WO2022143272A1 - 海上油田稠油热采提供锅炉补给水的海水淡化工艺系统 - Google Patents

海上油田稠油热采提供锅炉补给水的海水淡化工艺系统 Download PDF

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WO2022143272A1
WO2022143272A1 PCT/CN2021/139828 CN2021139828W WO2022143272A1 WO 2022143272 A1 WO2022143272 A1 WO 2022143272A1 CN 2021139828 W CN2021139828 W CN 2021139828W WO 2022143272 A1 WO2022143272 A1 WO 2022143272A1
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reverse osmosis
water
unit
enters
membrane
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PCT/CN2021/139828
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French (fr)
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陈赞
刘宗园
李阳
于海斌
王林江
张树友
田莉
臧毅华
郑秋红
吴巍
佟建超
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中海油天津化工研究设计院有限公司
中国海洋石油集团有限公司
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Publication of WO2022143272A1 publication Critical patent/WO2022143272A1/zh

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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
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • 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
    • C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5281—Installations for water purification using chemical agents
    • 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
    • C02F2103/08—Seawater, e.g. for desalination
    • 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
    • C02F2209/05—Conductivity or salinity
    • C02F2209/055—Hardness
    • 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
    • C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
    • 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
    • C02F2209/22—O2
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C02F5/04—Softening water by precipitation of the hardness using phosphates
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • the invention belongs to the technical field of seawater desalination, and in particular relates to a seawater desalination process system for providing boiler feed water for thermal recovery of heavy oil in offshore oil areas.
  • Bohai Oilfield The heavy oil resources in Bohai Oilfield are characterized by large reserves, deep burial and wide viscosity range. At present, a total of 48 heavy oil fields and oil and gas structures have been discovered in the Bohai Oilfield. The proven heavy oil geological reserves account for 50.4% of the total proven oil geological reserves, while unconventional heavy oil accounts for 30.2% of the total heavy oil reserves. For unconventional heavy oil reservoirs, thermal recovery is adopted at home and abroad.
  • the high-pressure boiler that provides steam has extremely high requirements on the quality of the make-up water, and the use of pure fresh water is conducive to the long-term stable operation of the steam injection boiler.
  • the reverse osmosis membrane method it is most suitable to use the reverse osmosis membrane method to desalinate the sea and produce fresh water as the make-up water for the thermal recovery steam injection boiler.
  • the reverse osmosis membrane and incoming water quality requirements are very high.
  • Ultrafiltration technology can filter the preliminarily treated seawater to the required water quality requirements for the reverse osmosis system, which can ensure the stable operation of the reverse osmosis system.
  • the ultrafiltration pretreatment system generally uses organic membrane materials, which have short service life and weak impact resistance, and the organic membrane will be broken, resulting in the penetration of bacteria, high turbidity/SDI raw water, and increasing the frequency of subsequent reverse osmosis membrane cleaning. , there are also problems such as high membrane cleaning requirements and poor membrane performance recovery.
  • EDI Continuous Electrodemineralization Technology
  • EDI Continuous Electrodemineralization Technology
  • the overall system of this process is relatively fragile, and the membranes used are easily contaminated by impurities, and are easily degraded when encountering high temperature or oxidizing substances and high-value metal ions.
  • the water quality of seawater fluctuates greatly, and the currently commonly used single-stage or two-stage reverse osmosis has limited ability to treat salt.
  • the conductivity and silicon content of the reverse osmosis product water may exceed the influent index of EDI, which may cause scaling inside the module. Lead to scrapping of equipment, affecting the normal production of offshore platforms.
  • offshore oilfields have large sediment content and large water quality fluctuations.
  • the existing seawater desalination process has problems such as unstable water quality, complex structure, long process flow, and low degree of integration, which cannot meet the area and space of offshore oil production platforms. Limited construction conditions and water quality requirements for boiler make-up water.
  • the technical problem to be solved by the present invention is to solve the two major technical problems in the application of the membrane seawater desalination technology in the steam injection process for thermal recovery of heavy oil in offshore oilfields: 1.
  • the sea cement sand content is large, the water quality fluctuates greatly, and the existing membrane water treatment The treatment process of the system has poor impact resistance and cannot achieve stable water quality for a long time; 2.
  • the existing membrane seawater desalination technology has the characteristics of complex structure, huge project and low degree of integration, which cannot meet the area and space of the offshore oil production platform.
  • a seawater desalination process system for providing boiler make-up water for thermal recovery of heavy oil in offshore oilfields is provided.
  • a seawater desalination process system for providing boiler make-up water for thermal recovery of heavy oil in an offshore oilfield comprising an ultrafiltration unit, a desalination unit and a thermal deoxygenation unit connected in sequence,
  • the ultrafiltration unit includes a seawater lift pump, a self-cleaning filter, a plate heat exchanger, a pipeline coagulator and an ultrafiltration membrane connected in sequence, and the ultrafiltration membrane is a ceramic ultrafiltration membrane;
  • the desalination unit includes a produced water buffer tank, a reverse osmosis water supply pump, a security filter, a three-stage reverse osmosis unit, and an electrodialysis unit connected in sequence; wherein the three-stage reverse osmosis unit includes a first-stage reverse osmosis and a second-stage reverse osmosis.
  • each stage of reverse osmosis is provided with a reverse osmosis booster pump, and the rear end is connected with a reverse osmosis buffer tank; wherein the concentrated water outlet of the second stage reverse osmosis is connected with the inlet of the produced water buffer tank, The concentrated water outlet of the electrodialysis unit and the reverse osmosis buffer tank set at the back end of the secondary reverse osmosis enter into the tertiary reverse osmosis for desalination treatment;
  • the thermal deaerator unit includes a plate heat exchanger and a deaerator
  • the ultrafiltration membrane of the ultrafiltration unit is connected with the water production buffer tank of the desalination unit, and the reverse osmosis buffer tank at the rear end of the three-stage reverse osmosis of the desalination unit is connected with the plate heat exchanger of the thermal deoxygenation unit;
  • the water product outlet of the deaerator is connected with the heat exchange medium inlet of the heat exchanger, so as to provide heat exchange and temperature rise for the seawater.
  • the thermal deoxygenation unit preferably further comprises a decompression and temperature reduction device, and the decompression valve of the decompression and decompression device is a multi-stage labyrinth structure decompression valve.
  • the heat exchanger described in the ultrafiltration unit is a fully welded plate heat exchanger, and the lining heat exchange plate is made of titanium; Welded plate heat exchanger, lined with heat exchange plate made of 316L stainless steel.
  • the membrane element of the reverse osmosis is a rolled-plate membrane.
  • the present invention further provides a method for carrying out membrane seawater desalination using the above-mentioned seawater desalination process system, comprising the following steps:
  • the ultrafiltration membrane is used to separate and remove the oil and small-sized suspended solids in the incoming water, so that the turbidity of the produced water meets the requirements for entering the reverse osmosis membrane;
  • the water produced by the ultrafiltration membrane enters the water production buffer tank to be mixed with the reducing agent, and the scale inhibitor and non-oxidizing bactericide are added to the water supply through the water supply pump to enter the security filter;
  • the water produced by the osmosis membrane enters the reverse osmosis buffer tank; then it enters the secondary reverse osmosis through the reverse osmosis booster pump, the reverse osmosis membrane water enters the buffer tank, and the concentrated water returns to the produced water buffer pump; then it enters the third stage through the reverse osmosis booster pump.
  • Stage reverse osmosis, reverse osmosis membrane produced water enters the reverse osmosis buffer tank, concentrated water enters the reverse osmosis buffer tank at the back end of the first stage reverse osmosis, and then is treated by the second stage reverse osmosis; then enters the electrodialysis device through the water supply pump of the electrodialysis unit , the concentrated water enters the reverse osmosis buffer tank at the back end of the secondary reverse osmosis and then undergoes treatment through the third stage reverse osmosis, and the electrodialysis water enters the thermal deaeration unit through the water supply pump;
  • the electrodialysis product water enters the deaerator and is mixed with steam for deoxygenation to obtain deoxidized product water.
  • the deaerated product water passes through the heat exchanger of the filtration unit and is used as boiler make-up water after heat exchange.
  • the coagulant described in step 1) is one or more of ferric chloride, aluminum chloride, polyaluminum chloride, aluminum chloride-polyacrylamide .
  • the filtration mode of the ultrafiltration membrane is cross-flow filtration, and the concentration ratio is 1-10, which is adjusted according to the influent water quality.
  • the first-stage reverse osmosis recovery rate of the salt unit is 30-50%, and the produced concentrated water is discharged;
  • the secondary reverse osmosis recovery rate of the desalination unit is 80-90%, and the produced concentrated water enters the primary reverse osmosis for desalination treatment;
  • the recovery rate of the three-stage reverse osmosis in the desalination unit is 80-90%, and the produced concentrated water enters the second-stage reverse osmosis for desalination treatment;
  • the EDI recovery rate of the desalination unit is 90-95%, 70% of the produced concentrated water enters the three-stage reverse osmosis for desalination treatment, and the remaining 30% is discharged.
  • the scale inhibitor is sodium hexametaphosphate, sodium tripolyphosphate, hydroxyethylenediphosphonic acid, trimethylenephosphonic acid, ethylenediaminetetramethylenephosphine
  • the non-oxidative bactericides are diclofenac, dioxycyanomethane, isothiazolinone, dodecylbenzylammonium chloride , a kind of dodecyl dimethyl benzyl ammonium bromide.
  • the reducing agent is prepared by using secondary reverse osmosis product water.
  • seawater passes through three units of ultrafiltration, desalination and thermal deoxygenation in sequence, and the produced water meets the water quality requirements of boiler feed water.
  • the ultrafiltration unit replaces the traditional process of sedimentation + coagulation + filtration with inorganic ultrafiltration membrane, which shortens the process flow of pretreatment, ensures the water quality of pretreatment, and meets the influent requirements of reverse osmosis membrane;
  • desalination unit uses three Stage reverse osmosis + electrodialysis (EDI) can ensure that the total hardness of the produced water reaches the water quality index of the boiler feed water in the case of large fluctuations in the water quality at the front end; After heating, enter the boiler to complete the water replenishment.
  • EDI Stage reverse osmosis + electrodialysis
  • the seawater desalination process system and method of the invention has the following beneficial effects: the invention uses the ceramic ultrafiltration membrane to pretreat the seawater, saves the sedimentation and filtration processes, shortens the pretreatment process, and improves the Long-term pretreatment can resist the impact of heavy load pollution and adapt to complex water quality conditions at sea; three-stage reverse osmosis is set in the desalination unit to meet the water inflow requirements of EDI when the water quality at the front end fluctuates greatly, so that the entire desalination system can be stable.
  • the accompanying drawing is a schematic flow chart of the seawater desalination process system of the present invention for improving boiler make-up water for thermal recovery of heavy oil in offshore oilfields.
  • 1 is a seawater lift pump
  • 2 is an automatic backwash filter
  • 3 is a plate heat exchanger
  • 4 is a pipeline mixer
  • 5 is an ultrafiltration membrane system
  • 6 is a water production buffer tank
  • 7 is a reverse osmosis water supply pump
  • 8 is the security filter
  • 9 is the primary reverse osmosis booster pump
  • 10 is the primary reverse osmosis
  • 11 is the reverse osmosis buffer tank
  • 12 is the secondary reverse osmosis booster pump
  • 13 is the secondary reverse osmosis
  • 14 is the secondary reverse osmosis booster pump.
  • Reverse osmosis buffer tank 15 is three-stage reverse osmosis booster pump, 16 is three-stage reverse osmosis, 17 is reverse osmosis buffer tank, 18 is EDI water supply pump, 19 is EDI device, 20 is plate heat exchanger, and 21 is thermal Deaerator.
  • Embodiment 1 apply seawater desalination process system and process method of the present invention at a certain platform in the Bohai Sea.
  • the average seawater temperature was 2.1°C
  • the average seawater turbidity was 103.4NTU
  • the average conductivity was 46000
  • the average total dissolved solids (TDS) was 31.5g/L.
  • the seawater enters the self-cleaning filter through the seawater lift pump, and enters the heat exchanger after filtration, where it is heated up with deoxygenated water, and then heated to 25 °C, and then the coagulant ferric chloride is added; then it enters the ultrafiltration membrane for treatment, and the ultrafiltration membrane produces
  • the water enters the produced water buffer tank to be mixed with the reducing agent, and the scale inhibitor sodium tripolyphosphate and the non-oxidizing bactericide dodecyl benzyl ammonium chloride are added to the water supply through the water supply pump to enter the reverse osmosis security filter; then enter the reverse osmosis security filter through the high pressure pump
  • the first stage reverse osmosis, the reverse osmosis membrane produced water enters the buffer tank; then it enters the second stage reverse osmosis through the high pressure pump, and the reverse osmosis membrane product water enters the buffer tank; then it enters the third stage reverse osmosis through the high pressure pump
  • the process equipment has been running continuously for 30 days.
  • the average total hardness of the boiler feed water is 0.005mg/L
  • the average value of dissolved oxygen is 4.5 ⁇ g/L
  • the average value of silica is 5.1 ⁇ g/L
  • the average value of soluble solids is 500mg/L.
  • Embodiment 2 apply this technology in a certain platform of Bohai Sea.
  • the average seawater temperature was 13.5°C
  • the average seawater turbidity was 86.3NTU
  • the average conductivity was 44500
  • the average total dissolved solids (TDS) was 32.1g/L.
  • the membrane seawater desalination process system of the thermal recovery steam injection boiler of the offshore oilfield of the present invention is used to carry out the seawater desalination treatment, and the treatment steps are as follows:
  • the seawater enters the self-cleaning filter through the seawater lift pump, enters the heat exchanger after filtration, uses deoxygenated water to heat up, and then adds the coagulant ferric chloride after the temperature rises to 30 °C; then enters the ultrafiltration membrane for treatment, and the ultrafiltration membrane produces
  • the water enters the produced water buffer tank to be mixed with the reducing agent, and the scale inhibitor sodium tripolyphosphate and the non-oxidizing bactericide dodecyl benzyl ammonium chloride are added to the water supply through the water supply pump to enter the reverse osmosis security filter; then enter the reverse osmosis security filter through the high pressure pump
  • the first stage reverse osmosis, the reverse osmosis membrane produced water enters the buffer tank; then it enters the second stage reverse osmosis through the high pressure pump, and the reverse osmosis membrane product water enters the buffer tank; then it enters the third stage reverse osmosis through the high pressure pump, and the
  • the process equipment has been continuously operated for 30 days.
  • the average total hardness of the boiler feed water is 0.004mg/L
  • the average value of dissolved oxygen is 3.8 ⁇ g/L
  • the average value of silica is 4.2 ⁇ g/L
  • the average value of soluble solids is 550mg/L.
  • Embodiment 3 apply this technology in a certain platform of Bohai Sea.
  • the average seawater temperature was 28.1°C
  • the average seawater turbidity was 83.4NTU
  • the average conductivity was 44300
  • the average total dissolved solids (TDS) was 30.1g/L.
  • the seawater enters the self-cleaning filter through the seawater lift pump, enters the heat exchanger after filtration, uses deoxygenated water to heat up, and then adds the coagulant polyaluminum chloride after the temperature rises to 35 °C; then enters the ultrafiltration membrane for treatment, the ultrafiltration membrane
  • the produced water enters the produced water buffer tank to be mixed with the reducing agent, and the water is supplied by the water supply pump to add the scale inhibitor sodium tripolyphosphate and the non-oxidative bactericide dodecylbenzyl ammonium chloride to enter the reverse osmosis security filter; then pass through the high pressure pump
  • the reverse osmosis membrane produced water enters the buffer tank; then it enters the second stage reverse osmosis through the high pressure pump, and the reverse osmosis membrane product water enters the buffer tank; then it enters the third stage reverse osmosis through the high pressure pump, and the reverse osmosis membrane product water enters
  • the process equipment has been continuously operated for 30 days.
  • the average total hardness of the boiler feed water is 0.004mg/L
  • the average value of dissolved oxygen is 3.6 ⁇ g/L
  • the average value of silica is 4.5 ⁇ g/L
  • the average value of soluble solids is 600mg/L.

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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)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

一种海上油田稠油热采提供锅炉补给水的海水淡化工艺系统，包括依次连接的超滤单元、脱盐单元和热力除氧单元，超滤单元包括依次连接的海水提升泵（1）、自清洗过滤器（2）、板式换热器（3）、管道混凝器和超滤膜（5），超滤膜（5）为陶瓷超滤膜；脱盐单元包括依次连接的产水缓冲罐（6）、反渗透供水泵（7）、保安过滤器（8）、三级反渗透单元、电渗析单元；热力除氧单元包括板式换热器（20）和除氧器（21）。通过陶瓷膜超滤、反渗透、EDI和低能耗深度脱氧工艺技术集成，开发工艺精简、装置紧凑、重量轻的补给水处理集成系统；降低废液排放量，减少膜设备损耗，大幅降低操作、运维工作强度，保证设备稳定达标运行。

Description

海上油田稠油热采提供锅炉补给水的海水淡化工艺系统 技术领域
本发明属于海水淡化技术领域，特别是涉及一种用于海上油区稠油热采提供锅炉补给水的海水淡化工艺系统。
背景技术
我国海域蕴藏着丰富的油气资源，目前陆地油气产量呈现递减趋势，而国家的石油需求量稳步增长，海上油田产量的持续增长已经成为国家石油产量增长和产量接替的重要组成部分。渤海油田稠油资源具有储量规模大、油藏埋藏深、粘度范围广等特点。目前，渤海油田共发现48个稠油油田及油气构造，探明稠油地质储量占总探明石油地质储量的50.4％，而非常规稠油占稠油总储量的30.2％。对于非常规稠油油藏，国内外通过采用热采开发。在热采工艺中，提供蒸汽的高压锅炉对补给水水质要求极高，使用纯净的淡水有利于注汽锅炉长时间稳定运行。针对海上平台的特殊情况，综合考虑低成本、节能、稳定性、高效率、操作便利等因素，使用反渗透膜法对海上进行淡化处理，生产淡水作为热采注汽锅炉的补给水最为合适。但是，反渗透膜与来水水质要求很高，如果进入反渗透膜前的预处理工艺不能保证产水水质的稳定，就会造成反渗透膜使用寿命降低，膜材料频繁更换，导致增加大量的运营成本，更严重的会造成整套海水淡化系统的瘫痪。
超滤技术能够将初步处理的海水过滤至进反渗透系统所需水质要求，能够确保反渗透系统的稳定运行。超滤预处理系统一般使用有机膜材料，存在使用寿命短、抗冲击力弱，会出现有机膜的断丝情况，造成细菌、高浊度/SDI原水的穿透，增加后续反渗透膜清洗频率，还存在膜清洗要求高，膜性能恢复性较差等问题。
EDI(连续电除盐技术)与传统离子交换树脂相比具有能够连续运行，不需要化学试剂再生，无废液外排，操作简单、自动化程度高，占地面积小等特点。但是，该工艺整体系统比较脆弱，采用的膜易被杂质污染，且遇到高温或氧化性物质、高价金属离子时易降解，对入水水质要求比较高，需要水质波动较低。海水水质波动较大，目前常用的单级或二级反渗透处理盐的能力有限，反渗透产水的电导率和硅含量很可能超出EDI的进水指标，很可能会造成模块内部结垢，导致设备报废，影响海上平台的正常生产。
综上，海上油田泥沙含量大，水质波动大，现有海水淡化工艺存着在产水水质不稳定、结构复杂、工艺流程长、集成化程度低等问题，无法满足海上采油平台面积和空间有限的施 工条件及锅炉补给水的水质要求。
发明内容
本发明所要解决的技术问题是解决膜法海水淡化技术在海上油田稠油热采注汽工艺中应用的两大技术难题：1、海水泥沙含量大，水质波动大，现有膜法水处理系统的处理工艺抗冲击能力差，无法实现产水水质长时间保持稳定；2、现有膜法海水淡化工艺技术结构复杂，工程庞大，集成化程度低等特点，无法满足海上采油平台面积和空间有限的技术要求，提供一种海上油田稠油热采提供锅炉补给水的海水淡化工艺系统。
本发明主要是通过下述技术方案得以解决：
一种海上油田稠油热采提供锅炉补给水的海水淡化工艺系统，包括依次连接的超滤单元、脱盐单元和热力除氧单元，
其中，所述的超滤单元包括依次连接的海水提升泵、自清洗过滤器、板式换热器、管道混凝器和超滤膜，所述的超滤膜为陶瓷超滤膜；
所述的脱盐单元包括依次连接的产水缓冲罐、反渗透供水泵、保安过滤器、三级反渗透单元、电渗析单元组成；其中三级反渗透单元包括一级反渗透、二级反渗透和三级反渗透，每级反渗透的前端设有反渗透增压泵，后端连接有反渗透缓冲罐；其中所述的二级反渗透的浓水出口与产水缓冲罐的进口连接，电渗析单元的浓水出口与二级反渗透后端设置的反渗透缓冲罐，从而进入三级反渗透进行脱盐处理；
所述的热力除氧单元包括板式换热器和除氧器；
所述的超滤单元的超滤膜与脱盐单元的产水缓冲罐相连，所述的脱盐单元的三级反渗透后端的反渗透缓冲罐与热力除氧单元的板式换热器连接；
所述的除氧器的产水出口与换热器的换热介质进口相连，以为海水提供换热升温。
在本发明海水淡化工艺系统中，所述的热力除氧单元优选还包括减压减温装置，所述减温减压装置的减压阀为多级迷宫结构减压阀。
在本发明海水淡化工艺系统中，优选，超滤单元中所述的换热器为全焊接板式换热器，内衬换热板为钛材质；除氧单元所述的板式换热器为全焊接板式换热器，内衬换热板为316L不锈钢材质。
在本发明海水淡化工艺系统中，优选，反渗透的膜元件为卷板式膜。
本发明还进一步提供了一种采用上述海水淡化工艺系统进行膜法海水淡化的方法，包括如下步骤：
1)海水通过海水提升泵进入自清洗过滤器过滤去除粒径较大的杂质后，进入换热器升温，使用除氧产水进行升温至25-80℃，升温后加入混凝剂，随后进入超滤膜进行分离去除来水中 的油脂、小粒径悬浮物，使产水浊度达到进入反渗透膜的要求；
2)超滤膜产水进入产水缓冲罐与还原剂混合，通过供水泵供水加入阻垢剂和非氧化性杀菌剂进入安保过滤器；之后通过反渗透增压泵进入一级反渗透，反渗透膜产水进入反渗透缓冲罐；之后通过反渗透增压泵进入二级反渗透，反渗透膜产水进入缓冲罐，浓水返回至产水缓冲泵；之后通过反渗透增压泵进入三级反渗透，反渗透膜产水进入反渗透缓冲罐，浓水进入一级反渗透后端的反渗透缓冲罐后再通过二级反渗透进行处理；之后通过电渗析单元的供水泵进入电渗析装置，浓水进入二级反渗透后端的反渗透缓冲罐后再通过三级反渗透进行处理，电渗析产水通过供水泵进入热力除氧单元；
(3)电渗析产水进入除氧器与蒸汽混合除氧得到除氧产水，除氧产水通过过滤单元的换热器换热后作为锅炉补给水。
在本发明膜法海水淡化方法中，优选，步骤1)中所述的混凝剂为氯化铁、氯化铝、聚合氯化铝、氯化铝-聚丙烯酰胺中的一种或多种。
在本发明膜法海水淡化方法中，优选，所述超滤膜的过滤方式为错流过滤，浓缩比为1-10，根据进水水质进行调节。
在本发明膜法海水淡化方法中，优选，盐单元所述一级反渗透回收率为30-50％，所产生浓水排放；
脱盐单元所述二级反渗透回收率为80-90％，所产生浓水进入一级反渗透进行脱盐处理；
脱盐单元所述三级反渗透回收率为80-90％，所产生浓水进入二级反渗透进行脱盐处理；
脱盐单元所述EDI回收率为90-95％，所产生的浓水的70％进入三级反渗透进行脱盐处理，剩余30％排放。
在本发明膜法海水淡化方法中，优选，所述阻垢剂为六偏磷酸钠、三聚磷酸钠、羟基亚乙基二膦酸、三亚甲基膦酸、乙二胺四亚甲基膦酸钠、聚丙烯酸钠、水解聚马来酸酰中的一种；所述非氧化性杀菌剂为双氯酚、二氧氰基甲烷、异噻唑啉酮、十二烷基苄基氯化铵、十二烷基二甲基苄基溴化铵中的一种。
在本发明膜法海水淡化方法中，优选，所述还原剂使用二级反渗透产水进行配制。
本发明方法中海水依次通过超滤、脱盐和热力除氧三个单元，产水达到锅炉补给水的水质要求。其中超滤单元以无机超滤膜代替沉降+混凝+过滤的传统工艺，缩短了预处理的工艺流程，并且保证了预处理的水质，达到了反渗透膜的进水要求；脱盐单元使用三级反渗透+电渗析(EDI)在前端水质波动较大的情况下，可以保证产水总硬度达到锅炉补给水水质指标；热力除氧单元将脱盐单元产水进行脱氧，脱氧水对前端海水进行加热后，进入锅炉完成补水。
本发明海水淡化工艺系统及方法，与现有技术相比，具有如下有益效果：本发明使用陶瓷超滤膜对海水进行预处理，省去了沉降、过滤工序，缩短了预处理流程，提高了预处理长效抗大负荷污染冲击能力，适应海上复杂水质状况；在脱盐单元设置三级反渗透，在前端水质波动较大的情况下，满足EDI的进水要求，使整套海水淡化系统可以稳定运行；通过无机膜超滤、反渗透、EDI和低能耗深度脱氧工艺技术集成，开发工艺精简、装置紧凑、重量轻的补给水处理集成系统；降低废液排放量，减少膜设备损耗，大幅降低操作、运维工作强度，保证设备稳定达标运行。产水水质满足《GBT12145-2016》要求：溶解氧≤7μg/L、总硬度≤0.01mg/L、二氧化硅≤10μg/L、可溶性固体≤7000mg/L。
附图说明
附图是本发明海上油田稠油热采提高锅炉补给水的海水淡化工艺系统流程示意图。
图中，1为海水提升泵，2为自动反冲洗过滤器，3为板式换热器，4为管道混合器，5为超滤膜系统，6为产水缓冲罐，7为反渗透供水泵，8为保安过滤器，9为一级反渗透增压泵，10为一级反渗透，11为反渗透缓冲罐，12为二级反渗透增压泵，13为二级反渗透，14为反渗透缓冲罐，15为三级反渗透增压泵，16为三级反渗透，17为反渗透缓冲罐，18为EDI供水泵，19为EDI装置，20为板式换热器，21为热力除氧器。
具体实施方式
下面通过实施例，对本发明的技术方案做进一步具体说明。
实施例1:在渤海某平台应用本发明海水淡化工艺系统及工艺方法。海水温度平均值为2.1℃，海水浊度平均值为103.4NTU，电导率平均值为46000，溶解性总固体(TDS)平均值为31.5g/L。
采用本发明海上油区稠油热采注汽锅炉的膜法海水淡化工艺系统进行海水淡化，具体流程如下：
海水通过海水提升泵进入自清洗过滤器，过滤后进入换热器，使用除氧水进行升温，升温至25℃后加入混凝剂氯化铁；之后进入超滤膜进行处理，超滤膜产水进入产水缓冲罐与还原剂混合，通过供水泵供水加入阻垢剂三聚磷酸钠和非氧化性杀菌剂十二烷基苄基氯化铵进入反渗透安保过滤器；之后通过高压泵进入一级反渗透，反渗透膜产水进入缓冲罐；之后通过高压泵进入二级反渗透，反渗透膜产水进入缓冲罐；之后通过高压泵进入三级反渗透，反渗透膜产水进入缓冲罐；之后通过EDI供水泵进入EDI装置，EDI产水通过供水泵进入热力 除氧单元，浓水进入三级反渗透进行处理；EDI产水进入除氧器与减温减压后的低压蒸汽混合除氧，得到锅炉补给水。工艺设备连续运行30日，锅炉补给水平均总硬度为0.005mg/L，溶解氧平均值为4.5μg/L，二氧化硅平均值为5.1μg/L，可溶性固体平均值为500mg/L。
实施例2:在渤海某平台应用本工艺。海水温度平均值为13.5℃，海水浊度平均值为86.3NTU，电导率平均值为44500，溶解性总固体(TDS)平均值为32.1g/L。
采用本发明海上油田稠油热采注汽锅炉的膜法海水淡化工艺系统进行海水淡化处理，其处理步骤为：
海水通过海水提升泵进入自清洗过滤器，过滤后进入换热器，使用除氧水进行升温，升温至30℃后加入混凝剂氯化铁；之后进入超滤膜进行处理，超滤膜产水进入产水缓冲罐与还原剂混合，通过供水泵供水加入阻垢剂三聚磷酸钠和非氧化性杀菌剂十二烷基苄基氯化铵进入反渗透安保过滤器；之后通过高压泵进入一级反渗透，反渗透膜产水进入缓冲罐；之后通过高压泵进入二级反渗透，反渗透膜产水进入缓冲罐；之后通过高压泵进入三级反渗透，反渗透膜产水进入缓冲罐；之后通过EDI供水泵进入EDI装置，EDI产水通过供水泵进入热力除氧单元，浓水进入三级反渗透进行处理；EDI产水进入除氧器与减温减压后的低压蒸汽混合除氧，得到锅炉补给水。工艺设备连续运行30日，锅炉补给水平均总硬度为0.004mg/L，溶解氧平均值为3.8μg/L，二氧化硅平均值为4.2μg/L，可溶性固体平均值为550mg/L。
实施例3:在渤海某平台应用本工艺。海水温度平均值为28.1℃，海水浊度平均值为83.4NTU，电导率平均值为44300，溶解性总固体(TDS)平均值为30.1g/L。
海水通过海水提升泵进入自清洗过滤器，过滤后进入换热器，使用除氧水进行升温，升温至35℃后加入混凝剂聚合氯化铝；之后进入超滤膜进行处理，超滤膜产水进入产水缓冲罐与还原剂混合，通过供水泵供水加入阻垢剂三聚磷酸钠和非氧化性杀菌剂十二烷基苄基氯化铵进入反渗透安保过滤器；之后通过高压泵进入一级反渗透，反渗透膜产水进入缓冲罐；之后通过高压泵进入二级反渗透，反渗透膜产水进入缓冲罐；之后通过高压泵进入三级反渗透，反渗透膜产水进入缓冲罐；之后通过EDI供水泵进入EDI装置，EDI产水通过供水泵进入热力除氧单元，浓水进入三级反渗透进行处理；EDI产水进入除氧器与减温减压后的低压蒸汽混合除氧，得到锅炉补给水。工艺设备连续运行30日，锅炉补给水平均总硬度为0.004mg/L，溶解氧平均值为3.6μg/L，二氧化硅平均值为4.5μg/L，可溶性固体平均值为600mg/L。
以上所述仅为本发明的具体实施例，但本发明的结构特征并不局限于此，任何本领域的技术人员在本发明的领域，所做的变化或修饰皆涵盖在本发明的专利范围内。

Claims (10)

  1. 一种海上油田稠油热采提供锅炉补给水的海水淡化工艺系统，其特征在于，包括依次连接的超滤单元、脱盐单元和热力除氧单元，
    其中，所述的超滤单元包括依次连接的海水提升泵、自清洗过滤器、板式换热器、管道混凝器和超滤膜，所述的超滤膜为陶瓷超滤膜；
    所述的脱盐单元包括依次连接的产水缓冲罐、反渗透供水泵、保安过滤器、三级反渗透单元、电渗析单元组成；其中三级反渗透单元包括一级反渗透、二级反渗透和三级反渗透，每级反渗透的前端设有反渗透增压泵，后端连接有反渗透缓冲罐；其中所述的二级反渗透的浓水出口与产水缓冲罐的进口连接，电渗析单元的浓水出口与二级反渗透后端设置的反渗透缓冲罐，从而进入三级反渗透进行脱盐处理；
    所述的热力除氧单元包括板式换热器和除氧器；
    所述的超滤单元的超滤膜与脱盐单元的产水缓冲罐相连，所述的脱盐单元的三级反渗透后端的反渗透缓冲罐与热力除氧单元的板式换热器连接；
    所述的除氧器的产水出口与超滤单元的板式换热器的换热介质进口相连，为海水提供换热升温。
  2. 根据权利要求1所述的海水淡化工艺系统，其特征在于，所述的热力除氧单元还包括减压减温装置，所述减温减压装置的减压阀为多级迷宫结构减压阀。
  3. 根据权利要求1所述的海水淡化工艺系统，其特征在于，超滤单元中所述的板式换热器为全焊接板式换热器，内衬换热板为钛材质；除氧单元所述的板式换热器为全焊接板式换热器，内衬换热板为316L不锈钢材质。
  4. 根据权利要求1所述的海水淡化工艺系统，其特征在于，反渗透的膜元件为卷板式膜。
  5. 根据权利要求1所述的海水淡化工艺系统进行膜法海水淡化的方法，其特征在于，包括如下步骤：
    1)海水通过海水提升泵进入自清洗过滤器过滤去除粒径较大的杂质后，进入换热器升温，使用除氧产水进行升温至25-80℃，升温后加入混凝剂，随后进入超滤膜进行分离去除来水中的油脂、小粒径悬浮物，使产水浊度达到进入反渗透膜的要求；
    2)超滤膜产水进入产水缓冲罐与还原剂混合，通过供水泵供水加入阻垢剂和非氧化性杀菌剂进入安保过滤器；之后通过反渗透增压泵进入一级反渗透，反渗透膜产水进入反渗透缓冲罐；之后通过反渗透增压泵进入二级反渗透，反渗透膜产水进入缓冲罐，浓水返回至产水缓冲泵；之后通过反渗透增压泵进入三级反渗透，反渗透膜产水进入反渗透缓冲罐，浓水进 入一级反渗透后端的反渗透缓冲罐后再通过二级反渗透进行处理；之后通过电渗析单元的供水泵进入电渗析装置，浓水进入二级反渗透后端的反渗透缓冲罐后再通过三级反渗透进行处理，电渗析产水通过供水泵进入热力除氧单元；
    (3)电渗析产水进入除氧器与蒸汽混合除氧得到除氧产水，除氧产水通过过滤单元的板式换热器换热后作为锅炉补给水。
  6. 根据权利要求5所述的方法，其特征在于，步骤1)中所述的混凝剂为氯化铁、氯化铝、聚合氯化铝、氯化铝-聚丙烯酰胺中的一种或多种。
  7. 根据权利要求5所述的方法，其特征在于，所述超滤膜的过滤方式为错流过滤，浓缩比为1-10，根据进水水质进行调节。
  8. 根据权利要求5所述的方法，其特征在于，脱盐单元所述一级反渗透回收率为30-50％，所产生浓水排放；
    脱盐单元所述二级反渗透回收率为80-90％，所产生浓水进入一级反渗透进行脱盐处理；
    脱盐单元所述三级反渗透回收率为80-90％，所产生浓水进入二级反渗透进行脱盐处理；
    脱盐单元所述EDI回收率为90-95％，所产生的浓水的70％进入三级反渗透进行脱盐处理，剩余30％排放。
  9. 根据权利要求1所述的方法，其特征在于，所述阻垢剂为六偏磷酸钠、三聚磷酸钠、羟基亚乙基二膦酸、三亚甲基膦酸、乙二胺四亚甲基膦酸钠、聚丙烯酸钠、水解聚马来酸酰中的一种；所述非氧化性杀菌剂为双氯酚、二氧氰基甲烷、异噻唑啉酮、十二烷基苄基氯化铵、十二烷基二甲基苄基溴化铵中的一种。
  10. 根据权利要求1所述的方法，其特征在于，所述还原剂使用二级反渗透产水进行配制。
PCT/CN2021/139828 2020-12-29 2021-12-20 海上油田稠油热采提供锅炉补给水的海水淡化工艺系统 WO2022143272A1 (zh)

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