装置产生的含硫含氨酸性水混合处理后，部分汽提净化水直接回用工艺装置实现汽提净化水污水资源化利用，不能回用的汽提净化水排放进入污水处理场。全厂的汽提净化水回用效率不足60％。
实施例
经过全汽提净化水产生及回用全流程的系统分析，采用本发明的方法对上述现有技术中的该大型炼油厂进行优化，如图1所示，具体步骤为：
(1)通过水质分析化验，确定渣油加氢、柴油加氢、蜡油加氢等临氢生产工艺装置产生的挥发酚浓度不大于10mg/L的酸性水作为低酚酸性水；将其他工艺装置产生的挥发酚浓度大于10mg/L的酸性水作为高酚酸性水；
(2)渣油加氢、柴油加氢、蜡油加氢等临氢生产工艺装置产生的低酚酸性水专门设置低酚酸性水收集管网，送酸性水汽提塔I，经第一汽提处理确保硫化物和氨氮达标(硫化物≤20mg/L和氨氮≤50mg/L)， 获得低酚汽提净化水；
(3)将低酚汽提净化水直接回用于催化裂化烟气脱硫、渣油加氢、柴油加氢、蜡油加氢等各临氢生产工艺装置和酸性水汽提塔I的水封；
(4)常减压、催化裂化、溶剂再生等工艺装置(如图1所示)产生的高酚酸性水专门设置高酚酸性水收集管网，送酸性水汽提塔II，经第二汽提处理确保硫化物和氨氮达标(硫化物≤20mg/L和氨氮≤50mg/L)，获得高酚汽提净化水。
(5)高酚汽提净化水可直接回用于电脱盐、催化裂化等生产工艺装置(如图1所示)和酸性水汽提塔II水封，超过各直接回用工艺装置用量的高酚汽提净化水排污进入污水处理场进行处理后达标排放；其中，排入污水处理场的高酚汽提净化水不计入汽提净化水资源化利用；
(6)电脱盐工艺能利用原油萃取回收高酚汽提净化水中的挥发酚，对挥发酚的去除率可达90％以上，最终进入炼厂污水处理场的挥发酚污染负荷因此每年可以减少50吨。
(7)在高酚汽提净化水水量不能满足常减压、催化裂化、溶剂再生等工艺装置水量需求时，可以将低酚汽提净化水回用以上优先使用高酚汽提净化水的工艺装置。可以节约新鲜水，并提升全厂汽提净化水资源化利用率。
(8)超过各直接回用工艺装置用量的低酚汽提净化水排污进入污水处理场进行处理后达标排放，排入污水处理场的低酚汽提净化水不计入汽提净化水资源化利用。
现有技术中，该炼油厂没有考虑汽提净化水中挥发酚浓度不同，未对对酸性水进行分质收集，采用混合收集各工艺装置产生的酸性水，按水量平均分配2套汽提装置的操作导致2套酸性水汽提装置的产水 水质含酚量均偏高，催化裂化烟气非再生湿法洗涤脱硫装置等对生产水质要求较高的装置无法直接回用汽提净化水，全厂的汽提净化水回用效率不足60％。
通过采用实施例中的优化措施，该炼油厂在没有额外工程投资的情况下，汽提净化水的回用率提升到95％以上，每年资源化利用汽提净化水共145万m3，因此节约新鲜水和除盐水145万吨左右，减少污水产生量减少145万m3，减少挥发酚排放量50吨。低酚汽提净化水代替新鲜水直接回用于催化裂化烟气脱硫装置的碱液补水，不仅节省55m3/h新鲜水，而且由于低酚汽提净化水的硬度不足当地新鲜水硬度的十分之一，装置和管道的结垢堵塞现象显著减少。因此，本发明方法实现汽提净化水处理的资源化，提升污水资源利用效率，实现节水减排，绿色发展。
以上详细描述了本发明的优选实施方式，但是，本发明并不限于此。在本发明的技术构思范围内，可以对本发明的技术方案进行多种简单变型，包括各个技术特征以任何其它的合适方式进行组合，这些简单变型和组合同样应当视为本发明所公开的内容，均属于本发明的保护范围。

Claims (15)

  1. 一种石油炼制汽提净化水污水资源化利用方法，其特征在于，所述方法包括如下步骤：
    将炼油厂含硫含氨酸性水按照所含挥发酚的浓度划分为高酚酸性水和低酚酸性水；
    将所述高酚酸性水进行第一汽提处理，得到高酚汽提净化水；
    将所述低酚酸性水进行第二汽提处理，得到低酚汽提净化水；
    将所述高酚汽提净化水和低酚汽提净化水分别进行回用。
  2. 根据权利要求1所述的方法，其中，所述高酚酸性水中所含挥发酚的浓度大于10mg/L；
    所述低酚酸性水中所含挥发酚的浓度不大于10mg/L。
  3. 根据权利要求1或2所述的方法，其中，所述高酚酸性水来源于炼油厂的常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置产生的含硫含氨酸性水。
  4. 根据权利要求1或2所述的方法，其中，所述低酚酸性水来源于炼油厂的至少一种临氢炼油工艺装置产生的含硫含氨酸性水；
    优选地，所述临氢装置包括渣油加氢装置、柴油加氢装置和蜡油加氢装置。
  5. 根据权利要求1或2所述的方法，其中，将所述高酚汽提净化水直接回用于常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置。
  6. 根据权利要求5所述的方法，其中，在所述高酚汽提净化水的水量不足的情况下，使用低酚汽提净化水、新鲜水或除盐水补足，优选使用低酚汽提净化水补足。
  7. 根据权利要求5或6所述的方法，其中，对所述常减压的电脱盐注水采用的高酚汽提净化水和/或低酚汽提净化水进行水质监测，确保水质的pH值为6.5-8.5、悬浮物不超过5mg/L和以CaCO3计的总硬度不超过140mg/L。
  8. 根据权利要求1或2所述的方法，其中，将所述低酚汽提净化水直接回用于催化裂化烟气非再生湿法洗涤脱硫装置、渣油加氢装置、柴油加氢装置和蜡油加氢装置中的至少一种炼油工艺装置。
  9. 根据权利要求8所述的方法，其中，所述催化裂化烟气非再生湿法洗涤脱硫装置采用低酚汽提净化水作为洗涤循环液补充水。
  10. 根据权利要求9所述的方法，其中，对所述催化裂化烟气非再生湿法洗涤脱硫装置采用的低酚汽提净化水进行水质监测，确保低 酚汽提净化水中所含挥发酚的浓度不超过10mg/L、TOC的浓度不超过10mg/L和油的浓度不超过1mg/L。
  11. 根据权利要求8-10中任意一项所述的方法，其中，在所述低酚汽提净化水的水量不足的情况下，使用低硬度新鲜水补足。
  12. 根据权利要求1-11中任意一项所述的方法，其中，所述高酚汽提净化水所含的硫化氢≤20mg/L，以N计的氨氮≤50mg/L；
    所述低酚汽提净化水所含的硫化氢≤20mg/L，以N计的氨氮≤50mg/L。
  13. 一种石油炼制汽提净化水污水资源化利用系统，其特征在于，所述系统包括：低酚酸性水收集管网、高酚酸性水收集管网、酸性水汽提塔I、酸性水汽提塔II、低酚汽提净化水回用管网和高酚汽提净化水回用管网；
    所述低酚酸性水收集管网连接至少一种产生低酚酸性水的炼油工艺装置，用于收集低酚酸性水；所述酸性水汽提塔I与所述低酚酸性水收集管网连接，用于将收集到的低酚酸性水进行汽提处理，得到低酚汽提净化水；所述低酚汽提净化水回用管网与所述酸性水汽提塔I连接，用于将低酚汽提净化水直接回用于催化裂化烟气脱硫装置、渣油加氢装置、柴油加氢装置和蜡油加氢装置中的至少一种炼油工艺装置以及酸性水汽提塔I的水封，回用超出的部分低酚汽提净化水进 入污水处理场；
    所述高酚酸性水收集管网连接至少一种产生高酚酸性水的炼油工艺装置，用于收集高酚酸性水；所述酸性水汽提塔II与所述高酚酸性水收集管网连接，用于将收集到的高酚酸性水进行汽提处理，得到高酚汽提净化水；所述高酚汽提净化水回用管网与所述酸性水汽提塔II连接，用于将高酚汽提净化水直接回用于常减压装置、催化裂化装置、催化重整装置和溶剂再生装置中的至少一种炼油工艺装置以及酸性水汽提塔II的水封，回用超出的部分高酚汽提净化水进入污水处理场。
  14. 根据权利要求13所述的系统，其中，产生低酚酸性水的炼油工艺装置包括炼油厂的渣油加氢装置、柴油加氢装置和蜡油加氢装置；
    和/或，产生高酚酸性水的炼油工艺装置包括炼油厂的常减压装置、催化裂化装置、催化重整装置和溶剂再生装置。
  15. 根据权利要求13所述的系统，其中，产生低酚酸性水的炼油工艺装置所产生的低酚酸性水中所含挥发酚的浓度不大于10mg/L；
    和/或，产生高酚酸性水的炼油工艺装置所产生的高酚酸性水中所含挥发酚的浓度大于10mg/L。
PCT/CN2023/136431 2023-05-24 2023-12-05 石油炼制汽提净化水污水资源化利用方法及系统 Ceased WO2024239595A1 (zh)

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Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
CN119038657A (zh) * 2023-05-29 2024-11-29 中国石油天然气股份有限公司 一种炼化企业含硫污水处理回用方法及系统

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1393725A (en) * 1971-05-11 1975-05-14 Texaco Ag Process for treating waste waters
US4746434A (en) * 1987-06-24 1988-05-24 Amoco Corporation Process for treating sour water in oil refineries
CN101117259A (zh) * 2006-07-31 2008-02-06 中国石油化工股份有限公司 炼油厂污水处理与回用工艺系统及其运行方法
CN102452750A (zh) * 2010-10-15 2012-05-16 中国石油化工股份有限公司 炼油污水分类控制分级处理方法
CN103466874A (zh) * 2013-09-30 2013-12-25 河南龙成煤高效技术应用有限公司 高浓度酚氨污水处理方法
CN109399666A (zh) * 2018-12-14 2019-03-01 南京新世纪江南环保科技发展有限公司 一种从酸性水中回收氨的方法及装置
CN113121052A (zh) * 2019-12-30 2021-07-16 青岛海湾精细化工有限公司 一种含酚废水的处理方法及装置
CN114249634A (zh) * 2020-09-24 2022-03-29 宝武炭材料科技有限公司 一种低酚含量废水排放的酚精制方法
CN114716050A (zh) * 2021-01-06 2022-07-08 中国石油天然气集团有限公司 炼厂汽提净化水处理回用的方法

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4931146A (en) * 1988-04-05 1990-06-05 Mitsui Toatsu Chemicals, Inc. Process for obtaining high-purity bisphenol A
CN108585351B (zh) * 2018-04-11 2021-07-09 东华大学 新疆纺织工业园印染废水分质处理及提升回用率集成工艺

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1393725A (en) * 1971-05-11 1975-05-14 Texaco Ag Process for treating waste waters
US4746434A (en) * 1987-06-24 1988-05-24 Amoco Corporation Process for treating sour water in oil refineries
CN101117259A (zh) * 2006-07-31 2008-02-06 中国石油化工股份有限公司 炼油厂污水处理与回用工艺系统及其运行方法
CN102452750A (zh) * 2010-10-15 2012-05-16 中国石油化工股份有限公司 炼油污水分类控制分级处理方法
CN103466874A (zh) * 2013-09-30 2013-12-25 河南龙成煤高效技术应用有限公司 高浓度酚氨污水处理方法
CN109399666A (zh) * 2018-12-14 2019-03-01 南京新世纪江南环保科技发展有限公司 一种从酸性水中回收氨的方法及装置
CN113121052A (zh) * 2019-12-30 2021-07-16 青岛海湾精细化工有限公司 一种含酚废水的处理方法及装置
CN114249634A (zh) * 2020-09-24 2022-03-29 宝武炭材料科技有限公司 一种低酚含量废水排放的酚精制方法
CN114716050A (zh) * 2021-01-06 2022-07-08 中国石油天然气集团有限公司 炼厂汽提净化水处理回用的方法

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
"Industrial Water Processing Technology, Volume 2", 31 December 1999, SINOPEC PRESS, CN, ISBN: 7-80043-855-4, article XIE, SHUIHAI: "Section 21: Research on the Corrosivity of Sulfur-containing Sewage and Desulfurization Purified Water", pages: 80 - 85, XP009560860 *
ZHANG, JINLIN: "Study on Water-Saving Technologies for Refineries", PETROLEUM REFINERY ENGINEERING, vol. 37, no. 4, 15 April 2007 (2007-04-15), pages 46 - 49, XP093242126 *

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