WO2013170507A1 - 一种回收重油开采采出水作为锅炉给水的水处理工艺 - Google Patents

一种回收重油开采采出水作为锅炉给水的水处理工艺 Download PDF

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Publication number
WO2013170507A1
WO2013170507A1 PCT/CN2012/076540 CN2012076540W WO2013170507A1 WO 2013170507 A1 WO2013170507 A1 WO 2013170507A1 CN 2012076540 W CN2012076540 W CN 2012076540W WO 2013170507 A1 WO2013170507 A1 WO 2013170507A1
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Prior art keywords
water
brine
falling film
film evaporator
heat exchange
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PCT/CN2012/076540
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English (en)
French (fr)
Inventor
彼得森⋅丹尼尔
卡尼纳伽⋅迪恩
马明
刘丰
李东
Original Assignee
江苏中圣高科技产业有限公司
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Priority to CA2863015A priority Critical patent/CA2863015C/en
Publication of WO2013170507A1 publication Critical patent/WO2013170507A1/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
    • 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
    • C02F1/08—Thin film evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/06—Evaporators with vertical tubes
    • B01D1/065—Evaporators with vertical tubes by film evaporating
    • 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
    • C02F1/042—Prevention of deposits

Definitions

  • the invention belongs to the field of water treatment, and relates to a water treatment process for recovering heavy oil extraction produced water as boiler feed water. Background technique
  • Heavy oil recovery involves injecting steam into the oil-bearing formation and recovering the oil-water mixture from the well.
  • the oil is separated from the water, and the separated water is produced water.
  • the produced water In order to recycle the produced water to produce steam, the produced water must be treated to meet the steam generator or boiler steam requirements.
  • SOR oil recovery ratio
  • the produced water needs to be treated to meet the boiler's use.
  • the two methods can be used individually or in combination.
  • Chemical water treatment removes hardness and silica, allowing treated water to be used in a single pass steam generator (OTSG).
  • Chemical methods used to treat produced water to make it suitable for use in OTSG typically include hot lime treatment, filtration, and ion exchange, where the hardness is removed below the detection limit and the silica is removed to a low level.
  • OTSG produces high pressure steam from low quality feed water with near zero hardness, low silica and total dissolved solids (TDS) levels up to 12,000 ppm.
  • TDS total dissolved solids
  • the OTSG produces a mixture of up to 80% water vapor and 20% brine (or boiler blowdown).
  • the water flow in the OTSG allows all heat transfer surfaces to be wetted by liquids, which minimizes dirt problems when producing steam. There are more dirt problems in boilers with more fluid processes. Whether the OTSG blowdown is separated from the steam depends on the quality of the steam required for the heavy oil layer.
  • the OTSG When dealing with produced water, the OTSG is considered a reliable boiler compared to conventional boilers or drum boilers.
  • the main advantage of OTSG over traditional boiler or drum boilers is the ability to produce high pressure steam from high TDS feed water.
  • Another advantage is that the OTSG can be cleaned by pipeline cleaning. If high quality water is used in the OTSG, it is usually not necessary to clean it for a long time.
  • the evaporative treatment process is superior to the chemical treatment process in producing high-quality distilled water from produced water for use as boiler feed water.
  • Evaporator distilled water from produced water has been successfully used in lOOOpsig drum boilers and 1500 psig OTSG. When the evaporator is supplied with water to the OTSG, the distilled water is used to benefit the OTSG and is rarely cleaned.
  • Evaporation typically recovers about 95% of the produced water as high quality distilled water. Recovery level with chemical composition and current The field needs to change. In general, the most energy efficient evaporator system concentrates produced water from 0.2 to 2.0% TDS to 10 to 15% TDS. Up to 25% of the total dissolved solids content can be achieved in the evaporation system, but this usually requires economic considerations because the thicker the treated brine, the higher the energy required for evaporation.
  • the physical and chemical processes in production are much more efficient than the evaporation process because physicochemical systems operate at lower cost and have been used to improve oil recovery for decades.
  • the evaporator requires a large amount of energy to evaporate water from the brine, and operating costs are an important economic factor in selecting the evaporation process.
  • the evaporator has been used to improve oil recovery for about 10 years, the evaporator is a relatively new technology compared to the physicochemical process.
  • the TDS of produced water is generally not high, but the need to replenish water may result in a process that processes TDS much higher than produced water.
  • Water loss in the rock layer, loss of oil treated water, boiler blowdown, steam removal, concentrated brine waste, etc. require the system to replenish a certain level of water to maintain water balance and steam production.
  • the main advantage of the evaporator is the high quality of the recovered water.
  • the boiler feed water has a non-volatile content of less than 2 PP m, which produces a small amount of blowdown in the boiler.
  • the obtained distilled water is directly sent to the boiler as feed water, and the blowdown amount of the boiler is less than 2%.
  • Conventional or steam drum boilers use a higher quality distilled water produced by the evaporator and have a working pressure of up to 1000 psig.
  • Conventional or steam drum boilers that use evaporator distilled water directly for more than 1000 psig, and many organizations recommend higher boiler water quality.
  • additional water treatment is required for the distilled water obtained from the produced water.
  • the main disadvantage of the evaporator compared to the hot lime softening process is the energy required to evaporate the salted produced water. Water changes from liquid The latent heat of gasification is higher, and the energy required is high. If no cheap steam is available, applying mechanical vapor compression as an energy source is generally an economical option. Adjusting the evaporator design can reduce energy costs, but increases equipment investment.
  • Any evaporation process must overcome the difficulties encountered in concentrating produced water with a high dissolved silicon content. All systems that increase crude oil production generally produce high silicon content produced water that will elute from the rock as it condenses in the formation. Some produced water contains not only silica which is easy to form hard scale, but also other compounds such as hardness or organic matter which are dissolved or incompatible. The chemical properties of reservoirs in different parts of the world are different. The main components in the produced water that cause fouling on the heat transfer surface of the evaporator will eventually stop the evaporator from working.
  • the evaporation process currently applied to northern Alberta, Canada is relatively new compared to the hot lime softening process. At least one evaporation process has not yet been commercialized.
  • the two main production water evaporation processes are as follows:
  • High pH process By adding alkali, the pH of the wastewater is greater than 12, so that the silica is dissolved in water without scaling on the evaporation surface. This process requires a large amount of alkali to be consumed. When high hardness is present, the high pH evaporation process cannot avoid scaling of high hardness components on the evaporation surface. If additives such as chelating or dispersing agents are used to inhibit hard component fouling, the system requires higher chemical costs. Several high pH evaporation units currently in use in Alberta require frequent cleaning or addition of large amounts of chemicals in addition to the large amount of alkali to avoid hard component fouling.
  • Adsorption slurry process The pH of the produced water is adjusted to 10-11 by adding magnesium oxide and a small amount of alkali. Magnesium is used to precipitate the silicon component and act as a seed to prevent scaling of silicon and other hard components. Due to the higher alkalinity of the brine (high carbonate content), the pH of the distilled water produced is lower (the bicarbonate in the brine decomposes to produce C0 2 ). Low quality distilled water requires additional facilities to remove C0 2 or add a base to the steam boiler to increase the pH of the distilled water (boiler feed water). However, the addition of alkali will cause an increase in the amount of boiler blowdown. Because boiler blowdown eventually circulates back to the evaporator, it results in higher operating costs. Several sets of adsorption slurry evaporation units are being built in Alberta, Canada, and will be completed in 2012 or 2013 and have not yet been commercialized.
  • Figure 1 and Figure 2 show the main equipment layout of the hot lime softening and evaporation process, respectively.
  • the suspended solids must be removed first to avoid clogging of the treatment well. Due to the high suspended solids and dissolved silicon content, the above two evaporation processes have problems in handling the concentrate. Once the concentrate enters the treatment well containing the lower pH natural water, precipitation occurs.
  • the high pH brine in the high pH process contains thousands of ppm of dissolved silicon that must be removed before the concentrate enters the deep well for disposal. If high levels of silicon are not removed, the concentrate will react with the natural water in the bilge well. After a short period of operation, the precipitated silicon will clog the treatment well. To remove silicon from the solution, acid is required, which is another major operating cost. The addition of acid to the concentrate produced by the high pH evaporation process produces very fine suspended particles of silicon that are difficult to settle or filter.
  • the adsorption slurry process precipitates silicon by adding magnesium to the evaporator.
  • the concentrate contains tens of thousands of ppm of suspended solids (mainly magnesium hydroxide and silicon compounds).
  • the brines of the above two evaporation processes contain fine and difficult to remove suspended solids. Long residence times are generally required to allow the suspended solids to settle.
  • the concentrated scum is concentrated to form a concentrated sludge using a reaction clarifier (slow rate of rise with sludge circulation). Even if the suspended solids are moderately concentrated, the concentrated slurry produced by filtration is still not commercially operated. If the suspended solids can be successfully separated, the resulting clear liquid is discharged into the sewage well and the resulting solids are sent to the landfill.
  • salt caves In order to solve the problem that the suspended solids in the brine is difficult to separate, many treatment companies use salt caves to settle the concentrated brine.
  • the salt cave provides a large volume of settled suspended solids.
  • the brine slurry is injected into the bottom of the salt cavern.
  • the brine discharged from the top of the salt cave is treated in a deep well.
  • the salt cave provides space for separation and storage of suspended solids in concentrated brine.
  • An object of the present invention is to provide a water treatment process for recovering heavy oil extraction produced water as boiler feed water in view of the above-mentioned deficiencies of the prior art.
  • Another object of the present invention is to provide a brine distributor for a vertical falling film evaporator used in the process.
  • the object of the present invention can be achieved by the following technical solutions:
  • a water treatment process for recovering heavy oil extraction produced water as boiler feed water conveying inflow water mainly based on produced water to a vertical falling film evaporator with a brine distribution device, and producing distilled water for boiler feed water by evaporation; Adding scrub particles to the circulating concentrated brine of the influent or vertical falling film evaporator mainly in the produced water to form a brine slurry, and using the vertical falling film evaporator to evaporate the brine slurry, using the solid in the brine slurry The particles prevent or reduce fouling on the heat transfer surface of the evaporator.
  • the produced water evaporation treatment process is combined with a brine slurry containing scrub particles which are circulated in the falling film evaporator.
  • the process is designated as the ShaVap process, and the invention is based on the fact that the evaporation system includes a scrubbing function of a brine slurry, a falling film evaporator, and a brine distribution device.
  • Figure 5 shows scrub particles and dirt particles suspended in a slurry flowing down the wall of the tube.
  • the ShaVap process adds the scrubbing granules to the circulating brine to form a brine slurry.
  • the particles rub against the heat transfer surface.
  • the silica, hardness, organic matter, etc. are removed before deposition on the tube wall, keeping the surface of the heat exchange tube clean, and the brine falling film is not concentrated.
  • the dirt component is deposited on the tube wall.
  • the added particles in the brine adhere to the added particles rather than adhering to the heat transfer surface of the evaporator.
  • the scrubbing particles are abrasive particles that are insoluble in the influent.
  • the choice of the particulate material is affected by the characteristics of the concentrated brine precipitates, and is selected from sand, gravel, glass beads or particles having a particle size greater than 0 and less than 100 microns. Other metal derivative particles having a particle density of rio g / cm 3 .
  • sand also silicon oxide
  • the choice of sand (also silicon oxide) as a filler particle not only scrubs the heat transfer surface but also sands the seed.
  • the concentration of the scouring particles in the brine slurry is preferably 0.5% - 5% ("%" means mass percentage).
  • the ShaVap evaporation process involves adding scrub particles to the two subsystems of the system.
  • One is a supplemental particle system that continuously adds supplemental particles to the system; a portion of the particles are added while the evaporator is driving.
  • Another subsystem is the particle recycling system, which recycles the particles back to the evaporator, saving the number of continuously added particles.
  • the replenishing particle system consists of a conventional solid slurry replenishing device that, depending on the size of the system, uses a solids feeder (such as a screw feeder) to store and move solid particles to a slurry mixing tank.
  • the slurry mixing tank mixes the scrubbing granules with a clear liquid (cooled distilled water or clear brine) and the resulting slurry stream can be fed directly to the evaporator through a recycle line or evaporator sink.
  • a solids feeder such as a screw feeder
  • the supplemental granule system is capable of producing a slurry with a scrubbing particle content of up to 50%, depending on the physical properties of the selected particles.
  • the particle recycle system separates the brine from the suspended scrub particles and other suspended components from the concentrate by conventional methods. Separation can be accomplished with a cyclone separator or a cone bottom tank, a centrifuge, a filter, and the like.
  • the scrubbing particles are preferentially removed by the circulation system because the selected scrubbing particles have a higher density than the precipitate formed in the influent.
  • the recycle stream contains more concentrated scrub particles, and the discharged brine stream or brine mixture stream contains more of the other suspended components resulting from the concentration of the feed.
  • the brine distribution device comprises a brine distribution tank at the top of the vertical falling film evaporator and a liquid distributor at the top of each heat exchange tube.
  • the liquid distributor is mainly composed of a guide body having a concave surface around the main body and a cross-sectional area of the bottom cover of the vertical falling film evaporator is larger than that of the cross-sectional area of the heat transfer tube of the vertical falling film evaporator, and
  • the fluid is movable or fixedly supported at a corresponding position in the upper portion of the heat transfer tube of the vertical falling film evaporator, so that the bottom edge of the top cover of the fluid guide is spaced apart from the upper surface of the upper tube of the vertical falling film evaporator to form a support for the liquid inlet channel Component composition; liquid enters along the concave passage of the inlet passage and the fluid guide and is distributed on the inner surface of the heat exchange tube.
  • the diameter of the bottom surface of the fluid guide is greater than or equal to 0.3 times the inner diameter of the heat exchange tube and smaller than the inner diameter of the heat exchange tube.
  • the upper surface of the fluid guiding tube exposes the upper end of the heat exchange tube to a height of 0.3 to 3 times the inner diameter of the heat exchange tube.
  • the conductive fluid is symmetrically distributed along the central axis of the heat exchange tube of the vertical falling film evaporator.
  • the top cover is hemispherical, plate-shaped, or any one of the bottom surfaces being flat, and the bottom area is larger than the shape of the heat transfer tube nozzle area.
  • the main body of the fluid guiding body has a smooth concave surface; or the main body of the fluid guiding body is connected from the top to the bottom by a rounded table body, a cylindrical body and a perfect circular table body without a gap to form a whole concave surface, and the bottom surface of the rounding table body
  • a cylinder with the same diameter as the bottom surface, and the bottom surface of the cylinder is connected with a perfect circular table body.
  • the diameter of the bottom surface of the cylinder is the same as the diameter of the top surface of the circular circular body; the diameter of the bottom surface of the circular circular body is greater than or equal to 0.3 times the inner diameter of the heat exchange tube, and is less than Heat pipe inner diameter.
  • the number of the supporting members is 2-6, which is a polygonal rib, one side of which is connected with the concave surface of the fluid guiding body, and at least two adjacent sides of the remaining sides are perpendicular to each other, and the supporting member depends on the adjacent vertical
  • the side frame is placed on the upper tube plate of the vertical falling film evaporator, so that the fluid guiding activity is fixed or fixedly supported at the corresponding position in the upper part of the heat transfer tube of the vertical falling film evaporator, and the bottom edge of the top cover of the fluid guiding body and the vertical falling film evaporation
  • the top surface of the upper tube sheet of the device forms a liquid inlet passage.
  • the support member is composed of 3 to 6 spiral blades connected to the bottom surface of the top cover and support pieces integrally connected downwardly at the lower end of each blade, and the diameter of the circle formed by the outer edge track of each blade tip is slightly larger than
  • the outer diameter of the heat exchange tube is such that the tip end of each vane is pressed against the upper port of the heat exchange tube or the upper tube plate, and the bottom edge of the top surface of the fluid guide is spaced apart from the top surface of the upper tube sheet of the vertical falling film evaporator.
  • the gap forms a liquid inlet passage
  • the height of the spiral portion of each blade ie, the vertical distance of the tip end of the spiral portion from the bottom surface of the fluid guide cap
  • the width of each support sheet corresponds to the inner wall of the heat exchange tube and the fluid guide
  • the distance between the outer walls is closely matched, so that the supporting piece of each blade abuts between the inner wall of the heat exchange tube and the outer wall of the corresponding position of the fluid guiding body, thereby guiding or supporting the fluid guiding body to the upper part of the heat exchange tube of the vertical falling film evaporator. Corresponding location.
  • the liquid distributor is mainly connected by a conical fluid having a concave surface, a fluid guiding activity or a fixed support to a corresponding position in the upper portion of the heat exchange tube of the vertical falling film evaporator, and a fluid guiding body.
  • the upper surface is formed by a support member that exposes the upper end of the heat exchange tube; the upper surface diameter of the fluid guide is larger than the outer diameter of the heat exchange tube, so that the upper edge of the concave surface of the fluid guide and the top surface of the upper tube plate of the vertical falling film evaporator A certain gap is formed between the inlet channels, and the liquid enters along the concave passage of the inlet passage and the fluid guide and is distributed on the inner surface of the heat exchange tube.
  • the diameter of the bottom surface of the fluid guide is greater than or equal to 0.3 times the inner diameter of the heat exchange tube and smaller than the inner diameter of the heat exchange tube.
  • the upper surface of the fluid guiding body exposes the upper end of the heat exchange tube to a height of 0.3 to 3 times the inner diameter of the heat exchange tube. Said fluid guide The central axis of the heat exchange tubes along the vertical falling film evaporator is symmetrically distributed.
  • the guiding fluid is surrounded by a smooth concave surface; or the guiding fluid is connected from the top to the bottom by a rounded table body, a cylindrical body and a perfect circular table body without a gap to form a whole concave surface, and the diameter of the upper surface of the rounded table body is larger than
  • the outer diameter of the heat pipe, the bottom surface of the rounded table body is connected with a cylinder having the same diameter as the bottom surface, and the bottom surface of the cylinder body is connected with a perfect circular table body, the diameter of the bottom surface of the cylindrical body is the same as the diameter of the top surface of the circular circular plate body;
  • the inner diameter of the heat pipe is 0.3 times and smaller than the inner diameter of the heat exchange tube.
  • the number of the support members is 2-6, which is a polygonal rib, one side is connected with the concave surface of the fluid guide, and at least two adjacent sides of the other sides are perpendicular to each other, and the support member depends on the adjacent vertical edge. It is placed on the upper tube plate of the vertical falling film evaporator, so that the fluid guide is movable or fixedly supported at the corresponding position in the upper part of the heat transfer tube of the vertical falling film evaporator, the bottom edge of the top cover of the fluid guide and the vertical falling film evaporator The top surface of the upper tube sheet forms a liquid inlet passage.
  • the brine slurry is distributed through the brine distribution tank to the upper tube sheet of the vertical falling film evaporator, and is immersed in the top of the fluid guide, and is formed between the bottom edge of the top cover and the upper tube sheet of the vertical falling film evaporator.
  • the liquid passage forms an inlet passage between the upper edge of the concave surface of the fluid guide and the top surface of the upper tube sheet of the vertical falling film evaporator to enter the liquid distributor inwardly and radially, and flows down the concave surface of the fluid guide to reach the guide. At the bottom of the fluid, the liquid flows outward toward the inner surface of the heat transfer tube.
  • the steam from the compressor or the external steam is condensed outside the heat exchange tubes to heat the heat exchange tubes, and the slurry in the tubes begins to evaporate (Fig. 5).
  • the liquid slurry (Fig. 5) and water vapor (Fig. 5) flow down together in the tube, exit at the lower tube sheet and enter the brine tank, which is pumped again into the brine distribution unit via the circulating pump together with the incoming water from the input brine tank.
  • the steam separates from the falling slurry and enters the defogging system at the annular gap of the evaporator sink.
  • the demisting system can be composed of several defogging forms, including blades, screens, liquid contacting devices, washing systems, or combinations thereof.
  • the demisting device of Figure 4 is a demisting device that can be used in an evaporator system. Other arrangements are possible, not exclusively demisting devices, and do not affect embodiments of the present invention.
  • the steam leaves the defogging system and is drawn into the compressor. If steam is used to evaporate the brine directly, the steam leaves the demisting system and enters the condenser. In the case of using a compressor, in order to have a temperature difference between the slurry boiling in the tube and the steam condensed outside the tube, the steam is compressed to a higher temperature. If steam is applied directly, it must have a sufficiently high pressure on the evaporator shell side to achieve the same heat transfer. In general, compression systems are more energy efficient than direct application of steam unless multiple evaporators are used to effect multiple evaporations.
  • the steam from the compressor or the external steam is condensed on the outer wall of the heat exchange tube in the shell side. Condensed water collects at the bottom of the shell side and flows into the distillation water tank.
  • the hot distilled water produced by the compressor drive or the hot distilled water produced by the steam heating is sent from the distilled water tank by the distilled water pump.
  • the hot distilled water is cooled in the incoming water from which the influent preheater is fed, as described above, while the influent water is heated.
  • the cooled distilled water is sent to the boiler system and may require further processing or direct use in the boiler.
  • Tables 2 and 3 give the water supply requirements for the drum boiler and the one-pass boiler (0TSG).
  • the produced water in the ShaVap evaporation process is preferably one or more of chemical dosing, preheating, and degassing.
  • the chemical dosing treatment can be set before the pre-heat treatment and degassing treatment, or after the pre-heat treatment and degassing treatment, before the evaporation treatment, it can also be directly added.
  • Evaporator brine tank Figure 4).
  • the inlet preheater (Fig. 4) and the degasser (Fig. 4) can be designed to be slurryed, or the evaporator system design can be adjusted to eliminate these pretreatment equipment, according to the entire plant integration shown in Figure 3. Depending on the needs.
  • the added chemicals depend on the chemical composition of the influent water. Chemicals include but are not limited to the following categories:
  • a scale inhibitor that prevents the formation of substances that may become dirt and prevents fouling of the inlet preheater, degasser, and evaporator.
  • Commonly used scale inhibitors are sodium nitrate, sodium phosphate, and the like.
  • a dispersing agent for preventing the deposit from adhering to the surface of the water inlet preheater or the degasser to form dirt Dispersants are also used to prevent solid particles from depositing on the heat transfer surfaces and other surfaces of the falling film evaporator to prevent the formation of fouling.
  • Commonly used dispersing agents are phosphate ester, polyethylene glycol and the like.
  • Acid used to lower the ra value.
  • Conventional practice is to add acid to the feed water tank to convert the basic carbonate and bicarbonate to carbon dioxide, which can be removed in the degasser. This technique eliminates the possibility of scaling of the calcium carbonate compound on the surface of the evaporator by removing an element of the compound.
  • Alkali used to increase the ra value.
  • Prior art applications add alkali to increase the ra value to dissolve the silica compound.
  • a soluble magnesium compound such as magnesium chloride dissolved in water, provides a source of magnesium for silica precipitation when the brine is concentrated in a falling film evaporator. This process is called the adsorption slurry process.
  • the water treatment process for recovering heavy oil extraction produced water as boiler feed water preferably comprises the following steps:
  • the degassed treated effluent enters the brine tank at the bottom of the vertical falling film evaporator, and a thick slurry containing a high concentration of scrubbing particles is added to the brine tank through the supplementary granule system to form the insoluble solution in the brine tank.
  • the concentration of the solid particles is 0.5% 5% of the slurry; the slurry is pumped into the brine distribution device at the top of the vertical falling film evaporator through a circulation pump, and distributed to each heat transfer through the liquid distributor of the brine distribution device.
  • the insoluble solid particles rub against the inner wall of the heat exchange tube, scrubbing off the dirt on the inner wall of the heat exchange tube; the obtained steam and the slurry flow downward together in the tube, and the steam enters the location
  • the defogging system at the annular gap of the evaporator brine tank is processed into a compressor for supplying thermal energy to the vertical falling film evaporator, or is condensed into a condenser to obtain cooled distilled water, and the slurry is placed under the vertical falling film evaporator.
  • the plate flows out and enters the brine tank for recycling; the particle recovery system is arranged on the brine circulation path for circulating the insoluble solid particles back to the vertical Falling film evaporator; vertical falling film evaporator heat exchanger tube outer wall is used to provide thermal energy steam exothermic condensation, collected at the bottom of the vertical falling film evaporator, into the distilled water tank, used for preheating of the incoming water to be cooled Distilled water.
  • a recovery heavy oil extraction produced water suitable for the ShaVap process as a water treatment system for boiler feed water comprising an evaporation system, a supplementary particle system, and a particle recovery system;
  • the evaporation system is a vertical falling film evaporator, including a brine tank, brine a distribution device, a vertical heat exchange tube, a circulation pump, a circulation line, and an energy driver for evaporation (which may be a compressor, or an external steam-attached condenser),
  • the supplementary particle system comprising a solid feeder, a slurry a mixing tank and a corresponding conveying pipeline
  • the particle recovery system is mainly composed of one selected from a cyclone separator, a cone bottom tank, a centrifuge or a filter, and a corresponding conveying pipeline;
  • the brine tank of the neutral falling film evaporator of the evaporation system is connected, and the thick slurry output pipeline of the supplementary particle system is connected with the brine tank or the
  • the brine distribution device includes a brine distribution tank at the top of the vertical falling film evaporator and a liquid distributor at the top of each heat exchange tube.
  • the water treatment system for recovering heavy oil extraction produced water as boiler feed water further comprises a further pre-water treatment system and/or a further concentration or crystallization system of concentrated brine, the feed water pretreatment system comprising a chemical treatment device and an evaporator One or more of a feed water pump, a preheating device, and a degasser; the further concentration or crystallization system of the concentrated brine comprises a concentrator or crystallizer; the concentrated brine is in a concentrator or crystallizer Further processing.
  • the chemical treatment apparatus includes a water inlet tank, a water tank agitator, and a chemical addition device, but the number of chemical addition devices is not limited to two, depending on the chemical composition of the influent water.
  • the mixed feed water enters the sink at a steady flow rate and composition.
  • Influent water includes produced water (typical composition is shown in Table 1), make-up water (two components are shown in Table 1), boiler blowdown, and possibly other plant wastewater, flow must be controlled, and individual components are mixed using traditional methods (eg Mix in a large sedimentation tank with a mixer).
  • the sink provides a mixing area with a blender.
  • the size of the inlet trough is generally calculated as a residence time of about 10 minutes, but should be determined by the chemical reaction that takes place.
  • the mixed feed water is adjusted by the added chemicals, it is sent from the feed water tank to the feed water preheater, and the feed water is heated by the hot distilled water from the distilled water pump in the feed water preheater.
  • the heated feed water enters the top of the degasser.
  • the degasser removes the non-condensable gas from the downward flowing influent with upward flowing steam. Some volatile components in hot water, such as light component organics, sulfides, ammonia compounds, etc., are removed. The most important thing is that the oxygen in the influent that causes the evaporator to corrode is removed.
  • the chemically treated and degassed feed water enters the vertical falling film evaporator brine tank.
  • a pump can be added to deliver the incoming water to the vertical falling film evaporator brine tank.
  • a transfer pump is installed there, and the magnesium oxide slurry is mixed with the deaerated feed water before entering the evaporator brine tank.
  • the purpose of adding chemicals here is to avoid clogging of the equipment as it passes through the water inlet preheater and degasser.
  • Figure 5 shows the liquid distributor at the top of a heat exchange tube in a vertical falling film evaporator in the ShaVap process.
  • the brine distribution tank at the top of the vertical falling film evaporator and the specially designed liquid distributor inserted in each heat exchange tube distribute the brine slurry evenly in the turbulent flow to the upper tube sheet of the vertical falling film evaporator. And inside the heat exchange tube.
  • the 360 degree entry of the brine slurry of the liquid distributor provides a thin layer of turbulence within the distribution box. This turbulence keeps all scrub particles suspended in the brine.
  • the present invention provides a key process for treating produced water from enhanced heavy oil recovery and reducing emissions from water treatment plants.
  • the process can be directly used to treat produced water, recovering more than 95%, and producing high quality boiler feed water for producing steam required for heavy oil production.
  • the process can also be used to treat boiler blowdown, thereby reducing plant emissions, mitigating physicochemical processing requirements, and increasing total water recovery from the water treatment plant.
  • the process includes a special falling film evaporation system that controls the formation of fouling while concentrating the produced water, processing most of the produced water into high quality distilled water that can be used in boiler feed water to increase the recovery rate of heavy oil.
  • Boiler feed water boiler water supply unit ( ⁇ 1000 psig) ( ⁇ 1001 psig)
  • Non-volatile TOC is reasonable ⁇
  • the ShaVap evaporation process of the invention can overcome the formation of hard scale by using inorganic salts such as silica, calcium sulfate, calcium carbonate, magnesium hydroxide and other metals and hardness compounds in the produced water, and can also overcome the formation of organic substances separated or precipitated in the brine during evaporation and concentration.
  • Dirt The particles suspended in the liquid polish the evaporating heat exchange surface to prevent the dirt particles from adhering to the tube wall, and this frictional effect of the particles prevents the evaporator from fouling.
  • Cheap sand, gravel, glass beads and other metal derivative particles can be used to polish the heat transfer surface.
  • the added suspended friction particles can also increase the heat transfer efficiency of the produced water having a high organic content.
  • the ShaVap process reduces the cost of chemicals and produces high quality distilled water for use in boilers that increase oil recovery.
  • the resulting distilled water is used directly in fast-fired boiler steam generation equipment up to 1000 psig and can also be used directly in single-pass steam generators (OTSG) or circulating tube boilers up to 1500 psig.
  • OTSG single-pass steam generators
  • a special structure liquid distributor is used to evenly distribute the brine slurry to the inner wall of the heat exchange tube, due to the liquid fraction
  • the cloth allows the slurry to flow horizontally from the 360° direction of the liquid distributor, and the flow characteristics in the equipment prevent suspended solids from depositing at the heat exchanger tubesheet.
  • the liquid distributor of the liquid distributor of the invention reduces the area of the low-speed region of the liquid on the one hand, thereby reducing the deposition of suspended solids; on the other hand, the inner wall of the heat-exchange tube is formed into a smooth liquid flow, and the amount of entrained bubbles is extremely small, and is more likely to form. A uniform liquid film.
  • the concave surface of the bottom of the liquid guide of the liquid distributor of the invention can reduce the amount of liquid droplets falling into the center of the heat exchange tube, so that the liquid can be more distributed to the inner wall of the heat exchange tube, thereby improving the evaporation efficiency.
  • FIG 1 shows the existing process for treating produced water from a steam-assisted gravity drainage (SAGD) heavy oil recovery unit using hot lime softening, filtration, and weak acid cation exchange.
  • SAGD steam-assisted gravity drainage
  • Figure 2 shows another prior art process in which the physicochemical process steps of Figure 1 are replaced with an evaporator system.
  • the evaporation process can be carried out with several different chemicals, corresponding to a high pH evaporation process, an adsorption slurry evaporation process, or a slurry evaporation process using calcium sulphate as a seed crystal to control fouling.
  • Figure 3 shows the process flow of the present invention, including a particle addition and recovery system to reduce the amount of primary chemical added.
  • the boiler shown in the figure can be selected from steam drum boiler or 0TSG boiler according to system requirements.
  • Figure 3 illustrates how the ShaVap evaporation process can be integrated into the overall enhanced crude oil production process.
  • Figure 3 is similar to the prior art shown in Figure 2.
  • the ShaVap evaporation system shown in Figure 3 is unique in that it includes a particle addition and recovery system that makes the ShaVap evaporation process different from existing technologies.
  • Figure 4 details the ShaVap process, which shows the specific implementation of the evaporator components and particle addition and particle recovery.
  • 8 is the heat exchange tube
  • 7 is the upper tube sheet
  • 11-1 and 11-2 are the dosing equipment
  • 12 is the sink mixer
  • 13 is the inlet tank
  • 14 is the inlet pump
  • 15 is the inlet preheater
  • 16 is the degasser
  • 17 is the vertical falling film evaporator
  • 18 is the brine tank
  • 19 is the brine distribution tank
  • 20 is the lower tube sheet
  • 21 is the circulation pump
  • 22 is the circulation pipeline
  • 23 is the compressor
  • 24 is The condenser
  • 25 is a supplementary particle system
  • 26 is a particle recovery system
  • 27 is a defogging system
  • 28 is a distilled water tank
  • 29 is a distilled water pump.
  • Figure 5 depicts how the scrub particles and the precipitated suspended soil solids flow together through the system.
  • a brine distributor was specifically designed to prevent the heavier scrub particles from depositing at the upper tubesheet of the vertical falling film evaporator.
  • 7 is the upper tube plate of the vertical falling film evaporator
  • 8 is the heat exchange tube of the vertical falling film evaporator
  • 10 is the liquid distributor.
  • 1 is the top plate
  • 2 is the rounded table body
  • 3 is the cylinder body
  • 4 is the circular circle body
  • 5 is the support member
  • 6 is the main body of the fluid guide
  • 7 is the upper tube plate of the vertical falling film evaporator
  • 8 is the stand Heat exchange tube of falling film evaporator
  • 9 is a fluid guide
  • 10 is a liquid Cloth.
  • Embodiment 1 Support member, wherein 5 is a support member and 7 is an upper tube sheet of a vertical falling film evaporator.
  • FIG. 9 Schematic diagram of the structure of the liquid distributor.
  • 1 is the top cover
  • 5 is the support member
  • 6 is the main body of the fluid guide
  • 7 is the upper tube plate of the vertical falling film evaporator
  • 8 is the heat exchange tube of the vertical falling film evaporator
  • 9 is the fluid guide
  • 10 For the liquid distributor.
  • Figure 10 is a bottom view of the support member, wherein 1 is a top cover and 5 is a spiral support member. Detailed description of the invention
  • a liquid distributor 10 for a vertical falling film evaporator as shown in FIG. 6 is mainly composed of a concave surface around the main body 6 and a bottom surface area of the top cover 1 is larger than that of the heat transfer tube 8 of the vertical falling film evaporator.
  • the fluid 9 and the movable fluid 9 are movably supported at corresponding positions in the upper portion of the heat exchange tube 8 of the vertical falling film evaporator, so that the bottom edge of the top cover 1 of the fluid guide 9 and the upper surface of the upper tube sheet 7 of the vertical falling film evaporator
  • the support member 5 is formed with a certain gap to form an inlet passage.
  • the fluid guiding body 9 is symmetrically distributed along the central axis of the heat transfer tube of the vertical falling film evaporator, and is composed of a main body 6 and a top cover 1.
  • the top cover 1 has a cap shape, and the bottom surface thereof is connected to the upper surface of the fluid guiding body 6 without a gap, and the bottom area is larger than the area of the heat transfer tube nozzle.
  • the diameter of the bottom surface of the fluid guiding body 6 is about 0.5 times the inner diameter of the heat exchange tube.
  • the number of the support members 5 is three, which are polygonal ribs (Figs.
  • the bottom edge of the top cover 1 of the fluid guiding body 9 forms a liquid inlet passage with the top surface of the upper tube sheet 7 of the vertical falling film evaporator.
  • the liquid forms an inlet passage between the bottom edge of the top cover 1 and the top surface of the upper tube sheet 7 of the vertical falling film evaporator to radially enter the liquid distributor 10 inwardly, and flows down the concave surface of the main body 6 of the flow guiding body, When reaching the bottom of the fluid guiding body 6, the liquid flows outward toward the inner wall of the heat exchange tube.
  • the flow rate of liquid entering the heat transfer tubes 8 is determined by the height of the feed channels.
  • the height of the inlet passage is 0.3 to 3 times the inner diameter of the heat exchange tube 8. According to the actual situation, the height of the inlet passage is changed by changing the shape of the support member 5, thereby adjusting the flow rate of each heat transfer tube.
  • a liquid distributor 10 for a vertical falling film evaporator as shown in FIG. 9 is mainly concave from the periphery of the main body 6 and has a top cover a guide body 9 having a bottom area larger than a nozzle area of the heat transfer tube 8 of the vertical falling film evaporator, and a movable guide body 9 movably supported at a corresponding position in the upper portion of the heat transfer tube 8 of the vertical falling film evaporator, so that the fluid guide body
  • the bottom edge of the top cover 1 of the 9 is composed of a support member 5 which is spaced apart from the top surface of the upper tube sheet 7 of the vertical falling film evaporator to form a liquid inlet passage.
  • the fluid guiding body 9 is symmetrically distributed along the central axis of the heat exchange tube of the vertical falling film evaporator, and the diameter of the bottom surface of the guiding fluid 9 is 0.6 times the inner diameter of the heat exchange tube 8.
  • the support member 5 is composed of four spiral blades connected to the bottom surface of the top cover 1 and a support piece integrally formed downward at the lower end of each blade (Fig. 10), and the diameter of the circle formed by the outer edge of each blade tip is slightly larger than the diameter of the circle.
  • the inner diameter of the heat pipe 8 is such that the tip end of each blade is pressed against the upper port of the heat exchange tube 8 or the upper tube sheet 7, and the bottom edge of the top cover 1 of the fluid guiding body 9 and the upper tube sheet 7 of the vertical falling film evaporator
  • the top surface is separated by a certain gap to form a liquid inlet passage, and the height of the spiral portion of each blade is the height of the inlet passage;
  • the width of each support piece is closely matched with the distance between the inner wall of the heat exchange tube 8 and the corresponding outer wall of the fluid guide, so that the blades are
  • the support piece abuts between the inner wall of the heat exchange tube 8 and the outer wall of the corresponding position of the fluid guide, so that the fluid guide 9 is movably or fixedly supported at a corresponding position in the upper portion of the heat exchange tube 8 of the vertical falling film evaporator.
  • the liquid forms a liquid inlet passage from the bottom edge of the top cover 1 and the top surface of the upper tube sheet 7 of the vertical falling film evaporator to enter the radiation inwardly, and enters the liquid distributor 10 in a spiral shape along the adjacent spiral blades.
  • the liquid is more easily distributed to the inner wall of the heat exchange tube, and the liquid enters the heat exchange tube and spirally flows down along the concave surface of the main body 1 of the fluid guide body. When reaching the bottom of the main body 1 of the fluid guide body, the liquid flows outward toward the inner wall of the heat exchange tube.
  • the flow rate of liquid entering the heat exchange tubes 8 is determined by the height of the inlet passage. According to the actual situation, the height of the inlet passage is changed by changing the shape of the support member 5, thereby adjusting the flow rate of each heat exchange tube.
  • Example 3
  • a water treatment system for recovering heavy oil extraction produced water as boiler feed water comprising an influent pretreatment system, an evaporation system, a supplementary particle system, and a particle recovery system.
  • the influent pretreatment system includes an influent pretreatment system including a chemical treatment unit, a water inlet preheater, and a degasser.
  • the chemical treatment device is composed of dosing devices 11-1, 11-2, a water inlet mixer 12, and a water inlet tank 13.
  • the inlet tank and the inlet preheater are connected by a feed water pump 14.
  • the influent water mainly from the produced water enters the water inlet tank, and the chemical treatment agent is added to the water supply tank 13 through the dosing equipment 11-1, 11-2, and is reacted under stirring of the water inlet mixer 12.
  • the chemically treated influent water is pumped into the influent preheater 15 by the feed water pump 14 to be preheated, and then enters the deaerator from the top of the deaerator 16 for degassing treatment, and the deaerated water enters the vertical state.
  • the evaporation system is a vertical falling film evaporator, comprising a brine tank 18, a brine distribution device, a vertical heat exchange tube 8, a circulation pump 21, a circulation line 22, and an energy driver for evaporation (which may be a compressor 23 or an external addition)
  • the steam is supplied with a condenser 24).
  • the supplemental granule system 25 comprises a conventional solids slurry replenishing device which, depending on the size of the system, uses a solids feeder (such as a screw feeder) to store and transfer the scouring granules to a slurry mixing tank, the slurry mixing tank
  • a solids feeder such as a screw feeder
  • the scrubbing granules and the clear liquid are mixed to form a high concentration of rub
  • the thick slurry of the washed particles can be directly added to the vertical falling film evaporator through a circulating pipe of a vertical falling film evaporator or a brine tank.
  • the supplemental particle system is capable of producing a slurry having a scrub particle content of up to 50%, depending on the physical properties of the selected particles.
  • the particle recovery system 26 separates the brine from the suspended scrub particles and other suspended components produced by concentration using conventional methods. Separation can be accomplished with a cyclone separator or a cone bottom tank, a centrifuge, a filter, and the like.
  • the concentrated brine input end and the particle output end of the particle recovery system are respectively connected to the circulating pipe of the vertical falling film evaporator, and the separated scrubbing particles are preferentially input into the circulating pipe to be removed, because the density of the selected scrubbing particles is higher than that of the influent The resulting precipitate is high, so that the recycle stream that is refluxed into the recycle line contains more scrub particles, and the discharged brine stream or the brine mixture stream fed to the supplemental particle system contains more of the other suspensions produced by the feed concentrate. ingredient.
  • the degassed influent water enters the brine tank 18 and is mixed with the scrubbing particle slurry input from the supplementary granule system 25 to form a scrubbing granule having a concentration of 0.5% by weight of the brine slurry, which falls in the heat exchange tube during the evaporation process.
  • the brine slurry is pumped together by a circulation pump to a brine distribution device at the top of the evaporator.
  • the brine distribution device is composed of a brine distribution tank 19 and a liquid distributor 10 (as described in Embodiment 1 or 2) inserted at the top of each heat exchange tube, and uniformly distributes the slurry in the upper tube sheet and the heat exchange tube in a turbulent flow form. .
  • the slurry enters the brine distribution tank 19 of the brine distribution unit, and the brine slurry is spread by the blades on the upper tubesheet 7 of the evaporator (Fig. 5).
  • the brine slurry enters the liquid distributor 10 in a thin layer of turbulence 360 degrees, and this turbulent flow keeps all the scrub particles uniformly suspended in the brine slurry.
  • the slurry is distributed along the outer surface of the liquid distributor while being displaced to displace the inner wall surface of the heat pipe 8, and the steam is condensed and heated outside the tube, and the inside of the tube begins to evaporate.
  • the brine slurry and water vapor flow down together in the tube and exit at the lower tube sheet 20.
  • the scrubbing particles are in contact with the inner wall of the heat exchange tube 8, and the scrubbing action keeps the surface of the tube clean, and the substance precipitated in the brine adheres to the added particles instead of adhering to the heat transfer surface of the evaporator, so the salt falling film is thick No dirt components are deposited on the tube wall during shrinkage.
  • the steam is separated from the falling brine into a defogging system 27 located in the annular gap of the vertical falling film evaporator brine tank.
  • the demisting system can be composed of several defogging forms, including blades, screens, liquid contacting devices, washing systems, or combinations thereof.
  • the steam leaves the defogging system and is drawn into the compressor 23. If the external source steam is used to heat the evaporated brine, the steam exits the defogging system and enters the condenser 24.
  • the distilled water obtained in the condenser can be used directly in fast-discharge steam generators up to 1000 psig or directly in single-pass steam generators (0TSG) or circulating tube boilers up to 1500 psig.
  • the steam from the compressor 23 or the external steam is condensed on the outer wall of the heat transfer tube 8.
  • the condensed water is collected at the bottom of the falling film evaporator 17 and flows into the distilled water tank 28.
  • the hot distilled water is sent to the influent preheater through the distilling water pump 29, and is cooled by the influent water while preheating the influent water in the influent preheater, and is cooled.
  • the distilled water can be used directly in fast-fired boiler steam generation equipment up to 1000 psig or directly used in single pass steam generators (0TSG) or circulating tube boilers up to 1500 psig.

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Abstract

本发明公开了一种回收重油开采采出水作为锅炉给水的水处理工艺。把以采出水为主的进水输送至带有盐水分布装置的立式降膜蒸发器，通过蒸发生产用于锅炉给水的蒸馏水；其中，向以采出水为主的进水中或立式降膜蒸发器的循环浓盐水中加入擦洗颗粒形成浆液，通过立式降膜蒸发器对浆液进行蒸发时，利用浆液中的固体粒子防止或减轻蒸发器换热面上的结垢。本工艺把采出水的大部分加工成可用于锅炉产蒸汽以提高重油采出率的高质量的蒸馏水，可直接用于处理采出水，回收量达95%以上，产出用于生产开采重油所需蒸汽的高质量锅炉给水。所述工艺也可用于处理锅炉排污，从而减少工厂的排放量，减轻物理化学处理的要求，增加水处理厂的总水回收量。

Description

一种回收重油开采采出水作为锅炉给水的水处理工艺
技术领域
本发明属于水处理领域， 涉及一种回收重油开采采出水作为锅炉给水的水处理工艺。 背景技术
重油开采包括把蒸汽注入含油层和从油井回收油 -水混合物。 油从水中被分离出来， 分离 后的水就是采出水。 为了循环使用采出水生产蒸汽， 采出水必须经过处理以满足蒸汽发生器 或锅炉产蒸汽的要求。
蒸汽注入重油层是广泛运用的提高石油采收率的方法。 通常每产出 1吨重油需要几吨蒸 汽， 蒸汽 /油比经常被称作油回收比 （SOR)。 因为 SOR值一般在 2~4， 用水量高， 所以环保 和经济方面鼓励把采出水处理成满足锅炉的给水， 用于生产注入含油层的蒸汽。
采出水需经过处理才能满足锅炉使用。 目前常用的处理工艺分为两种： 一种是通过 （物 理） 化学方法处理， 另一种是通过蒸发进行处理。 视处理对象的水质情况， 两种方法即可单 独使用， 也可组合使用。
化学水处理可除去硬度和硅石， 使处理过的水能用于一次通过蒸汽发生器 （OTSG )。 用 来处理采出水使之适合用于 OTSG 的化学方法典型地包括热石灰处理、 过滤和离子交换， 其 中硬度被除去达到低于检出限， 硅石被除去达到低水平。
OTSG可用近乎零硬度、 低硅石且总溶解固体 （TDS ) 含量高达 12000 ppm的低质量给水 产出高压蒸汽。 在蒸汽从盐水中蒸出时， OTSG基本上要求水被浓縮 5倍左右时给水要维持 盐的溶解度， 及具有低水平的硬度和硅石。
OTSG产生多达 80%的水蒸气和 20%盐水 （或锅炉排污） 的混合物。 在 OTSG内水流程让 所有换热表面有液体润湿， 产蒸气时使污垢问题最少。 在具有更多样的液体流程的锅炉内存 在更多的污垢问题。 OTSG排污是否和蒸汽分开取决于重油层所需的蒸汽质量。
在处理采出水时， 与传统的锅炉或汽包锅炉相比较 OTSG被认为是可靠的锅炉。 OTSG优 于传统的锅炉或汽包锅炉的主要优势是能够从高 TDS给水产出高压蒸汽。另一个优势是 OTSG 可用管线清管方法清洗。 如果高质量水被用于 OTSG, 通常长时间内不必清洗。
在从采出水生产高质量蒸馏水用作锅炉给水方面， 蒸发处理工艺优于化学处理工艺。 来 自采出水的蒸发器蒸馏水已成功用于 lOOOpsig汽包锅炉和 1500 psig OTSG。当用蒸发器向 OTSG 提供给水， 使用蒸馏水使 OTSG获益， 很少清洗。
蒸发通常情况下能回收约 95%的采出水作为高质量的蒸馏水。 回收水平随化学成分和现 场需求而变化。 一般而言， 最高效节能的蒸发器系统把采出水从 TDS 0.2~2.0%浓縮到 TDS 10~15%。 高达 25%的总溶解固体含量可以在蒸发系统内实现， 但是这通常需要考虑经济性， 因为处理的盐水越浓， 蒸发所需能量越高。
生产中物理化学工艺比蒸发工艺运用得多， 因为物理化学系统操作费用较低， 已被用于 提高石油采收几十年了。 蒸发器需要大量的能量从盐水中蒸发水， 在选择蒸发工艺时操作费 成为重要的经济因素。蒸发器虽已被用于提高石油采收 10年左右， 相对于物理化学工艺而言 蒸发器是相对较新的技术。
当人工成本不高时， 安装费也倾向于用物理化学系统。 随着安装人工费增加， 蒸发器最 终可以比大型物理化学系统便宜， 因为蒸发器系统在运抵现场前可以做成模块。
采出水的 TDS—般不高， 但是补充水的需求可能导致处理过程要处理比采出水高得多的 TDS。 岩石层内水损失、 油处理水损失、 锅炉排污处理、 排汽、 浓縮的盐水废物等要求系统补 充一定水平的水来维持水平衡和蒸汽生产。
有些地方， 例如加拿大阿尔伯塔省北部， 发现应用蒸汽采油需要补充大量的水。 如果使 用的是淡水， 通常硬度和硅石含量极少， 与盐、 硬度和硅石含量高的苦咸水相比 TDS很低， 需要水处理工艺处理的 TDS很少。 但是， 淡水在阿尔伯塔油砂的使用是受限制的， 当地政府 通过限制使用淡水和限制工厂盐水排放水平来保护淡水资源。 这就要求工厂使用高 TDS的盐 水， 水中钙、 镁、 硅等结垢成分含量高。
根据阿尔伯塔法律， 使用化学处理法 （如热石灰软化法） 的工厂必须考虑增加处理过程 来处理补充水和锅炉排污水， 以满足法定的补水和排放要求。 这就使蒸发成为首选的处理采 出水的主要工艺， 或者需要在下游增加蒸发过程来减少工厂的总排放量， 如 OTSG排污。
一旦在用蒸汽开采重油的地方出现环境限制的法规， 蒸发工艺就开始变得在经济上更具 吸引力了。 因为减少废弃物和限制使用淡水是大势所趋， 更多的蒸发系统将被用于处理采出 水。
与物理化学处理工艺相比， 应用蒸发器具有优势和劣势。
蒸发器的主要优势在于回收水的质量高。锅炉给水的不挥发物小于 2PPm，这种水在锅炉 内产生很少的排污量。 目前在采用蒸发器处理采出水的装置中， 把得到的蒸馏水作为给水直 接送进锅炉， 锅炉的排污量低于 2%。
传统的或汽包型锅炉应用蒸发器产出的更高质量的蒸馏水， 工作压力已高达 1000psig。现 在有很多关于把蒸发器蒸馏水直接用于超过 lOOOpsig的传统的或汽包型锅炉的讨论， 许多组 织推荐用更高的锅炉水质。 为了达到更高压力下的水质， 需要对从采出水得到的蒸馏水进行 额外的水处理。
与热石灰软化法相比， 蒸发器的主要缺点在于需要能量蒸发含盐的采出水。 水从液态变 成气态气化潜热较高， 需要的能量高。 如果没有便宜的蒸汽可用， 应用机械蒸汽压縮作为能 源一般是经济的选择。 调整蒸发器的设计可以减少能源成本， 但增加了设备投资。
最近 10年之内，传统的热石灰软化和离子交换被利用蒸汽压縮机驱动的降膜蒸发器的蒸 发工艺替代了。 两个有竞争力的蒸发工艺目前正在应用， 其中一个蒸发工艺已经上了几套装 置， 而另一个蒸发工艺将在 2012年的下半年首次商业化应用。 已应用的几个蒸发工艺都使用 了相同的降膜蒸发器设计， 仅仅在防止结垢形成的化学方法有所不同。 除了化学药品添加系 统， 进料的化学成分、 蒸发器内的盐水的化学成分和蒸发器都是相同的。
任何一个蒸发处理工艺都必须克服在浓縮高溶解硅含量的采出水时遇到的困难。 所有提 高原油采出的系统一般都产生高硅含量的采出水， 因为蒸汽在岩层内冷凝时硅会从岩石中溶 出。 有些采出水不仅含有容易形成硬垢的硅石， 而且还含有其他化合物， 如溶解或不互容的 硬度、 有机物等。 世界上不同地区的油藏的化学特性是不同的。 采出水中导致蒸发器换热面 结垢的主要成分最终会使蒸发器无法工作而停车。
易结垢的无机组分如碳酸钙、 硫酸钙、 氢氧化镁及其它重金属的化合物必须在蒸发工艺 中去除， 以使系统运行的更有效， 延长使用寿命。 热石灰软化工艺去除废水中的硅石及其它 易结垢组分， 而不会浓縮其余组分； 蒸发工艺脱去浓盐水中的水分， 会引起易结垢组分形成 悬浮固体， 一旦形成将在传热面上生成污垢。 应用在加拿大阿尔伯塔的两种采出水蒸发工艺 采用不同的处理结垢方法， 以实现蒸发系统的可操作性。
目前应用于加拿大阿尔伯塔北部的蒸发工艺相对于热石灰软化工艺而言是比较新的。 至 少有一种蒸发工艺还未商业化运行。 两个主要的采出水蒸发工艺如下：
( 1 ) 高 pH工艺： 通过加碱使废水的 pH值大于 12， 从而使硅石溶解于水中， 不会在蒸 发表面结垢。 此工艺需要消耗大量的碱。 当高硬度存在时， 高 pH蒸发工艺无法避免高硬度 组分在蒸发表面结垢。 如果用添加剂如螯合剂或分散剂抑制硬组分结垢， 那么系统需要更高 的化学药品成本。 目前在阿尔伯塔投用的几套高 pH蒸发装置除了消耗大量碱外， 需要经常 清洗或添加大量化学药剂， 以避免硬组分结垢。
(2) 吸附浆液工艺： 通过加入氧化镁和少量碱调节采出水的 pH在 10~11。 利用镁使硅 组分沉淀， 并起到晶种作用防止硅和其他硬组分结垢。 由于盐水碱度较高（碳酸盐含量高） ， 产生的蒸馏水的 pH较低 （盐水中重碳酸盐分解产生 C02) 。 低品质的蒸馏水需要额外的设 施脱除 C02， 或在蒸汽锅炉中添加碱以提高蒸馏水 （锅炉给水） 的 pH。 但加碱会引起锅炉排 污量增大。 因为锅炉排污最终循环回到蒸发器， 所以会导致更高的操作费用。 在加拿大阿尔 伯塔正在建设几套吸附浆液蒸发装置， 到 2012或 2013年竣工， 还未商业化运行。
以上两种蒸发工艺均会产生废液 （浓縮液） ， 废液必须进行后续处理或以不危害环境的 方式排放。 浓縮液的量取决于采出水的化学成分及系统补水的品质及水量。 相对于传统热石 灰软化工艺， 蒸发工艺产生的浓縮液体积少得多， 水的回收率更高， 因为蒸发工艺锅炉排污 更少， 要处置的浓縮液浓度更高。
图 1和图 2分别为热石灰软化和蒸发工艺的主要设备布置图。
如果蒸发系统产生的浓縮液去处理井， 必须先除去悬浮固体， 以免造成处理井堵塞。 由 于悬浮固体及溶解硅含量高， 以上两种蒸发工艺在处理浓縮液时存在问题， 一旦浓縮液进入 含有较低 pH天然水的处理井， 便会发生沉淀。
高 pH工艺中高 pH盐水含有数千 ppm的溶解硅， 在浓縮液进入深井处置前必须去除。 如果高含量的硅未被去除， 浓縮液会与污水井中的天然水反应， 短时间运行后， 沉淀出来的 硅就会堵塞处理井。 要去除溶液中的硅， 需要加酸， 这是另一项主要的运行成本。 向高 pH 蒸发工艺产生的浓縮液中添加酸， 会产生非常细小的硅的悬浮颗粒， 很难沉降或过滤。
吸附浆液工艺通过向蒸发器中加镁， 使硅析出。 当浓縮液出蒸发器时， 浓縮液含有几万 ppm的悬浮固体 （主要是氢氧化镁和硅化合物） 。
以上两种蒸发工艺的盐水中均含有细小且难以去除的悬浮固体。 一般需要较长的停留时 间以使悬浮固体沉降。 利用反应澄清器 （上升速度慢， 并带有污泥循环） 浓縮悬浮固体以形 成浓縮的污泥。 即便悬浮固体适度地浓縮， 用过滤方式处理产生的浓浆液仍没有商业化运行。 如果悬浮固体可以成功分离， 产生的澄清液被排入污水井， 产生的固体送到地上垃圾填埋场。
为解决蒸发器浓盐水中悬浮固体难以分离的问题，很多处理公司采用盐洞来沉降浓盐水。 盐洞提供了沉降悬浮固体的大容积。 盐水浆液被注入盐洞的底部。 从盐洞的顶部排出的盐水 去深井处理。 盐洞为浓盐水中的悬浮固体提供分离及储存的空间。
替代深井处理蒸发器浓縮液的另一种方法是用额外的蒸发设备分离可处理的固体。 在水 处理行业中， 这被叫做零排放。 对于高 pH浓縮液， 零排放已经实现， 但据报道设备维护要 求很高。 吸附浆液工艺还未在大规模装置上投用， 所以零排放设备的应用尚且未知。
在其他工业有几种蒸发工艺， 如硫酸钙盐种浓盐水， 可能被用于回收采出水， 并将回收 的水用作 OTSG 锅炉和传统锅炉 （汽包式锅炉） 给水。 不管采用何种工艺， 采出水蒸发工艺 要克服的困难是硅组分和硬组分易结垢， 从而影响蒸发系统的运行。 另外由于存在易挥发组 分， 如有机物和碳酸盐， 蒸发产生蒸馏水需要更多的生产成本， 因为这需要设置额外的水处 理设施， 锅炉的给水化学成分要求更高， 锅炉排污量更高。
发明内容
本发明的目的是针对现有技术的上述不足， 提供一种回收重油开采采出水作为锅炉给水 的水处理工艺。
本发明的另一目的是提供该工艺中使用的立式降膜蒸发器用盐水分布器
本发明的又一目的是提供回收重油开采采出水作为锅炉给水的水处理系统。 本发明的目的可通过如下技术方案实现：
一种回收重油开采采出水作为锅炉给水的水处理工艺， 把以采出水为主的进水输送至带 有盐水分布装置的立式降膜蒸发器， 通过蒸发生产用于锅炉给水的蒸馏水； 其中， 向以采出 水为主的进水中或立式降膜蒸发器的循环浓盐水中加入擦洗颗粒形成盐水浆液， 通过立式降 膜蒸发器对盐水浆液进行蒸发时， 利用盐水浆液中的固体粒子防止或减轻蒸发器换热面上的 结垢。
在本发明中， 采出水蒸发处理工艺与含有擦洗颗粒的盐水浆液结合， 所述盐水浆液在降 膜蒸发器内循环流动。本工艺被命名为 ShaVap工艺， 发明点在于蒸发系统包括有擦洗功能的 盐水浆液、 降膜蒸发器以及盐水分布装置。
图 5给出了悬浮于沿管壁向下流动的浆液中的擦洗颗粒和污垢颗粒。 ShaVap工艺把擦洗 颗粒加入到循环盐水中形成盐水浆液， 颗粒摩擦换热面， 硅石、 硬度、 有机物等在管壁上沉 积前就被除去， 保持换热管表面清洁， 盐水降膜浓縮时没有污垢成分沉积在管壁上。 加入的 颗粒除了具有擦洗作用之外， 盐水中析出的物质可粘附在所加入的颗粒上， 而不是粘附在蒸 发器换热面上。 所述的擦洗颗粒为不溶于进水的具有磨擦作用的固体颗粒， 颗粒材料的选择 受浓縮盐水析出物的特性影响， 选自颗粒尺寸大于 0且小于 100微米的沙子、 砂砾、 玻璃珠 或其他的金属衍生物颗粒， 颗粒密度为 riog/cm 3。 选择沙子（也是硅氧化物）作为加入颗 粒， 不仅能够擦洗换热表面而且沙子也作晶种用。
所述的盐水浆液中擦洗颗粒的浓度优选 0. 5% -5% ("%"表示质量百分比）。
ShaVap蒸发工艺包括把擦洗颗粒加入系统的两个子系统。 一个是补充颗粒系统， 把补充 颗粒连续地加入系统； 在蒸发器开车时加入一部分颗粒。另一个子系统是颗粒循环回收系统， 把颗粒循环回蒸发器， 可以节省连续添加的颗粒数量。
补充颗粒系统包含传统的固体浆料补充设备， 取决于系统大小， 这种系统使用一个固体 进料器 （如螺杆进料器） 贮存和移动固体颗粒到一个浆料混合槽。 浆料混合槽把擦洗颗粒和 清澈的液体 （冷却的蒸馏水或清澈的盐水） 混合， 形成的浆液流可以通过循环线或者蒸发器 水槽直接加入蒸发器。 这种设备存在多种选择， 在许多工业有应用。
补充颗粒系统能够生产擦洗颗粒含量高达 50%的浆料， 根据所选择颗粒的物理性质决定。 颗粒循环回收系统用传统的方法把盐水和悬浮的擦洗颗粒以及由浓縮生成的其他悬浮成分分 离。 分离可用旋流分离器或者锥底槽、 离心机、 过滤器等完成。 擦洗颗粒被循环系统优先除 去， 因为所选用的擦洗颗粒的密度比进水中生成的沉淀物高。循环物流含有更浓的擦洗颗粒， 排出的盐水物流或盐水混合物流含有更多由进料浓縮生成的其他悬浮成分。
本发明提供的盐水分布装置包括位于立式降膜蒸发器顶部的盐水分布箱和位于每根换热 管顶部的液体分布器。 作为本发明的一种优选方式， 所述的液体分布器主要由主体四周呈凹面且其顶盖底截面 积大于立式降膜蒸发器的换热管管口截面积的导流体， 以及将导流体活动或固定支撑于立式 降膜蒸发器的换热管内上部相应位置， 使导流体的顶盖底面边缘与立式降膜蒸发器的上管板 上表面间隔一定空隙形成进液通道的支撑部件组成； 液体沿所述的进液通道、 导流体的凹面 进入并分布于换热管内表面。
其中,所述的导流体的底面直径大于等于换热管内径的 0.3倍， 且小于换热管内径。 所述的导流体的上表面露出换热管上口的高度为换热管内径的 0.3~3倍。
所述的导流体沿立式降膜蒸发器的换热管的中心轴对称分布.
所述的顶盖为半球状、 板状， 或任意一种底面为平面， 且底面积大于换热管管口面积的 形状。
所述的导流体的主体四周呈光滑凹面； 或者所述的导流体的主体自上而下依次由倒圆台 体、 圆柱体、 正圆台体无间隙连接形成四周呈凹面的整体， 倒圆台体底面连有与底面直径相 同的圆柱体， 圆柱体底面连有正圆台体， 圆柱体底面直径与正圆台体顶面直径相同； 正圆台 体底面直径大于等于换热管内径的 0.3倍， 且小于换热管内径。
所述的支撑部件的个数为 2~6个， 为多边形筋板， 其一边与导流体的凹面无缝隙连接， 其余各边中至少有相邻两边相互垂直， 支撑部件依靠该相邻的垂直边架于立式降膜蒸发器的 上管板上， 使导流体活动或固定支撑于立式降膜蒸发器的换热管内上部相应位置， 导流体的 顶盖底面边缘与立式降膜蒸发器的上管板顶面形成进液通道。
或者所述的支撑部件由 3~6个连接在顶盖底面的成螺旋形的叶片及各叶片后部下端一体 向下连接的支撑片组成， 各叶片尖端外缘轨迹形成的圆的直径略大于换热管的外径， 使得各 叶片的尖端抵压在换热管的上端口上或上管板上， 导流体的顶盖底面边缘与立式降膜蒸发器 的上管板顶面间隔一定空隙形成进液通道， 各叶片螺旋部分的高度 （即螺旋部分的尖端距导 流体顶盖底面的垂直距离） 即为进液通道高度； 各支撑片的宽度与换热管内壁和导流体对应 位置外壁之间的距离紧密配合， 使得各叶片的支撑片紧靠在换热管内壁和导流体对应位置外 壁之间， 从而将导流体活动或固定支撑于立式降膜蒸发器的换热管内上部相应位置。
作为本发明的另一种优选方式， 所述的液体分布器主要由四周呈凹面的导流体、 将导流 体活动或固定支撑连接于立式降膜蒸发器的换热管内上部相应位置， 导流体的上表面露出换 热管上口的支撑部件组成； 所述的导流体上表面直径大于换热管的外径， 使导流体凹面的上 部边缘与立式降膜蒸发器的上管板顶面之间间隔一定空隙形成进液通道， 液体沿进液通道、 导流体的凹面进入并分布于换热管内表面。
所述的导流体的底面直径大于等于换热管内径的 0.3倍， 且小于换热管内径。
所述的导流体的上表面露出换热管上口的高度为换热管内径的 0.3~3倍。 所述的导流体 沿立式降膜蒸发器的换热管的中心轴对称分布。
所述的导流体四周呈光滑凹面； 或者所述的导流体自上而下依次由倒圆台体、 圆柱体、 正圆台体无间隙连接形成四周呈凹面的整体， 倒圆台体上表面直径大于换热管的外径， 倒圆 台体底面连有与底面直径相同的圆柱体， 圆柱体底面连有正圆台体， 圆柱体底面直径与正圆 台体顶面直径相同； 正圆台体底面直径大于等于换热管内径的 0.3倍， 且小于换热管内径。
所述的支撑部件的个数为 2~6个， 为多边形筋板， 一边与导流体的凹面无缝隙连接， 其 余各边中至少有相邻两边相互垂直， 支撑部件依靠该相邻的垂直边架于立式降膜蒸发器的上 管板上， 使导流体活动或固定支撑于立式降膜蒸发器的换热管内上部相应位置， 导流体的顶 盖底面边缘与立式降膜蒸发器的上管板顶面形成进液通道。
盐水浆液通过盐水分布箱分布到立式降膜蒸发器的上管板上， 并浸过导流体顶部， 并从 顶盖的底面边缘与立式降膜蒸发器的上管板上面之间形成进液通道或者从导流体凹面的上部 边缘与立式降膜蒸发器的上管板顶面之间形成进液通道以向内的放射线状进入液体分布器， 沿导流体的四周凹面流下， 到达导流体底部时， 液体以向外的放射线状流向换热管内表面。 当盐水通过分布器均匀地分布在所有换热管中， 来自压縮机的蒸汽或外供蒸汽在换热管外冷 凝对换热管进行加热， 管内浆液开始蒸发 （图 5 ) 。 液体浆料 （图 5 ) 和水蒸汽 （图 5 ) 在管 内一起向下流动， 在下管板处流出后进入盐水槽， 与输入盐水槽的进水一起经循环泵再次泵 入盐水分布装置。 蒸汽与降落的浆液分离， 进入位于蒸发器水槽的环形空隙处的除雾系统。
除雾系统可由几种除雾形式组成， 包括叶片、 丝网、 液体接触装置、 洗涤系统或者是它 们的组合。 图 4中的除雾装置是可用于蒸发器系统的除雾设备。 其他安排布置是可能的， 不 完全是除雾装置， 不影响本发明的实施方案。
蒸汽离开除雾系统， 被吸入压縮机。 如果直接应用蒸汽加热蒸发盐水， 蒸汽离开除雾系 统进入冷凝器。 在使用压縮机的情况下， 为了管内沸腾的浆液和管外冷凝的蒸汽有一个温度 差， 蒸汽被压縮至更高的温度。 如果直接应用蒸汽， 其必须在蒸发器壳侧具有足够高的压力 来实现同样的换热。 一般而言， 压縮系统比直接应用蒸汽具有更高的能效， 除非用几个蒸发 器多效蒸发。
来自压縮机的蒸汽或者外供蒸汽， 在壳侧内的换热管外壁冷凝。 冷凝水在壳侧的底部汇 集后流入蒸馏水罐。
压縮机驱动产生的热蒸馏水或使用蒸汽加热产生的热蒸馏水从蒸馏水罐被蒸馏水泵输 送。 热蒸馏水在进水预热器被进来的进水冷却， 如前所述， 同时进水被加热。
冷却后的蒸馏水被送至锅炉系统， 可能需要进一步处理或者直接用于锅炉。 表 2和表 3 分别给出了汽包锅炉和一次通过锅炉 （0TSG) 的给水要求。
ShaVap蒸发工艺中采出水优选经化学加药处理、 预热处理、 脱气处理中的一项或多项处 理后进入立式降膜蒸发器； 所述的化学加药处理可设置在预热处理、 脱气处理之前， 也可设 置在预热处理、 脱气处理之后， 蒸发处理之前， 还可以直接加入蒸发器盐水槽 （图 4)。 进水 预热器（图 4)和脱气器（图 4)可以被设计成可进浆料， 或者蒸发器系统设计调整为不要这 些预处理设备， 根据图 3中所示的整个工厂的集成需求而定。
添加的化学药品根据进水的化学组成而定。 化学药品包括但不限于以下种类：
( 1 )污垢抑制剂， 用于防止可能变成污垢的物质生成， 预防进水预热器、 脱气器和蒸发器结 垢。 常用的污垢抑制剂为硝酸钠、 磷酸钠等。
( 2 )分散剂， 用于防止沉淀物粘附在进水预热器、 脱气器的表面而形成污垢。 分散剂也用于 防止固体颗粒在降膜蒸发器的换热表面及其他表面上沉积， 防止生成污垢。 常用的分散剂有 磷酸脂、 聚乙二醇等。
( 3 ) 消泡剂， 用于防止在包括进水预热器、 脱气器和蒸发器的系统内生成泡沫。
( 4) 酸， 用于调低 ra值。 常规的做法是在进水槽中加入酸， 把碱性的碳酸盐和重碳酸盐转 化成二氧化碳， 生成的二氧化碳可在脱气器内除去。 这种技术通过除去化合物的某个元素来 排除碳酸钙类化合物在蒸发器表面上的结垢的可能。
( 5 ) 碱， 用于调高 ra值。 现有技术应用加碱提高 ra值来溶解硅石化合物。
( 6 ) 可溶性镁化合物， 如溶于水的氯化镁， 在降膜蒸发器浓縮盐水时为硅石析出提供镁源。 这个工艺被叫做吸附浆液工艺。
为改善下游处理过程的性能， 其他的化学药品可以按一定比例加入到蒸发器内除去所有 的碳酸盐 （CaC03) 。 形成的 CaC03固体颗粒帮助钙及其他硬度成分粘附在添加熟石灰所形成 的晶种上。 除了用 CaC03晶种控制结垢之外， 把重碳酸盐转化成固态的碳酸盐， 消除了可挥发 到蒸馏水中的 C02生成， C02使蒸馏水不适合直接用于锅炉。 所述的一种回收重油开采采出水作为锅炉给水的水处理工艺优选包括以下步骤：
( 1) 以采出水为进水， 向其中添加化学药剂进行化学处理， 出水经预热后进行脱气处理；
( 2)经脱气处理的出水进入立式降膜蒸发器底部的盐水槽， 同时通过补充颗粒系统向盐水槽 中加入含高浓度的擦洗颗粒的浓浆， 使盐水槽中形成所述的不溶固体颗粒的浓度为 0. 5% 5% 的浆液； 所述的浆液经循环泵泵入立式降膜蒸发器顶部的盐水分布装置中， 通过盐水分布装 置的液体分布器分布到每根换热管中， 浆液在换热管中蒸发的过程中， 所述的不溶固体颗粒 与换热管内壁摩擦， 擦洗掉换热管内壁的污垢； 所得蒸汽和浆液在管内一起向下流动， 蒸汽 进入位于蒸发器盐水槽的环形空隙处的除雾系统处理后进入压縮机用于为立式降膜蒸发器提 供热能， 或者进入冷凝器冷凝得到冷却的蒸馏水， 浆液在立式降膜蒸发器下管板处流出， 进 入盐水槽循环使用； 颗粒回收系统设置在盐水循环通路上， 用于将不溶固体颗粒循环回立式 降膜蒸发器； 立式降膜蒸发器换热管外壁用于提供热能的蒸汽放热冷凝后， 在立式降膜蒸发 器底部汇集， 进入蒸馏水罐， 用于进水的预热后得到冷却的蒸馏水。 一种适用于 ShaVap工艺的回收重油开采采出水作为锅炉给水的水处理系统，包含蒸发系 统、 补充颗粒系统、 颗粒回收系统； 所述的蒸发系统即立式降膜蒸发器， 包含盐水槽、 盐水 分布装置、 立式换热管、 循环泵、 循环管道以及用于蒸发的能量驱动器 （可以是压縮机， 或 者是外加蒸汽附带冷凝器）， 所述的补充颗粒系统包含固体进料器、浆料混合槽及相应的输送 管道， 所述的颗粒回收系统主要由选自旋流分离器、 锥底槽、 离心机或过滤器中的一种及相 应的输送管道组成； 以采出水输送管道与蒸发系统中立式降膜蒸发器的盐水槽相连， 补充颗 粒系统的浓浆输出管道与立式降膜蒸发器的盐水槽或循环管道相连， 颗粒回收系统的浓盐水 输入端及颗粒输出端分别与立式降膜蒸发器的循环管道相连。
所述的盐水分布装置包括位于立式降膜蒸发器顶部的盐水分布箱和位于每根换热管顶部 的液体分布器。
所述的回收重油开采采出水作为锅炉给水的水处理系统还包括进水前处理系统和 /或浓 盐水的进一步浓縮或结晶系统， 所述的进水前处理系统包括化学处理装置、 蒸发器进水泵、 预热装置及脱气装置中的一种或多种； 所述的浓盐水的进一步浓縮或结晶系统包含浓縮器或 结晶器； 浓縮的盐水在浓縮器或结晶器中得到进一步处理。
所述的化学处理装置包含进水槽、 进水槽搅拌器、 化学药品添加装置， 但化学药品添加 装置的数量不限于 2个， 视进水的化学组成而定。
在图 4中， 混合进水以稳定的流量和组成进入进水槽。 进水包括采出水 （典型的组成见 表 1 ) 、 补充水 （两个组成示例于表 1 ) 、 锅炉排污、 以及可能的其他的工厂废水， 流量必须 控制， 各个成分应用传统方法进行混合 （如在带有混合器的大沉淀槽中混合） 。
进水槽提供了一个带有搅拌器的混合场所。进水槽的尺寸一般按约 10分钟的停留时间计 算， 但是应由所发生的化学反应具体确定。
混合进水经添加化学药品调整后， 被进水泵从进水槽输送至进水预热器， 进水在进水预 热器内被来自蒸馏水泵的热蒸馏水加热。 被加热的进水进入脱气器的顶部。 脱气器用向上流 动的蒸汽脱除向下流动的进水中的不凝气。热水中的一些挥发成分如轻组分有机物、硫化物、 氨化合物等被脱除。 最重要的是进水中的可导致蒸发器腐蚀的氧气被脱除了。
经化学处理和脱气的进水进入立式降膜蒸发器盐水槽。 根据设备布置， 可以选择加一个 泵输送进水到立式降膜蒸发器盐水槽。 在现有的技术吸附浆法中， 为了减少水的硬度和除去 硅石， 输送泵被安装在此处， 在进入蒸发器盐水槽之前把氧化镁浆料与脱气的进水混合。 在 此处加入化学药品的目的在于避免浆料经过进水预热器和脱气器时造成设备堵塞。 当 ShaVap蒸发系统运行时，加入的颗粒擦洗作用和所选择的盐水分布装置的作用变得很 显然。 图 5给出了 ShaVap工艺中的立式降膜蒸发器某根换热管顶部的液体分布器。位于立式 降膜蒸发器顶部的盐水分布箱以及特殊设计的插在每根换热管上的液体分布器一起， 以湍流 形式把盐水浆液均匀地分布在立式降膜蒸发器的上管板和换热管内。 液体分布器的盐水浆液 360度进入的设计在分布箱内提供了薄层湍流。 这种湍流保持所有擦洗颗粒悬浮在盐水中。 本发明提供了一种处理来自提高重油开采的采出水和减少水处理厂排放的关键工艺。 所 述工艺可直接用于处理采出水， 回收量达 95%以上， 产出用于生产开采重油所需蒸汽的高质 量锅炉给水。 所述工艺也可用于处理锅炉排污， 从而减少工厂的排放量， 减轻物理化学处理 的要求， 增加水处理厂的总水回收量。 本工艺包含一个特别的降膜蒸发系统， 在浓縮采出水 的同时控制污垢形成， 把采出水的大部分加工成可用于锅炉给水以提高重油采出率的高质量 的蒸馏水。 采出水处理系统的化学组成
采出水 补充水 （淡水） 补充水 （咸水） 钙 (Ca) 20 6 130
10 2 112
钠 (Na) 1004 968 6335 硫酸根 （so4 2— ) 70 8 140
氯 (CD 1310 1100 9173
碳酸氢根 （HC03— ) 429 687 1800
碳酸根 （co3 2— ) 2 4 10 硅石 （Si02) 195 5 8 总溶解固体 （TDS ) 3040 2780 17708 悬浮固体 （SS ) 〈25 <2 〈10 总有机碳 （T0C) 200 〈1 35
油脂 20 〈1 〈1
pH 7. 9 8. 0 8. 0
inn/ 185 41 41 表 2 汽包锅炉给水要求
锅炉给水 锅炉给水 单位 (≤ 1000 psig) (≥1001 psig)
溶解氧 <0. 007 <0. 007 ppm
铁 ≤0. 02 ≤0. 02 ppm
铜 ≤0. 01 ≤0. 01 ppm
硬度 ≤0. 05 不可检出 ppm (CaC03)
pH ( 25°C ) 8. 8-9. 6 8. 8-9. 6
不挥发 T0C <0. 2 <0. 2 ppm (C)
油性物质 <0. 2 <0. 2 ppm 表 3 OTSG锅炉给水要求
锅炉给水
(≤ 1800 psig)
溶解氧 可忽略 ppm
铁 ≤0. 25 ppm
TDS ≤ 12000 ppm
硬度 ≤0. 5 ppm (CaC03)
Si02 ≤50 ppm
pH ( 25°C ) 7. 5-9. 0
不挥发 TOC 合理 ―
油性物质 ≤0. 5 ppm 有益效果：
本发明 ShaVap蒸发工艺可以克服采出水中的硅石、硫酸钙、碳酸钙、氢氧化镁以及其他 金属、 硬度化合物等无机盐形成硬垢， 也可以克服蒸发浓縮时盐水中分离或析出的有机物形 成的污垢。 悬浮在液体中的颗粒抛光蒸发换热表面， 防止污垢颗粒粘附在管壁上， 颗粒的这 种摩擦效果防止了蒸发器结垢。 价格便宜的沙子、 砂砾、 玻璃珠及其他的金属衍生物颗粒可 以用于抛光换热表面。 此外， 所加入的悬浮摩擦颗粒还可以提高有机物含量高的采出水的传 热效率。
ShaVap工艺减少了化学药品成本， 生产高质量蒸馏水用于提高采油率的锅炉产蒸汽。 所 得到的蒸馏水被直接用于压力高达 1000 psig的快装锅炉蒸汽发生设备， 也可被直接用于压 力高达 1500 psig的一次通过式蒸汽发生器 (OTSG)或循环管式锅炉。
本发明中使用特殊结构的液体分布器将盐水浆液均匀分布与换热管内壁， 由于该液体分 布器可使浆液从液体分布器的 360° 方向水平流入， 设备中液流特性可避免悬浮固体在换热 器管板处沉积。
本发明液体分布器导流体的构造一方面縮小了液体低速区的面积， 从而可以减少悬浮固 体的沉积； 另一方面促使换热管内壁形成光滑的液流， 夹带的气泡量极少， 更易形成均匀液 膜。
本发明液体分布器导流体底部的凹面可减少落入换热管中心的液滴量， 使液体能够更多 的分布到换热管内壁， 提高蒸发效率。 附图说明
图 1所示为处理蒸汽辅助重力排泄 （SAGD ) 重油开采装置产生的采出水的现有的工艺， 应用了热石灰软化、 过滤、 弱酸阳离子交换。 这是处理采出水的最传统工艺， 并通常与 0TSG 配套使用， 0TSG可利用该物理化学处理工艺产生的低品质水发生蒸汽。
图 2所示是另外一种现有的工艺， 用蒸发器系统代替图 1中的物理化学工艺步骤。 蒸发 工艺可以有几种不同的化学药品添加， 相应有高 pH蒸发工艺、 吸附浆液蒸发工艺、 或利用硫 酸钙作为晶种控制结垢的晶浆蒸发工艺。
图 3所示为本发明的工艺流程， 包括颗粒添加与回收系统， 从而减少主要化学试剂的添加 量。 图中所示的锅炉可根据系统要求选用汽包式锅炉或 0TSG锅炉。 图 3说明如何把 ShaVap 蒸发工艺集成到总的提高原油采出工艺。 图 3类似于如图 2所示的现有技术。 图 3所示的 ShaVap蒸发系统的独特性在于它包括颗粒添加和回收系统， 这使得 ShaVap蒸发工艺不同于 现有的技术。
图 4详细描述了 ShaVap工艺，图中给出了蒸发器的组件和颗粒添加及颗粒回收的具体实 施。
其中 8为换热管， 7为上管板， 11-1和 11-2为加药设备， 12为进水槽混合器， 13为进 水槽， 14为进水泵， 15为进水预热器， 16为脱气器， 17为立式降膜蒸发器， 18为盐水槽， 19为盐水分布箱， 20为下管板， 21为循环泵， 22为循环管道， 23为压縮机， 24为冷凝器， 25为补充颗粒系统， 26为颗粒回收系统， 27为除雾系统， 28为蒸馏水罐， 29为蒸馏水泵。
图 5描述了擦洗颗粒与析出的悬浮污垢固体如何一起流经系统。 针对该工艺， 专门设计 了一种盐水分布器， 避免较重的擦洗颗粒在立式降膜蒸发器的上部管板处沉积。
其中， 7为立式降膜蒸发器的上管板， 8为立式降膜蒸发器的换热管， 10为液体分布器。
图 6、 实施例 1液体分布器的结构示意图。
其中 1为顶板， 2为倒圆台体， 3为圆柱体， 4为正圆台体， 5为支撑部件， 6为导流体的主 体， 7为立式降膜蒸发器的上管板， 8为立式降膜蒸发器的换热管， 9为导流体， 10为液体分 布器。
图 7、 实施例 1支撑部件， 其中 5为支撑部件， 7为立式降膜蒸发器的上管板。
图 8、 实施例 1支撑部件， 其中 5为支撑部件。
图 9、 实施例 2液体分布器的结构示意图。 其中 1为顶盖， 5为支撑部件， 6为导流体的 主体， 7为立式降膜蒸发器的上管板， 8为立式降膜蒸发器的换热管， 9为导流体, 10为液体 分布器。
图 10、 实施例 2支撑部件仰视图， 其中， 1为顶盖， 5为螺旋支撑部件。 发明详述
具体实施方式
以下结合附图对本发明的保护范围做举例说明， 但不作为对本发明保护范围的限制。 实施例 1
一种如图 6所示的立式降膜蒸发器用液体分布器 10， 主要由主体 6四周呈凹面且其顶盖 1底面积大于立式降膜蒸发器的换热管 8管口面积的导流体 9，以及将导流体 9活动支撑于立 式降膜蒸发器的换热管 8内上部相应位置， 使导流体 9的顶盖 1底面边缘与立式降膜蒸发器 上管板 7上表面间隔一定空隙形成进液通道的支撑部件 5组成。 导流体 9沿立式降膜蒸发器 的换热管的中心轴对称分布， 由主体 6和顶盖 1组成。 顶盖 1呈帽状， 其底面与导流体主体 6的上表面无缝隙相连， 且底面积大于换热管管口面积。 导流体主体 6底面直径约为换热管 内径的 0.5倍。 支撑部件 5的个数为 3个， 为多边形筋板 （图 7~8)， 其一边与导流体主体 6 的凹面无缝隙连接， 一边与顶盖 1的底面边缘无缝隙连接， 其余各边中至少有相邻两边相互 垂直， 支撑部件 5依靠该相邻的垂直边架于立式降膜蒸发器的上管板 7上， 使导流体 9活动 支撑于立式降膜蒸发器的换热管 8内上部相应位置， 导流体 9的顶盖 1底面边缘与立式降膜 蒸发器上管板 7顶面形成进液通道。
液体从顶盖 1的底面边缘与立式降膜蒸发器的上管板 7顶面之间形成进液通道以向内的 放射线状进入液体分布器 10， 沿导流体主体 6的四周凹面流下， 到达导流体主体 6底部时， 液体以向外的放射线状流向换热管内壁。
进入换热管 8 的液体流速由进液通道的高度决定。 进液通道的高度为换热管 8 内径的 0.3~3倍。根据实际情况， 通过改变支撑部件 5的形状来改变进液通道的高度， 从而调节每根 换热管的流量。 实施例 2
一种如图 9所示的立式降膜蒸发器用液体分布器 10， 主要由主体 6四周呈凹面且其顶盖 1底面积大于立式降膜蒸发器的换热管 8管口面积的导流体 9，以及将导流体 9活动支撑于立 式降膜蒸发器的换热管 8内上部相应位置， 使导流体 9的顶盖 1底面边缘与立式降膜蒸发器 的上管板 7顶面间隔一定空隙形成进液通道的支撑部件 5组成。 导流体 9沿立式降膜蒸发器 的换热管的中心轴对称分布， 导流体 9底面直径为换热管 8内径的 0.6倍。 支撑部件 5由 4 个连接在顶盖 1底面的成螺旋形的叶片及各叶片后部下端一体向下的支撑片组成 （图 10)， 各叶片尖端外缘轨迹形成的圆的直径略大于换热管 8的内径， 使得各叶片的尖端抵压在换热 管 8的上端口上或上管板 7上， 导流体 9的顶盖 1底面边缘与立式降膜蒸发器的上管板 7顶 面间隔一定空隙形成进液通道， 各叶片螺旋部分的高度即为进液通道高度； 各支撑片的宽度 与换热管 8内壁和导流体对应位置外壁之间的距离紧密配合， 使得各叶片的支撑片紧靠在换 热管 8内壁和导流体对应位置外壁之间， 从而将导流体 9活动或固定支撑于立式降膜蒸发器 的换热管 8内上部相应位置。
液体从顶盖 1的底面边缘与立式降膜蒸发器的上管板 7顶面之间形成进液通道以向内的 放射线状进入， 并沿相邻螺旋叶片以螺旋状进入液体分布器 10， 使得液体更易分布到换热管 内壁， 液体进入换热管后沿导流体主体 1的四周凹面螺旋流下， 到达导流体主体 1底部时， 液体以向外的放射线状流向换热管内壁。
进入换热管 8的液体流速由进液通道的高度决定。 根据实际情况， 通过改变支撑部件 5 的形状来改变进液通道的高度， 从而调节每根换热管的流量。 实施例 3
一种回收重油开采采出水作为锅炉给水的水处理系统， 包含进水前处理系统、蒸发系统、 补充颗粒系统、 颗粒回收系统。
进水前处理系统包括进水前处理系统， 包括化学处理装置、 进水预热器及脱气器。 化学 处理装置由加药设备 11-1、 11-2， 进水槽混合器 12、 进水槽 13组成。 进水槽与进水预热器 之间通过进水泵 14连接。 以采出水为主的进水进入进水槽， 通过加药设备 11-1、 11-2 向进 水槽 13投加化学处理剂， 在进水槽混合器 12的搅拌下反应。 经化学处理后的进水经进水泵 14泵入进水预热器 15中预热， 再从脱气器 16的顶端进入脱气器进行脱气处理， 经脱气后的 进水进入立式降膜蒸发器 17的盐水槽 18。
蒸发系统即立式降膜蒸发器， 包含盐水槽 18、盐水分布装置， 立式换热管 8、循环泵 21、 循环管道 22以及用于蒸发的能量驱动器（可以是压縮机 23或者是外加蒸汽附带冷凝器 24)。
补充颗粒系统 25包含传统的固体浆料补充设备， 取决于系统大小， 该系统使用一个固体 进料器 （如螺杆进料器） 贮存和转移擦洗颗粒到一个浆料混合槽， 浆料混合槽把擦洗颗粒和 清澈的液体 （冷却的蒸馏水或颗粒回收系统输出的清澈的盐水） 混合， 形成的含高浓度的擦 洗颗粒的浓浆可以通过立式降膜蒸发器的循环管道或者盐水槽直接加入立式降膜蒸发器。 这 种设备存在多种选择， 在许多工业有应用。 补充颗粒系统能够生产擦洗颗粒含量高达 50%的 浆料， 具体浓度根据所选择颗粒的物理性质决定。
颗粒回收系统 26用传统的方法把盐水和悬浮的擦洗颗粒以及由浓縮生成的其他悬浮成 分分离。 分离可用旋流分离器或者锥底槽、 离心机、 过滤器等完成。 颗粒回收系统的浓盐水 输入端及颗粒输出端分别与立式降膜蒸发器的循环管道相连， 分离得到的擦洗颗粒被优先输 入循环管道而除去， 因为所选用的擦洗颗粒的密度比进水中生成的沉淀物高， 因此回流入循 环管道的循环物流中含有更浓的擦洗颗粒， 而排出的盐水物流或输送至补充颗粒系统中的盐 水混合物流含有更多由进料浓縮生成的其他悬浮成分。
脱气的进水进入盐水槽 18， 就与从补充颗粒系统 25输入的擦洗颗粒浓浆混合形成擦洗 颗粒的浓度为 0. 5% ％的盐水浆液， 在蒸发过程中连同换热管中降落下来的盐水浆液一起被 循环泵输送至蒸发器顶部的盐水分布装置。盐水分布装置由盐水分布箱 19和插在每根换热管 顶部的液体分布器 10 (如实施例 1或 2所述） 组成， 以湍流形式把浆液均匀地分布在上管板 和换热管内。 浆液进入盐水分布装置的盐水分布箱 19， 通过叶片把盐水浆液散布在蒸发器的 上管板 7 (图 5 ) 。 盐水浆液以薄层湍流 360度进入液体分布器 10， 这种湍流保持所有擦洗 颗粒均匀悬浮在盐水浆液中。 浆液沿着液体分布器外表面往下流的同时被分布置换热管 8的 内壁表面， 蒸汽在管外冷凝加热， 管内开始蒸发。 盐水浆液和水蒸汽在管内一起向下流动， 在下管板 20处流出。擦洗颗粒与换热管 8内壁接触， 其擦洗作用保持管子表面清洁， 盐水中 析出的物质可粘附在所加入的颗粒上， 而不是粘附在蒸发器换热面上， 因此盐水降膜浓縮时 没有污垢成分沉积在管壁上。
蒸汽与降落的盐水分离， 进入位于立式降膜蒸发器盐水槽的环形空隙处的除雾系统 27。 除雾系统可由几种除雾形式组成， 包括叶片、 丝网、 液体接触装置、 洗涤系统或者是它们的 组合。
蒸汽离开除雾系统， 被吸入压縮机 23。 如果直接应用外源蒸汽加热蒸发盐水， 蒸汽离开 除雾系统进入冷凝器 24。 冷凝器中得到的蒸馏水可被直接用于压力高达 1000 psig的快装锅 炉蒸汽发生设备或者被直接用于压力高达 1500 psig的一次通过式蒸汽发生器 (0TSG)或循环 管式锅炉。
来自压縮机 23的蒸汽或者外供蒸汽， 在换热管 8外壁冷凝。 冷凝水在降膜蒸发器 17的 底部汇集后流入蒸馏水罐 28， 热蒸馏水通过蒸馏水泵 29输送至进水预热器， 在进水预热器 中预热进水的同时被进水冷却， 冷却的蒸馏水可被直接用于压力高达 1000 psig的快装锅炉 蒸汽发生设备或者被直接用于压力高达 1500 psig的一次通过式蒸汽发生器 (0TSG)或循环管 式锅炉。

Claims

权利要求书
1、 一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征在于把以采出水为主的 进水输送至带有盐水分布装置的立式降膜蒸发器， 通过蒸发生产用于锅炉给水的蒸馏水； 其中， 向以采出水为主的进水中或立式降膜蒸发器的循环浓盐水中加入擦洗颗粒形成盐水 浆液， 通过立式降膜蒸发器对盐水浆液进行蒸发时， 利用盐水浆液中的固体粒子防止或减 轻蒸发器换热面上结垢。
2、 根据权利要求 1所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的擦洗颗粒为不溶于进水的具有磨擦作用的固体颗粒，选自颗粒尺寸大于 0且小 于 100微米的沙子、 砂砾、 玻璃珠或其他的金属衍生物颗粒， 颗粒密度为 0.1~10g/cm3。
3、 根据权利要求 2所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的盐水浆液中擦洗颗粒的浓度为 0.5% ~5%。
4、 根据权利要求 1所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于通过补充颗粒系统和颗粒循环回收系统向立式降膜蒸发器加入擦洗颗粒。
5、 根据权利要求 4所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的补充颗粒系统包含传统的固体浆料补充设备：使用一个固体进料器贮存和转移 擦洗颗粒到一个浆料混合槽，浆料混合槽把擦洗颗粒和补给水混合后加入立式降膜蒸发器 的盐水槽或循环管道中。
6、 根据权利要求 5所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的颗粒循环回收系统是用传统的方法把盐水和悬浮的擦洗颗粒以及由浓縮生成 的其他悬浮成分分离， 得到更高浓度的擦洗颗粒回收液、 盐水及含有更高浓度的由浓縮生 成的其他悬浮成分的盐水悬浮液；将得到的更高浓度的擦洗颗粒回收液加入到立式降膜蒸 发器的循环浓盐水中， 将得到的盐水回流至补充颗粒处理系统； 所述的分离可用旋流分离 器或者锥形底槽、 离心机或过滤器完成。
7、 根据权利要求 1所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的盐水分布装置包括位于立式降膜蒸发器顶部的盐水分布箱和位于每根换热管 顶部的液体分布器。
8、 根据权利要求 7所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的液体分布器主要由主体四周呈凹面且其顶盖底面积大于立式降膜蒸发器的换 热管管口面积的导流体， 以及将导流体活动或固定支撑于立式降膜蒸发器的换热管内上部 相应位置，使导流体的顶盖底面边缘与立式降膜蒸发器上管板上表面间隔一定空隙形成进 液通道的支撑部件组成； 盐水浆液沿所述的进液通道、 导流体的凹面进入并分布于换热管 内表面；
或者所述的液体分布器主要由四周呈凹面的导流体、将导流体活动或固定支撑连接于 立式降膜蒸发器的换热管内上部相应位置，导流体的上表面露出换热管上口的支撑部件组 成； 所述的导流体上表面直径大于换热管的外径， 使导流体凹面的上部边缘与立式降膜蒸 发器的上管板上面之间间隔一定空隙形成进液通道， 盐水浆液沿所述的进液通道、 导流体 的凹面进入并分布于换热管内表面。
9、 根据权利要求 8所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的导流体的底面直径大于等于换热管内径的 0.3倍， 且小于换热管内径。
10、根据权利要求 9所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于所述的支撑部件的个数为 2~6个，为多边形筋板，其一边与导流体的凹面无缝隙连接， 其余各边中至少有相邻两边相互垂直，支撑部件依靠该相邻的垂直边架于立式降膜蒸发器 的管板上， 使导流体活动或固定支撑于立式降膜蒸发器的换热管内上部相应位置， 导流体 的顶盖底面边缘与立式降膜蒸发器上管板顶面形成进液通道，或者导流体的顶盖底面边缘 与立式降膜蒸发器上管板顶面形成进液通道；
或者所述的支撑部件由 3~6 个连接在顶盖底面的成螺旋形的叶片及各叶片后部下端一体 向下连接的支撑片组成， 各叶片尖端外缘轨迹形成的圆的直径略大于换热管的外径， 使得 各叶片的尖端抵压在换热管的上端口上或上管板上，导流体的顶盖底面边缘与立式降膜蒸 发器的上管板顶面间隔一定空隙形成进液通道， 各叶片螺旋部分的高度即为进液通道高 度； 各支撑片的宽度与换热管内壁和导流体对应位置外壁之间的距离紧密配合， 使得各叶 片的支撑片紧靠在换热管内壁和导流体对应位置外壁之间，从而将导流体活动或固定支撑 于立式降膜蒸发器的换热管内上部相应位置。
11、根据权利要求 1所述的一种回收重油开采采出水作为锅炉给水的水处理工艺， 其特征 在于采出水经化学加药处理、预热处理、 脱气处理中的一项或多项处理后进入立式降膜蒸 发器； 所述的化学加药处理可设置在预热处理、 脱气处理之前， 也可设置在预热处理、 脱 气处理之后， 蒸发处理之前。
12、 根据权利要求 1~11 中任一项所述的一种回收重油开采采出水作为锅炉给水的水处理 工艺， 其特征在于该工艺包括：
( 1 ) 进水预处理： 以采出水为进水， 向其中添加化学药剂进行化学处理， 出水经预热后 进行脱气处理；
(2) 蒸发处理： 经脱气处理的出水进入立式降膜蒸发器底部的盐水槽， 同时通过补充颗 粒系统向盐水槽中加入含高浓度的擦洗颗粒的浓浆， 使盐水槽中形成擦洗颗粒浓度为 0.5%~5%的盐水浆液；所述的盐水浆液经循环泵泵入立式降膜蒸发器顶部的盐水分布装置 中， 通过盐水分布装置的液体分布器分布到每根换热管中， 盐水浆液在换热管中蒸发的过 程中， 所述的擦洗颗粒与换热管内壁摩擦， 擦洗掉换热管内壁的污垢； 所得蒸汽和浆液在 管内一起向下流动，蒸汽进入位于蒸发器盐水槽的环形空隙处的除雾系统处理后进入压縮 机用于为立式降膜蒸发器提供热能， 或者进入冷凝器冷凝得到冷却的蒸馏水， 盐水浆液在 立式降膜蒸发器下管板处流出， 进入盐水槽循环使用； 颗粒回收系统设置在盐水循环通路 上， 用于将擦洗颗粒循环回立式降膜蒸发器； 立式降膜蒸发器换热管管外壁的蒸汽放热冷 凝后，在立式降膜蒸发器底部汇集，进入蒸馏水罐，用于进水的预热后得到冷却的蒸馏水。
13、 一种回收重油开采采出水作为锅炉给水的水处理系统， 其特征在于包含蒸发系统、 补 充颗粒系统、 颗粒回收系统； 所述的蒸发系统即立式降膜蒸发器， 包含盐水槽、 权利要求 7所述的盐水分布装置、 换热管、 循环泵、 循环管道以及用于蒸发的能量驱动器， 所述的 补充颗粒系统包含固体进料器、浆料混合槽及相应的输送管道， 所述的颗粒回收系统主要 由选自旋流分离器、 锥底槽、 离心机或过滤器中的一种及相应的输送管道组成； 采出水输 送管道与立式降膜蒸发器的盐水槽相连，补充颗粒系统的浓浆输出管道与立式降膜蒸发器 的盐水槽或循环管道相连，颗粒回收系统的浓盐水输入端及颗粒输出端分别与立式降膜蒸 发器的循环管道相连。
14、 根据权利要求 13所述的回收重油开采采出水作为锅炉给水的水处理系统， 其特征在 于所述的回收重油开采采出水作为锅炉给水的水处理系统还包括进水前处理系统和 /或浓 盐水的进一步浓縮或结晶系统， 所述的进水前处理系统包括化学处理装置、预热装置及脱 气装置中的一种或多种； 所述的浓盐水的进一步浓縮或结晶系统包含浓縮器或结晶器； 浓 縮的盐水在浓縮器或结晶器中得到进一步处理。
PCT/CN2012/076540 2012-05-18 2012-06-06 一种回收重油开采采出水作为锅炉给水的水处理工艺 WO2013170507A1 (zh)

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