WO2011032464A1 - 船用油污水分离处理方法及其处理装置 - Google Patents

船用油污水分离处理方法及其处理装置 Download PDF

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Publication number
WO2011032464A1
WO2011032464A1 PCT/CN2010/076650 CN2010076650W WO2011032464A1 WO 2011032464 A1 WO2011032464 A1 WO 2011032464A1 CN 2010076650 W CN2010076650 W CN 2010076650W WO 2011032464 A1 WO2011032464 A1 WO 2011032464A1
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Prior art keywords
oil
sewage
water
separation
membrane
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PCT/CN2010/076650
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English (en)
French (fr)
Inventor
陈海兵
梅冬兴
蔡晓幸
马如中
何丽君
Original Assignee
东台市东方船舶装配有限公司
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Publication of WO2011032464A1 publication Critical patent/WO2011032464A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63J—AUXILIARIES ON VESSELS
    • B63J4/00—Arrangements of installations for treating ballast water, waste water, sewage, sludge, or refuse, or for preventing environmental pollution not otherwise provided for
    • B63J4/004—Arrangements of installations for treating ballast water, waste water, sewage, sludge, or refuse, or for preventing environmental pollution not otherwise provided for for treating sludge, e.g. tank washing sludge

Definitions

  • Marine oil sewage separation treatment method and treatment device thereof Marine oil sewage separation treatment method and treatment device thereof
  • the invention relates to the technical field of oil sewage treatment, in particular to a method for separating and treating marine bilge oil sewage.
  • the present invention also relates to an oily sewage treatment apparatus using the oil sewage separation treatment method. Background technique
  • the existing oil sewage separation treatment method and its treatment device mostly adopt gravity separation treatment plus mechanical oil droplet concentrator.
  • the separation treatment device performs oil-water separation according to the difference of oil and water specific gravity and aggregation and adsorption. of.
  • the density of the residue with a density above 980 kg/m 3 is relatively high.
  • some pollutants such as rust
  • the oil droplets tend to adsorb some rust, making the density difference between the residue and water extremely small, or exceeding the water.
  • the density, and its high viscosity makes it difficult to collect and separate oil droplets, and it is impossible to achieve separation by conventional gravity methods. Furthermore, due to the resolution of MEPC.
  • the separation requirement of the separation device for oily wastewater containing emulsified oil is increased.
  • the oil impurities in the emulsified oil are long-term suspended and uniformly distributed in water, and have high stability and are impossible to aggregate. Undoubtedly, relying on the traditional gravity separation method, it is impossible to separate the oily sewage containing the emulsion.
  • the technical problem to be solved by the present invention is to provide a method for separating and treating marine oily sewage, which can not only realize the separation treatment of high-density residual oil and sewage, but also realize the treatment of oily sewage.
  • the emulsion is effectively separated to meet stringent emission standards.
  • Another technical problem to be solved by the present invention is to provide an oil sewage treatment apparatus for realizing the oil sewage separation processing method.
  • the marine oil sewage separation treatment method of the present invention comprises the following steps: First, preheating the bilge oil sewage to preheat it to 48 ° C to 58 ° C; and then preheating the oil
  • the sewage is sent to the gravity separation device, so that the oil sewage flows through several layers of the oil sewage flow passage in the gravity separation device, and the oil droplets are collected and the oil and water are gravity separated to separate the waste oil and the separated water;
  • the oil sewage channel in the gravity separation device is the largest height 9mm ⁇ 25 mm
  • HRT oily water separating device is a gravity 15mir!
  • the above-mentioned oil sewage separation treatment method is firstly increased by preheating the bilge oil sewage.
  • the difference in density between oil and water, and the viscosity of the residue decrease, which is beneficial to the heavy oil, especially the oil droplets with a density above 980kg/m 3 , which are collected and floated in the oil sewage, and the separated waste oil is also easier.
  • Exhausted from the oil collecting part of course, too high oil temperature will make the oil too thin, and easy to emulsify, and also consume too much heat. Therefore, the inventors have repeatedly analyzed and actual tests, the preheating temperature is controlled at 48. Between °C and 58 °C, with ideal separation effect and comprehensive benefits, it can achieve separation of residual oil with density over 1000k g / m 3 .
  • the coverage area of the oil-water interface and the flow path length of the oily sewage are greatly increased, which not only facilitates the accumulation of oil droplets and accelerates the floating, but is also more advantageous.
  • the collision of tiny oil droplets gathers.
  • reasonable channel height and hydraulic retention time are used, which also ensures the continuous and stable operation of the separation device.
  • the flow path height is too small, it can have a large specific surface area under a certain volume condition, but it is easy to form oil clogging and bubble clogging in the channel, which in turn reduces the working efficiency of the entire separation device, and the excessive flow path height.
  • the size will take up too much space, and the separation efficiency will be reduced, which is not conducive to saving limited cabin space.
  • the same hydraulic retention time also directly affects the working effect and separation efficiency of the separation device, and the maximum height of the oily sewage channel is controlled at 9mm— 25mm, hydraulic retention time control between 15min and 25min has an ideal comprehensive separation treatment effect.
  • the filter material filtering device is used to further remove the oil in the oily sewage, it is more important to remove the solid suspended matter such as iron oxide in the oily sewage, and the filter material filtering device is disposed in the front of the membrane processing device to The physical method better protects the separation membrane from being contaminated by solids and oil droplets and losing workability.
  • the hydraulic retention time in the filter material filtering device is controlled between 0.4 min and 2 min, and the surface flow load of the filter material is designed to be 3 mm 3 /mm 2 . s ⁇ 4 mm Vmm 2 . s (filter material per square millimeter per second time) The surface passes through the filtered water cubic millimeters), which results in higher filtration efficiency and processing capacity.
  • the separation membrane only filters the emulsified oil and the dissolved oil due to the high efficiency separation and filtration in the front.
  • the separation membrane has an ideal separation treatment effect on the emulsified oil, but it is easily blocked by the oil droplets and the suspended solids thereof. Therefore, the present invention adopts a gravity separation method with a plurality of oily sewage passages to make the oil content in the separated water close to 15ppm; the separated water is further subjected to physical filtration of the filter material to further remove suspended solid impurities and oil, thereby preparing for membrane separation and filtration of the emulsified oil.
  • a partial reflux of the concentrate is used in the membrane separation to avoid dead end operation of the separation membrane.
  • the 15% ⁇ 25% of the concentrate of the membrane separation treatment device is continuously sent back to the bilge oil sewage station, so that the oil sewage flows parallel to the membrane surface at a certain speed,
  • the scouring shear force generated by the reflux liquid suppresses the formation of a contaminant gel layer on the surface of the membrane, preventing concentration polarization of the membrane separation surface.
  • the gravity separation device well realizes the separation of oil droplets and moisture in the oily sewage, and the filter material filtering device filters out the solid impurities, and finally the membrane treatment device thoroughly performs only the emulsified oil and the dissolved oil.
  • the interception and separation has realized the conversion of oily sewage ⁇ separated water ⁇ filtered water ⁇ permeate water, and the “division of labor is clear and the divisions are responsible”. Coordinated and orderly guarantee the separation and treatment effect of oily sewage.
  • the membrane module in the membrane separation treatment apparatus employs an external pressure type ultrafiltration membrane module, and a concentration of 18% to 22% of the concentrated liquid is returned to the bilge oil sewage station.
  • the external pressure type ultrafiltration structure is adopted to facilitate the cleaning of the outer surface of the filter membrane; the process of returning the concentrated amount of the concentrated liquid to the bilge oil sewage station has higher separation efficiency and significant anti-pollution effect.
  • the marine oil sewage treatment device of the present invention comprises a heater, a gravity separator, a suction pump, a filter filter and a membrane processor, the heater, the gravity separator, The suction pump, the filter filter and the membrane processor are sequentially connected through the pipeline; the oil sewage inlet of the heater is connected to the bilge oil sewage station, and the permeate water outlet of the membrane processor is connected to the sea valve
  • the suction pump is located on a pipe connecting the gravity separator and the filter filter; a gas recoil valve is further connected to the oil sewage inlet of the membrane processor.
  • the structure is solved by preheating the oily sewage.
  • the problem that the density residue is difficult to be separated and treated the pre-heated oil sewage enters into the multi-layer oil sewage channel with a plurality of corrugated separation discs stacked one on another, so that the oil droplets gather in the oil sewage channel to increase the floating separation, and the oil-water separation time is more Fully, the oil bead gathers and floats more ideally; the suction pump is arranged at the downstream end of the gravity separator, which effectively avoids the disturbance and emulsification of the oil pump by the suction pump; the separated separated water passes through the filter filter The physical filtration filters out the suspended solid impurities and the remaining oil, which in turn prepares the separation membrane for further separation of the emulsified oil; and the membrane processor effectively filters and separates the emul
  • the heater includes a heater housing, and the heater housing is provided with an oil sewage inlet pipe and a heated oil sewage discharge pipe; an oil sewage inlet pipe and a heating oil sewage discharge pipe and heating
  • the cylinders of the casing are connected to each other; a steam heating pipe is disposed in the cavity of the heater casing, and the two ends of the steam heating pipe are respectively led to the steam inlet pipe and the steam discharge pipe.
  • the steam heating pipe is disposed in the cavity of the preheater casing, when the oil sewage to be separated and treated is introduced into the cavity of the preheater casing, the water vapor flowing through the steam heating pipe passes through the heating pipe.
  • the wall heats the oily sewage surrounding the wall of the pipe, so that the temperature of the oil sewage in the cavity of the preheater casing rises, the density decreases, and the viscosity decreases, thereby increasing the density difference between the oil and water, and ensuring the oil sewage in
  • the gravity separation device can be efficiently separated, which is particularly effective for the residual oil having a separation density of 980 kg/m 3 or more, which fundamentally solves the problem that the existing oil pollution gravity separation device cannot separate the oil sewage separation treatment containing the residual oil.
  • the utility model fully utilizes the physical characteristics of the water vapor heat capacity and can be used in a short time. It realizes rapid heating and heating of oily sewage, rapidly melts it and floats up, accelerates the separation speed of oily sewage, and completely overcomes the shortcomings of insufficient heating of electric heating method in the separation of existing oily sewage. At the same time, because large ships are always equipped with water steam boilers, the steam heat source is sufficient, and there is no shortage of severely limited electricity for electric heating.
  • the gravity separator includes a cylinder, and an oil sewage inlet, a waste oil discharge port, and a separation water discharge port disposed on the cylinder, and at least a first aggregate is disposed in the cylinder a separator and a second focusing separator, wherein the first collecting separator and the second collecting separator are respectively located on upper and lower sides of the flow guiding plate, and the periphery of the guiding orifice plate is fixedly fixedly mounted on the inner wall of the cylindrical body
  • a middle of the orifice plate is provided with a through-flow hole;
  • a top end of the first collecting separator is provided with a top cover, a gap is left between the periphery of the top cover and the inner wall of the cylinder;
  • the second gathering The bottom of the separator is provided with a flow guiding blind plate, and a gap is left between the periphery of the guiding blind plate and the inner wall of the cylindrical body; the first collecting separator and/or the second collecting separator
  • the above-mentioned collecting separator is formed by stacking the corrugated separating discs having a conical disc-like structure, and the disc surface of the separating disc having the disc surface taper angle is inclined in the 360° rotation direction, even when the ship is tilted and tilted.
  • the oily sewage between the separation discs is kept in a forward flow state at least in a certain direction, so that the ship is inclined in any direction, and the oil sewage separation device always maintains a normal and continuous working condition, so that the oily sewage of the ship is in any case.
  • the inclined structure of the disc surface is separated, and the existing advection sediment separation structure is skillfully changed into a sloping plate separation structure.
  • the applicant has repeatedly improved the separation effect of the structure compared with the ordinary advection separation structure after repeated trial and comparison.
  • the separation and removal effect of the loose oil beads is more significant; this laminated structure makes good use of the shallow pool theory principle, and the separation treatment effect of the separator is improved by the stacked corrugated cone under the condition that the volume of the cylinder is constant.
  • the cone surface of the separation disc has a corrugated structure, the cone-shaped corrugation peaks and valleys of the adjacent separation discs are alternately stacked to form an oil-sewage separation passage, and the separation passage has different cross-sectional areas in the radial direction, thereby forming a corrugated disc plate.
  • variable spacing, the variable water flow line, and the separation channel structure that changes the water cross section, in which the oil sewage flow is diffused and contracted and alternately flows to generate a sinusoidal pulsating water flow, which greatly increases the collision probability between the oil beads in the oil sewage. It promotes the aggregation of small and scattered oil beads, accelerates the floating speed of oil beads, and improves the separation effect of oil sewage. Also, due to the use of a plurality of sets of aggregated separators adjacent to each other, the oily sewage in the separator can be smoothly twisted from one set of the splitter to another set of aggregate separators, thus greatly extending the oily sewage on the one hand.
  • the length of the separation channel fundamentally solves the defect that the length of the separation channel is insufficient due to the narrow space of the ship, and can maximize the utilization of the space of the ship vacant, and ensure the oil-water separation effect of the separator, ensuring the marine separator.
  • this structure greatly increases the coverage area of the oil-water interface of the separator while extending the length of the separation channel, which makes the oil-water separation time more fully, and the oil-bead aggregation and floating effect is more ideal.
  • the tortuous oil-water separation flow path formed by this structure further increases the oil The effect of the collision and aggregation of the beads is more effective in promoting the expansion of the oil beads and accelerating the floating separation. Therefore, the structure has an ideal oil-water separation effect.
  • each of the corrugated separating discs is alternately stacked with the corrugated peaks and valleys of the disc surface, thereby forming a radial oil-sewage separation passage between the valley peaks which are offset from each other;
  • the small channel height can have a large specific surface area under a certain volume condition, it is easy to form a blockage of oil droplets and bubbles in the channel, which in turn reduces the working efficiency of the entire separation device; the excessive channel height dimension will Excessive space is occupied and the separation efficiency is lowered, which is not conducive to saving limited cabin space, and the height of the oil sewage passage in the circumferential direction (channel width direction) is changed from zero to maximum to zero.
  • the maximum height control of the oily sewage channel is in the range of 9mm ⁇ 25mm with an ideal integrated separation treatment effect.
  • the corrugated cone-disc separation structure not only makes a major breakthrough in the design concept, but is also particularly suitable for the oil-water separation device of the ship, and has the characteristics of simple structure, convenient production and maintenance.
  • the film processor includes a membrane module disposed in a metal cylinder body, and the upper and lower ends of the metal cylinder body are respectively fixedly connected with a bottom cover and a top cover; At least one membrane module concentrate outlet is disposed at the same end of the module, and the membrane module concentrate outlet is connected to the concentrate outlet.
  • the above structure utilizes the membrane module for oil-water separation, so that the oil-water emulsion, dispersing oil or dissolved oil which cannot be processed by gravity separation can be effectively separated, the separation efficiency is high, the energy consumption is low, and there is no phase change and no secondary pollution in the separation process.
  • the membrane module has a simple structure and a short separation process. Further, since at least two membrane module concentrate outlets are disposed on the end side of the membrane module, when the membrane membrane is flushed through the plurality of membrane module concentrate outlets, the flushing water or the compressed air or the cleaning agent can be The filter is effectively cleaned in a uniform direction, and the cleaning effect is reliable and stable, effectively eliminating the "cleaning dead angle" of the filter membrane.
  • the cleaning is not only convenient and quick, but also more clean and thorough, so that the filter membrane can maintain a stable working state for a long time, thereby
  • the breakthrough solves the problem of difficulty in taking out cleaning and high replacement cost. It has been repeatedly tested that the online cleaning method can extend the service life of the filter membrane to more than 8 years, greatly reducing the operating cost of the separation processing device. Also, since the membrane module is disposed in the metal cylinder body and the bottom cover and the top cover, the structure realizes effective protection of the membrane module, and the membrane module can be subjected to long-term harsh environments such as high temperature humidity, vibration, and tilting of the ship. Reliable work, completely avoiding the deformation of the membrane module, the occurrence of damage such as cracking, and avoiding the problem of toxic gas generated by the combustion of the fire membrane module, safe use and long service life.
  • FIG. 1 is a schematic structural diagram of a process of a specific embodiment of the present invention.
  • Figure 2 is a schematic view showing the structure of the heater in the structure shown in Figure 1;
  • FIG 3 is a schematic structural view of a gravity separator in the structure shown in Figure 1;
  • Figure 4 is a schematic view showing the structure of the front side of the gravity separator in the gravity separator shown in Figure 3;
  • Figure 5 is a front view showing the structure of the corrugated separating disc in the collecting separator shown in Figure 4;
  • Figure 6 is a schematic plan view showing the structure of the corrugated separating disc shown in Figure 5;
  • FIG. 7 is a schematic view showing the structure of another gravity separator in the structure shown in Figure 1;
  • Figure 8 is a schematic structural view of a film processor in the structure shown in Figure 1;
  • Figure 9 is an enlarged schematic view showing the structure of a portion A in the structure shown in Figure 8.
  • Figure 10 is a schematic structural view of the membrane module in the structure shown in Figure 8.
  • FIG. 11 is a schematic diagram of a flow structure of another embodiment of the present invention. detailed description
  • the marine oil sewage treatment device includes a heater 1, a gravity separator 2, a suction pump 3, a filter filter 5, and a membrane processor 6 which are sequentially connected through a pipe; the filter filter 5
  • the filtered water outlet is in communication with the membrane processor 6 filtered water inlet 608 and the sea-sealing valve 10 that are connected to each other.
  • the suction pump 3 uses a screw pump; the saturated water vapor pair passes through the heater 1
  • the oil sewage is preheated to 48 ° C to 58 ° C, preferably the preheating temperature is controlled between 52 ° C and 56 ° C.
  • the preheated oil sewage is continuously sucked into the gravity separator 2, the upper part of the gravity separator 2 is a static separation chamber having a dome-shaped top cover, and the lower cylinder chamber is formed with a gathering separator.
  • the waste oil separated by the gravity separator 2 is discharged from its arched top cover portion into the waste oil pool 24 through the waste oil discharge valve 25, and the gravity separator 2 also has a gravity separator backwashing pipe 2 1 and a drain valve 22
  • the hydraulic retention time of the oil sewage in the gravity separator 2 is 15 min to 25 min, preferably between 18 min and 22 min; the separated water separated by the gravity separator 2 is discharged through the separated water discharge valve 20 on the conveying pipe.
  • the filter medium filter 5 adopts a common filter element filtering device.
  • the filter element adsorbing material is a polymer fiber such as polypropylene fiber, and the filter element has a filter pore diameter of 30 m.
  • the filter element material may also be a common material such as wood or activated carbon.
  • the hydraulic retention time of the filter material filter 5 should be between 0.4 min and 2 min, and the surface flow load of the filter material should be designed to be 3 mm 3 /mm 2 . 4 mmVmm 2 .
  • the filter discharge valve II 1 9 the filter discharge valve II 1 9 , the anti-siphon 9 and the through-sea valve 10 to the outboard.
  • the filter discharge valve II 19 is closed, and the separated water passes through the filter discharge valve I 18 and the filtered water inlet 608 of the membrane processor 6 into the membrane processor. 6.
  • the permeate water after the membrane separation treatment is discharged to the outboard via the permeate water valve 7, the check valve 8, the anti-siphon tube 9, and the through-sea valve 10.
  • the membrane module in the membrane separation treatment device is external Pressurized ultrafiltration membrane module.
  • a drain valve 15 At the filtered water inlet 608 of the membrane processor 6, a drain valve 15, a gas recoil valve 16 and a tank shut-off valve 17 are also connected in parallel.
  • the membrane processor 6 After the membrane processor 6 is drained, the compressed air is air-cleaned through the gas recoil valve 16 to the separation membrane of the membrane module; the membrane processor 6 can also clean the membrane module with clean seawater or fresh water; After the use of the dosing pump 13, the drug wash stop valve 12 and the medicine box stop valve 17, the cleaning agent in the cleaning medicine box 14 is circulated between the membrane module and the medicine box, so that the separation membrane maintains a good working condition. The amount of the cleaning agent is continuously reused, and the membrane module does not need to be removed, which facilitates the use operation on the vessel and greatly prolongs the service life of the membrane module.
  • the heater 1 shown in Fig. 2 includes a heater casing 101 which has a cylindrical shape and is wrapped with a heat insulating material outside the cylindrical casing to improve thermal efficiency.
  • a heater casing 101 which has a cylindrical shape and is wrapped with a heat insulating material outside the cylindrical casing to improve thermal efficiency.
  • an oily sewage passage pipe 103 is disposed, and an upper portion of the heater casing 101 is provided with a heated oil sewage discharge pipe 108, and the oil sewage enters through the oil sewage passage pipe 103. It is discharged into the cylinder chamber of the heater casing 101, and then discharged from the heated oil sewage discharge pipe 108, and sent to the oil sewage gravity separator.
  • a plurality of steam heating pipes 102 arranged side by side are arranged in the cavity of the heater casing 101.
  • Each of the steam heating pipes 102 has an inverted U-shaped tubular shape, and one end of the U-shaped pipe is a steam inlet end, and the other end is a steam inlet end. It is the steam outlet end.
  • a heating pipe connecting seat is fixedly connected at a lower end of the heater casing 101, and the heating pipe connecting seat has a built-in cavity which is partitioned into a steam inlet cavity and a steam discharge cavity by a radially arranged partitioning partition.
  • the steam heating pipe 102 is fixedly mounted on the heating pipe connecting seat, and the inlet end of the inverted U-shaped steam heating pipe 102 communicates with the steam inlet cavity, and the outlet end of the steam heating pipe 102 communicates with the steam discharge cavity.
  • a steam inlet pipe 105 and a steam discharge pipe 106 are disposed on the heating pipe connection seat; the steam inlet pipe 105 is located at a steam inlet cavity of the heating pipe connection seat, and leads to the steam inlet cavity; the steam discharge pipe 106 is located at the heating pipe connection seat.
  • the steam exits the chamber and is in communication therewith.
  • a conventional trap is mounted on the steam exhaust pipe 106, which automatically removes condensed water in the steam line and prevents steam from leaking during operation.
  • a common steam on-off valve is installed on the steam inlet pipe 105 to control the inflow and cut-off of steam, and to control the flow rate of the steam to automatically maintain the constant temperature.
  • the gravity separator 2 includes a cylinder 211 and an oil sewage inlet port 213 provided thereon, a cylinder cover 201, a separation water discharge port 209, a sludge discharge port 210, and a A waste oil discharge port 214 on the can lid 201.
  • the cylinder of the gravity separator 2 is composed of a cylinder 211 and a cylinder cover 201 connected thereto.
  • the cylinder 211 and the cylinder cover 201 are connected by a connecting flange 202, and the cylinder chamber can be roughly divided into a static separation chamber and a flow.
  • the upper separation chamber; the upper portion of the cylinder 211 and the cylindrical cover 201 having a dome shape constitute a stationary separation chamber, and the lower portion of the cylinder 211 is provided with a corrugated stacked oil sewage flow passage separation chamber formed by a collecting separator.
  • a collecting separator Arranged adjacently from top to bottom in the lumen of the cylinder 211
  • the first collecting separator 204 and the second collecting separator 207 are two sets of collecting separators, and the two sets of collecting separators are respectively located on the upper and lower sides of the guiding orifice plate 206; the guiding orifice plate 206 has a disc-like structure.
  • the intermediate position of the orifice plate 206 is provided with a flow-through hole for flowing oily sewage from the first collecting separator 204 into the second collecting separator 207.
  • the periphery of the orifice plate 206 is fixedly mounted on the inner wall of the cylinder 211 by a welded support ring in the cylinder to block oily sewage from entering the lower space of the cylinder from the outer side of the first focus separator 204 and the inner wall of the cylinder. After the oily sewage is collected, it is introduced into the second collecting separator 207 from the conducting hole of the orifice plate 206.
  • a top cover plate 203 is disposed at a top end portion of the first collecting separator 204, and the top cover plate 203 has a flat bottom disc-like structure, and a gap is left between the periphery thereof and the inner wall of the cylindrical body 211 to force the oil sewage to be separated from the first aggregate.
  • the outer periphery of the vessel 204 uniformly enters the oil-sewage separation passage between the corrugation separation discs 215 of the first gathering separator 204 in a radial direction, and then collects into the pilot-through holes located therebetween.
  • the top cover 203 is fixedly coupled to the deflector plate 206 by a support screw 205.
  • a baffle blind plate 208 is fixedly disposed at the bottom of the second focus separator 207.
  • the baffle blind plate 208 also has a flat bottom disc-like structure, which passes through the connecting screw 212 and the diversion orifice plate located in the intermediate through-flow hole. 206 and the top cover 203 are fixedly connected to each other.
  • the flow guiding blind plate 208 blocks the oily water flowing in from the intermediate conducting flow hole of the focusing separator to continue to flow along the through hole, forcing it to uniformly rise upward into the oily water formed by the corrugated separating disk 215 of the second collecting separator 207. Separate the flow path.
  • the separated water separated by the two sets of the collecting separators has been relatively clean, and the separated water enters the bottom chamber of the cylindrical body 211 along the peripheral gap of the second collecting separator, and is finally discharged through the separated water discharge port 209.
  • the first collecting separator 204 and the second collecting separator 207 are each formed by laminating a plurality of corrugated separating discs 215.
  • Fig. 4 shows a schematic structure of a set of collecting separators (in the case of a first collecting separator, the second collecting separator has the same structure).
  • the collecting separator of the structure comprises a plurality of corrugated separating discs 215 stacked on each other, each of the corrugated separating discs 215 has a conical disc-shaped structure with a through-flow hole 216 in the middle, and the disc surface of the cone disc has a corrugated surface, and the disc surface is corrugated Extending in the circumferential direction of the disk surface.
  • Each of the corrugated separating discs 215 is alternately stacked with the corrugated peaks and valleys of the disc surface thereof to form a radial oil-sewage separation flow path between the valley peaks which are offset from each other, since the oil-sewage flow passage is circumferentially oriented (flow path width direction)
  • the height of the oily sewage channel should be controlled from 9mm to 25mm.
  • the cross-sectional area of the oil-sewage flow path in the radial direction gradually increases from the center to the outer side, or gradually decreases from the outer side to the center.
  • a plurality of support ears may be provided on the outer periphery of the separator for fixed support of the separator.
  • the separator of the structure since the corrugated disc structure is adopted, the bellows separating discs 215 are connected to each other very stably, and no other fixing members are required, and the mutual spacing or the cross-sectional size of the separating flow passages depends on the corrugation of the corrugated tubes. structure size.
  • the disc surface taper angle ⁇ of the corrugated separating disc 215 is 20°. Of course, according to the medium separation condition and the specific working condition, the disc surface taper angle ⁇ can be between 15° and 30°. It is preferred to carry out between. As shown in the figure, the disk surface taper angle ⁇ is an angle between the disk tilting bus bar and the horizontal line.
  • the disc material of the corrugated separating disc 215 is composed of a disc substrate and an oleophobic layer covering the substrate. In this embodiment, the disc substrate is made of steel sheet, and the oleophobic coating on the disc substrate is coated. The material is an existing hydrophobic oil nano material, and a corresponding oleophobic material such as poly 4 ethylene oxide can also be used.
  • Fig. 7 shows a gravity separator 2 of another structure in which the number of sets of the aggregate separators in the cylinder 211 and the associated mounting manner are different from those shown in Fig. 2. Other structures are the same.
  • a flow guiding blind plate 208 is still provided at the bottom side of the second collecting separator 207, and the third collecting separator 217 is located at the lower side of the flow guiding blind plate 208.
  • the flow guiding blind plate 208 is still in the form of a flat bottom disc, and a gap is left between the periphery thereof and the inner wall of the cylindrical body 211 to block the flow of water through the intermediate passage of the separator into the third collecting separator 217, forcing it to The outer side of the third collecting separator 217 flows toward the middle thereof.
  • the bottom of the third collecting separator 217 is provided with a bottom baffle plate 218, and the bottom baffle plate 218 has a disc-like structure with a through-flow hole in the middle, and the periphery of the bottom baffle plate 218 is closed by welding.
  • the ground is fixedly mounted on the inner wall of the cylinder 211.
  • the third separation separator 217 further separates the separated water and flows into the lower chamber of the cylinder 211 through the intermediate passage hole, and then discharges through the separation water discharge port 209.
  • the film processor 6 includes a film assembly 605 and a metal cylinder 610; the film assembly 605 is placed in a metal cylinder 610 with a gap, the film assembly 605
  • the membrane module housing 606 and the filter membrane 607 are used, which employ an ultrafiltration membrane module, and of course, a microfiltration membrane module or the like.
  • the metal cylinder 610 has a tubular structure, and both ends of the upper and lower ends are provided with a connecting flange, and the material is Q 2 3 5.
  • a top cover 611 is sleeved on the top of the membrane assembly 605.
  • the top cover 611 has a cup-shaped structure which is buckled on the top of the membrane assembly 605 and is fixedly connected to the metal cylinder 610 through a connecting flange.
  • the top end is provided with a permeate water outlet 601, and the side thereof is provided with a concentrate outlet port 604.
  • a top upper sealing ring 612 and a top lower sealing ring 613 are disposed between the inner wall of the top cover 611 and the top outer surface of the membrane assembly 605, and the top upper sealing ring 612 and the top lower sealing ring 613 are both used. Shaped seal.
  • a membrane module concentrate outlet 602 At the side of the top position of the membrane module 605 is provided a membrane module concentrate outlet 602, and the top upper seal ring 612 and the top lower seal ring 613 are located on the upper and lower sides of the membrane module concentrate outlet 602, thereby making it and the membrane module
  • the outer casing 606 and the top cover 611 enclose an annular cavity 603.
  • the concentrate outlet 604 is located at the annular chamber 603 on the top cover 611 through which the membrane module concentrate outlet 602 communicates with the concentrate outlet 604.
  • a bottom cover 609 is sleeved at the bottom of the membrane module 605, and a bottom seal 614 is disposed between the inner wall of the bottom cover 609 and the outer side of the bottom of the membrane assembly 605.
  • the bottom seal 614 employs a two-shaped seal ring.
  • the bottom cover 609 also has a cup-shaped structure that is sleeved to the bottom end of the membrane module 605 and is fixedly coupled to the metal cylinder 610 by a connecting flange.
  • the bottom end portion of the bottom cover 609 is provided with a filtered water inlet 608.
  • the bottom seal 614 prevents filtered water from entering the space between the membrane module 605 and the metal cylinder 610.
  • the membrane module 605 is a universal member, but is uniformly added to the side at the top position.
  • a plurality of membrane module concentrate outlets 602 are provided, and membrane module concentrate outlets 602 are disposed equidistantly on the same section of membrane module housing 606.
  • six membrane module concentrate outlets 602 are evenly distributed on the same section of the upper end of the membrane module 605.
  • the number of the membrane module concentrate outlet 6 should be selected according to the conditions of use, the selected membrane module specifications, etc., in the range of 2 to 10, according to a limited number of tests, the membrane module concentrate outlet 6 is the best.
  • Upper and lower sealing grooves are further provided on the upper and lower sides of the cross section of the membrane module concentrate outlet 602 to mount the sealing ring.
  • a seal groove is also added to the outer side of the bottom end of the membrane module 605.
  • Fig. 11 shows another embodiment of the present invention, except that the structure of the filter medium filter 5 is different from that of the above embodiment, and the other structures are the same.
  • the filter material filter 5 adopts two-stage filtration, and the filter core adsorption material still uses polymer fibers such as polypropylene fibers, but the filter element of the primary filter filter 51 has a filter pore size of 50 ⁇ , and The filtration filter diameter of the filter element of the filter material of the grade 2 filter is 30 ⁇ ⁇ ; the hydraulic retention time of the filter material of the two-stage filter material 5 is designed to be between 0.4 min and 2 min, and the flow rate load of the filter material surface should be designed to be 3 mm 3 / Mm 2 .
  • the filtered water discharge valve I 27 is opened, and the filtered water is discharged to the outboard through the filtered water discharge valve I 27, the anti-siphon 9 and the through-sea valve 10.
  • the filtered water discharge valve I 27 is closed, and the filtered water filtered by the primary filter filter 51 enters the secondary filter filter 52, and the filtered water that passes through the secondary filtration passes through the water discharge valve. 28 is sent to the membrane processor 6 for membrane separation treatment.

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Description

说明书
船用油污水分离处理方法及其处理装置 技术领域
本发明涉及油污水处理技术领域，特别涉及一种船用舱底油污水的分离处理方法。本 发明还涉及一种采用该油污水分离处理方法的油污水处理装置。 背景技术
随着世界航运事业的快速发展， 船舶吨位的迅速增加， 船舶舱底油污水的不当排放 已成为船舶造成海洋污染的最主要形式。船舶油污水排入海洋水体后，在水体表面形成一 层极薄的油膜， 据资料分析， 向水面排放 1吨油品， 即可形成 5 X 10W的油膜污染， 这种 油膜直接阻碍大气中的氧向水体中转移， 使水体缺氧， 水生物因缺氧而死亡； 油品还具有 一定的毒性， 对幼鱼和鱼卵的影响尤为突出， 另外， 大量的油膜甚至可能引起火灾而影响 水上交通。 船舶舱底油污水排放给海洋环保带来了巨大的威胁。
为此， 国际海事组织和各国政府相继出台了一系列的海事法律法规， 以最大限度地 减少船舶污染问题，国际海事组织海上环境保护委员会也将船舶在沿海和特殊区域排放舱 底水的含油量不超过 15ppm的规定扩大到了所有海域，船用油污水处理装置已成为强制配 备执行的船舶排污处理设备。国际海事组织于 2003年 7月 18日通过的 MEPC. 107 (49)决议 对 15ppm舱底油污水分离装置及报警器提出了更为严格的标准， 将分离处理重油密度 940kg/m3提升至 980kg/m3以上， 并且增加了对乳化油的处理要求； 含有乳化油的油污水特 别是含有表面活性剂的化学乳化油的油污水分离一直是油污水处理领域的一大难题，故而 此前的相关法规和排放标准均未提出乳化油的处理要求和处理装置的试验要求。
现有的油污水分离处理方法及其处理装置大都采用重力分离处理再加上机械状的油 滴聚集器，这类分离处理装置是根据油和水比重的不同以及聚集、吸附作用来进行油水分 离的。 但密度在 980kg/m3以上的渣油本身密度较高， 加之一些污染物 （如铁锈） 的存在， 油滴往往吸附了一些铁锈，使得渣油与水的密度差极小，或超过水的密度，且其粘度很高， 使得聚集分离油滴上浮的难度加大， 甚至无法通过传统的重力方法实现分离。 更由于 MEPC. 107 (49)决议增加了分离装置对含有乳化油的油污水的分离要求，乳化油中的油杂质 是长期悬浮、且均匀分布于水中， 具有高度的稳定性而不可能聚集上浮， 无疑依靠传统的 重力分离方法是无法实现含有乳化液的油污水分离的。
虽然人们通过在重力分离加上机械状的油滴聚合器的基础上， 再通过膜过滤分离， 理论上这种分离方法能够实现乳化油的分离处理， 然而由于分离膜在截留乳化油的过程 中， 被截留物在膜表面上的堆积会在膜表面产生薄层覆盖的凝胶层而导致分离膜的污染， 更为严重的是由于分离膜通常具有亲油性，分离过程中由于前段处理方法不能彻底分离油 污水中的油滴、 固体物和水， 膜分离过程中， 液体的快速流动使得油滴和固体杂质很快进 入到致密的细孔，引起膜的内部堵塞，膜表面的污染和膜孔的堵塞使得水分子无法在侧压 作用穿过致密的微孔而进入膜的另一侧。试验表明，这种结构的处理装置在短短几周甚至 几天内膜通量即出现明显的下降， 且随着时间的延长， 膜通量一般会成倍下降， 为此只得 从分离装置中取出分离膜进行清洗或更新分离膜，这不仅明显的增加了分离装置的运行成 本， 而且在船舶空间十分有限的条件下， 也是十分困难的。
由于现有的油污水分离处理装置中， 受其重力分离阶段分离结构和分离方法的局限， 既不能分离含有密度较高的渣油污水，又不能较为有效地消除油污水中的油滴成份和固体 杂质， 而加重膜分离阶段的负担， 导致膜分离很快失效， 出现分离处理装置各分离阶段功 能上的相互牵制， 不能各司其责， 最终导致整个装置无法正常工作。 发明内容
针对现有技术所存在的上述不足，本发明所要解决的技术问题是提供一种船用油污水 分离处理方法，该方法不仅能够实现高密度渣油油污水的分离处理，而且能够实现对油污 水中的乳化液进行有效分离处理， 使之满足严格的排放标准。
本发明另一个要解决的技术问题是还要提供一种实现该油污水分离处理方法的油污 水处理装置。
为了解决上述技术问题， 本发明的船用油污水分离处理方法包括以下步骤： 首先对舱 底油污水进行预加热处理， 使其预加热至 48°C〜58°C ; 再将预加热后的油污水送到重力 分离装置，使油污水流过该重力分离装置中的若干层油污水流道，进行油滴聚集和油水重 力分离而分离出废油和分离水； 该重力分离装置中的油污水流道最大高度为 9mm〜25mm， 油污水在重力分离装置中的水力停留时间为 15mir！〜 25min; 经重力分离装置分离后的废 油排出，分离水则再经输送管道输送至滤料过滤装置；分离水在所述滤料过滤装置中的水 力停留时间为 0. 4min〜2min，滤料表面流速负荷为 3mm3/mm2. s〜 4 mmVmm2. s ;经滤料过滤 装置过滤后的过滤水再经输送管道输送至膜分离处理装置， 将膜分离处理装置 15%〜25% 处理量的浓縮液继续送回舱底油污水站，余下浓縮液回收，膜分离处理装置的渗透水排出 舱外。
采用上述的油污水分离处理方法， 首先由于对舱底油污水进行预加热处理， 从而增 大了油、水之间的密度差， 且渣油粘度下降， 有利于重油尤其是密度在 980kg/m3以上的渣 油油滴在油污水中聚集上浮分离，而且分离出的废油也更容易从集油部位中排出； 当然过 高油温既会使油变得过稀， 且容易乳化， 也会消耗过多的热能， 因此， 发明人经过反复分 析和实际试验， 预加热温度控制在 48°C〜58°C之间， 具有理想的分离效果和综合效益， 能实现对密度超过 1000kg/m3渣油的分离。
第二， 由于采用具有多层油污水流道的流道重力分离方法， 大大增加了油水界面的 覆盖面积和油污水的流道长度，不仅有利于油滴的聚集增大和加速上浮，而且更有利于微 小油滴的碰撞聚集。同时采用合理的流道高度尺寸和水力停留时间，也有效保证了分离装 置连续稳定地工作。过小的流道高度虽能在一定容积条件下具有较大的比表面积，但很容 易形成油滴和气泡在通道中的堵塞，反而使整个分离装置的工作效率下降，过大的流道高 度尺寸又会占用过大的空间， 且使分离效率下降， 不利于节省有限的船舱空间， 同样水力 停留时间也直接影响着分离装置的工作效果和分离效率， 将油污水流道最大高度控制在 9mm— 25mm, 水力停留时间控制在 15min— 25min之间具有理想的综合分离处理效果。
第三， 由于采用滤料过滤装置不仅进一步去除油污水中的油份， 更为重要的是去除 油污水中的氧化铁等固体悬浮物，将该滤料过滤装置设置于膜处理装置的前道， 以物理方 法较好地保护了分离膜不被固体物和油滴污染而丧失工作能力。滤料过滤装置中的水力停 留时间控制在 0. 4min〜2min之间，滤料表面流速负荷设计为 3mm3/mm2. s〜 4 mmVmm2. s (在 每秒时间内每平方毫米滤料表面通过的过滤水立方毫米数）， 从而使之具有较高的过滤处 理效率和处理能力。
第四， 由于采用前道的高效分离、 过滤， 分离膜仅对乳化油及溶解油进行滤分处理。 分离膜对乳化油具有理想的分离处理效果，但其又容易被油滴及其悬浮固体物堵塞， 因此 本发明一方面通过具有多层油污水流道的重力分离方法， 使分离水中的油含量接近 15ppm; 该分离水再经滤料的物理过滤进一步除去悬浮固体杂质和油份， 从而为膜分离过 滤乳化油做好前期准备。
第五， 在膜分离中采用浓縮液部分回流的方法， 避免分离膜的死端操作。 综合考虑 膜表面的清洁和膜处理效率， 而将膜分离处理装置 15%〜25%处理量的浓縮液继续送回舱 底油污水站，让油污水以一定速度平行于膜表面流动， 以回流液所产生的冲刷剪切力抑制 膜表面污染物凝胶层的形成， 阻止膜分离表面的浓度极化。
在本发明的分离处理过程中， 重力分离装置很好地实现了油污水中油滴与水分的分 离，滤料过滤装置又滤去了固体杂质，最后膜处理装置仅对乳化油和溶解油进行彻底的截 留分离，实现了油污水→分离水→过滤水→渗透水的转化，各工序 "分工明确、各司其责"， 协调有序地保证油污水的分离处理效果。
本发明的一种优选实施方式， 所述膜分离处理装置中的膜组件采用外压式超滤膜组 件， 且将 1 8 %〜22%处理量的浓縮液送回舱底油污水站。采用外压式超滤结构， 便于对滤 膜外表面污染物进行清洗处理；采用该处理量的浓縮液送回舱底油污水站的工艺方法，具 有更高分离效率和显著防污染效果。
为了实现本发明船用油污水分离处理方法， 本发明的船用油污水处理装置， 包括加热 器、重力分离器、抽吸泵、滤料过滤器以及膜处理器， 所述加热器、重力分离器、抽吸泵、 滤料过滤器以及膜处理器通过管道依序相连通;所述加热器的油污水通入口连向舱底油污 水站，所述膜处理器的渗透水出口与通海阀相连通；所述抽吸泵位于连通重力分离器和滤 料过滤器的管道上； 在所述膜处理器的油污水入口处还并连有气体反冲阀。
本发明的油污水处理装置， 采用上述结构后， 由于加热器、 重力分离器、 抽吸泵、 滤 料过滤器及膜处理器依序连通排列，该结构通过对油污水的预加热而解决高密度渣油难以 分离处理的问题，预加热后油污水再进入到具有若干波纹分离盘相互错叠形成的多层油污 水流道中，使油滴在油污水流道中集聚增大上浮分离，油水分离时间更加充分，油珠聚集、 上浮效果更加理想；抽吸泵设置于重力分离器的下游端，有效避免了抽吸泵对油污水的扰 动和乳化作用；经分离后的分离水再经滤料过滤器的物理过滤而滤去悬浮固态杂质和剩余 的油份，这又为分离膜对乳化油的进一步分离作好了充分准备；而膜处理器又对乳化油进 行有效的过滤分离，且该膜处理器能在使用中即时在进行气流反冲清洗，稳定了膜组件的 使用通量。故而在本发明的处理装置中， 各步骤的工艺设备排布合理、 功能相辅， 协调有 效地对含有较高密度渣油、 悬浮固体杂质以及乳化液的油污水进行高效分离处理。
本发明的一种优选实施方式， 所述加热器包括加热器壳体， 该加热器壳体上设置有 油污水通入管和加热油污水排出管；油污水通入管和加热油污水排出管与加热器壳体筒腔 相连通；所述加热器壳体筒腔内设置有蒸汽加热管，该蒸汽加热管两端分别通向蒸汽通入 管和蒸汽排出管。
上述结构中， 由于在预热器壳体筒腔内设置有蒸汽加热管， 当预热器壳体筒腔内通入 待分离处理的油污水时，流经蒸汽加热管的水蒸汽通过加热管壁对包围其管壁四周的油污 水进行加热， 使预热器壳体筒腔内的油污水温度上升， 密度降低， 粘性下降， 从而加大了 污油和水的密度差， 保证油污水在重力分离装置中能够高效分离， 这对分离密度达到 980kg/m3以上的渣油显得特别有效，从根本上解决了现有油污重力分离装置无法分离含有 渣油的油污水分离处理问题。更由于位于加热器壳体筒腔内的蒸汽加热管是通以饱和水蒸 汽作为油污水的加热介质的，这就充分利用了水蒸汽热容量高的物理特性，能在短时间内 实现对油污水的快速升温加热， 快速使其融化上浮， 加快了油污水的分离速度， 彻底克服 了现有油污水分离中电加热方式升温严重不足的缺陷。同时也由于大型船舶总是配有水蒸 汽锅炉， 蒸汽热源充足， 不会出现电加热用电严重受限的不足。
本发明又一种优选实施方式， 所述重力分离器包括筒体， 以及设置于筒体上的油污 水进口、废油排放口和分离水排出口，在所述筒体内至少设置有第一聚集分离器和第二聚 焦分离器， 该第一聚集分离器和第二聚集分离器分别位于导流孔板的上、下两侧， 该导流 孔板的周边封闭地固定安装于筒体的内壁上，导流孔板的中间位置设有导流通孔；所述第 一聚集分离器的顶端设有顶部盖板，该顶部盖板的周边与筒体内壁间留有间隙；所述第二 聚集分离器的底部设有导流盲板，该导流盲板的周边与筒体的内壁间留有间隙；第一聚集 分离器和 /或第二聚集分离器包括若干相互叠置的波纹分离盘， 该波纹分离盘呈锥盘状且 盘面为波纹面，相邻波纹分离盘以其波纹峰谷相错叠而形成径向的油污水流道，该油污水 流道的最大高度为 9mm〜25mm。
上述的聚集分离器由于是由呈锥盘状结构的波纹分离盘相互错叠而成，具有盘面锥角 的分离盘的盘面在 360° 的回转方向内均呈倾斜结构， 即使在船舶摇摆倾斜的情况下， 分 离盘间的油污水至少在一定方向上保持顺流状态，使得船舶发生任何方向的倾斜，该油污 水分离装置总保持着正常地、连续工作状况，使船舶油污水在任何情况下总能处于高效分 离中。同时分离盘面的倾斜结构，又巧妙地将现有的平流沉淀分离结构改变成斜板分离结 构，申请人经过反复试验对比，该结构较普通平流式分离结构的分离效果有了成倍的提高， 特别对散性油珠的分离去除效果更加显著； 这种层叠结构又很好地运用了浅池理论原理， 在筒体体积不变的情况下，使分离器的分离处理效果提高了层叠波纹锥盘数的倍数。又由 于分离盘的锥盘面呈波纹状结构，相邻分离盘的锥面波纹峰谷相互交错叠置而形成油污水 分离通道， 该分离通道沿径向具有不同的截面积， 从而构成波纹盘板的变间距、变水流流 线、变过水断面的分离通道结构， 在该通道中油污水流呈扩散、收縮状态而交替流动产生 了正弦脉动水流，大大增加了油污水中油珠之间了碰撞机率，促使小而分散的油珠聚集变 大， 加快了油珠的上浮速度， 提升油污水的分离效果。还由于采用了多组聚集分离器相邻 设置的结构，使得在分离器中的油污水能从一组聚集分离器曲折回转地流至另一组聚集分 离器，这样一方面大大延伸了油污水分离通道的长度，从根本上解决了船舶空间狭小而带 来的分离通道长度不足的缺陷，既能最大限度地利用船舶空置的空间，又能确保分离器的 油水分离效果，确保了船用分离器的高效工作； 另一方面这种结构在分离流道延伸长的同 时， 也大大增加了分离器油水界面的覆盖面积， 使得油水分离时间更加充分， 油珠聚集、 上浮效果更加理想， 再一方面， 这种结构所形成的曲折油水分离流道， 又进一步增加了油 珠碰撞聚集的效果， 更有效地促进油珠并合长大， 加速上浮分离， 因此该结构具有十分理 想的油水分离效果。再由于油污水流道的最大高度设计为 9mm〜25mm， 各波纹分离盘以其 盘面的波纹峰谷相互交错叠置， 从而在相互错开对置的谷峰间形成径向的油污水分离通 道；过小的通道高度虽能在一定容积条件下具有较大的比表面积，但很容易形成油滴和气 泡在通道中的堵塞，反而使整个分离装置的工作效率下降；过大的通道高度尺寸又会占用 过大的空间， 且使分离效率下降， 不利于节省有限的船舱空间， 同时由于该油污水通道沿 周向（通道宽度方向）的高度是从零到最大再至零变化的。该油污水流道的最大高度控制 为 9mm〜25mm 范围内具有理想的综合分离处理效果。 同时这种采用波纹状的锥盘分离结 构， 不仅在设计理念进行了重大的突破， 特别适用于船舶的油水分离装置中， 而且具有结 构简单、 制作维护方便的特点。
本发明再一种优选实施方式，所述膜处理器包括膜组件，该膜组件设置于金属筒体内， 金属筒体的上、下两端分别固定连接有底罩和顶罩；在所述膜组件同一端至少设置有二个 膜组件浓縮液出口， 该膜组件浓縮液出口与浓縮液引出口相连通。
上述结构由于运用膜组件进行油水分离，使得重力分离无法处理的油水乳化液、分散 油或溶解油得以有效分离， 分离效率高， 能耗低， 且分离过程中无相变、 无二次污染， 膜 组件结构简单， 分离流程短。又由于在膜组件端侧至少设置有二个膜组件浓縮液出口， 当 通过多个膜组件浓縮液出口反向对滤膜进行冲洗时，冲洗水或压縮空气或清洗剂能从各个 方向均匀一致地对滤膜进行有效的清洗， 清洗作用可靠稳定， 有效消除了滤膜的"清洗死 角"， 清洗不仅方便快捷， 而且更加干净彻底， 使滤膜能保持长期的稳定工作状态， 从而 突破性解决了取出清洗困难， 更换成本高的问题， 通过反复试验表明， 该在线清洗方法能 使滤膜的使用寿命延长至 8年以上，大大降低分离处理装置的运行费用。还由于膜组件被 设置于金属筒体及底罩和顶罩中，这种结构实现了对膜组件的有效保护，使膜组件能长期 地在船上高温湿度、 振动、 倾斜摇摆等恶劣环境下可靠工作， 彻底避免了膜组件的变形， 开裂等损坏现象的发生， 也避免因火灾膜组件燃烧产生有毒气体等问题， 使用安全， 寿命 长。 附图说明
下面结合附图和具体实施方式对本发明作进一步详细的说明。
图 1是本发明一种具体实施方式的流程结构简图；
图 2是图 1所示结构中加热器的结构示意图；
图 3是图 1所示结构中一种重力分离器的结构示意图； 图 4是图 3所示重力分离器中聚集分离器的主视方向结构示意图;
图 5是图 4所示聚集分离器中波纹分离盘的主视方向结构示意图;
图 6是图 5所示波纹分离盘的俯视方向结构示意图；
图 7是图 1所示结构中另一种重力分离器的结构示意图；
图 8是图 1所示结构中膜处理器的结构示意图；
图 9是图 8所示结构中局部 A的结构放大示意图；
图 1 0是图 8所示结构中膜组件的结构示意图；
图 1 1是本发明另一种具体实施方式的流程结构简图。 具体实施方式
如图 1所示，船用油污水处理装置包括通过管道依序相连的加热器 1、重力分离器 2、 抽吸泵 3、滤料过滤器 5以及膜处理器 6; 该滤料过滤器 5的过滤水出口与相互并接的膜 处理器 6过滤水入口 608和通海阀 10相连通。 在抽吸泵 3的作用下， 舱底油污水站 23 中的油污水经油污水输入阀 26进入到加热器 1中， 抽吸泵 3采用螺杆泵； 饱和水蒸汽对 通过加热器 1中的油污水进行预加热至 48°C〜58°C， 最好预加热温度控制在 52°C〜56°C 之间。经预加热后的油污水继续被抽吸至重力分离器 2中，该重力分离器 2的上部为具有 圆拱型顶盖的静置分离腔，下部筒腔内则设有聚集分离器所形成的波纹叠盘油污水流道分 离腔。经重力分离器 2分离的废油从其拱形顶盖部通过废油排放阀 25被排放到废油池 24 中， 重力分离器 2上还有重力分离器反冲洗管 2 1和排污阀 22; 油污水在重力分离器 2 中的水力停留时间为 15min〜25min， 最好在 18min〜22min之间选择； 经重力分离器 2分 离后的分离水通过输送管道上的分离水排出阀 20、 抽吸泵 3以及初滤网板 4而进入滤料 过滤器 5，该初滤网板 4采用 30目〜 4 5目的网板或孔板。滤料过滤器 5采用常见的滤芯 过滤装置， 实施例中其滤芯吸附材料为聚丙烯纤维等高分子纤维， 其滤芯过滤孔径为 30 m, 当然该滤芯材料还可以是木材、 活性炭等常用材料。 考虑到滤料过滤器 5的实际过 滤效率和过滤效果， 滤料过滤器 5的水力停留时间应在 0. 4min〜2min之间， 滤料表面流 速负荷应设计为 3mm3/mm2. s〜 4 mmVmm2. s (在每秒时间内每平方毫米滤料表面通过的过滤 水立方毫米数）。 当经过滤料过滤器 5过滤后的过滤水已经符合排放标准时， 过滤水则经 过过滤器排放阀 II 1 9、 防虹吸管 9以及通海阀 10排至舷外。 当过滤水不满足排放标准 仍含有乳化油和溶解油等悬浮油时，过滤器排放阀 II 1 9关闭，分离水经过滤器排放阀 I 18、膜处理器 6的过滤水入口 608进入膜处理器 6。 经膜分离处理后的渗透水再经渗透水 阀 7、止回阀 8、 防虹吸管 9以及通海阀 10排至舷外。膜分离处理装置中的膜组件采用外 压式超滤膜组件。
在膜处理器 6的滤分处理过程中，总是有处理量 15%— 25%的浓縮液经回流阀 11被送 回舱底舱底油污水站 23中； 经过反复试验送回舱底油污水站的浓縮液控制在处理量的 1 8 %〜22%之间具有更好的膜防污染效果。在膜处理器 6的过滤水入口 608处，还并接有排 水阀 15、气体反冲阀 16和药箱截止阀 17。在膜处理器 6每次排水完成后， 压縮空气通过 气体反冲阀 1 6对膜组件的分离膜进行空气清洗;膜处理器 6还可以利用清洁的海水或淡 水对膜组件进行清洗； 长期使用后加药泵 13、 药洗截止阀 12和药箱截止阀 17的协调动 作， 将清洗药箱 14中的清洗药剂循环于膜组件和药箱之间， 使分离膜保持较好的工作通 量， 由于清洗药不断地回用， 膜组件不需要拆下， 方便了船舶上的使用操作， 大大延长了 膜组件的使用寿命。
如图 2所示的加热器 1， 包括加热器壳体 101， 该加热器壳体 101呈圆柱筒状， 使用 时在筒状壳体的外面包裹有隔热材料， 以提高热效率。 在圆柱形筒状的加热器壳体 101 的下部位置， 设置有油污水通入管 103， 加热器壳体 101的上部位置则设置有加热油污水 排出管 108， 油污水经油污水通入管 103进入到加热器壳体 101的筒腔内， 再由加热油污 水排出管 108排出，而被送至油污水重力分离器中。在加热器壳体 101的筒腔内设置有若 干根并列布置的蒸汽加热管 102， 每根蒸汽加热管 102均呈倒置的 U型管状， 其 U型管的 一端为蒸汽入口端，另一端则为蒸汽出口端。在加热器壳体 101的下端密闭地固定连接有 加热管连接座，该加热管连接座具有内置空腔，该内置空腔通过径向布置的分隔隔板分隔 成蒸汽通入腔和蒸汽排出腔，蒸汽加热管 102固定安装于加热管连接座上，倒置的 U型蒸 汽加热管 102的入口端与蒸汽通入腔相连通，蒸汽加热管 102的出口端与蒸汽排出腔相连 通。在加热管连接座上装有蒸汽通入管 105和蒸汽排出管 106; 蒸汽通入管 105位于加热 管连接座的蒸汽通入腔位置，而通向蒸汽通入腔；蒸汽排出管 106位于加热管连接座的蒸 汽排出腔位置而与其连通。在蒸汽排出管 106上安装有常用的疏水阀，工作时该疏水阀自 动地排除蒸汽管路中的冷凝水，并防止蒸汽泄漏。在蒸汽通入管 105上安装有常用的蒸汽 通断阀，以控制蒸汽的流入和截止，以及控制蒸汽的流量大小，达到自动维持恒温的目的。
在图 3所示的重力分离器 2中，重力分离器 2包括筒体 211以及设于其上的油污水进 入口 213、 筒盖 201、 分离水排放口 209、 污泥排放口 210和设置于筒盖 201上的废油排 放口 214。 重力分离器 2的筒腔由筒体 211和与之相连接的筒盖 201构成， 筒体 211和筒 盖 201通过连接法兰 202相连接， 其筒腔大体可分为静置分离腔和流道分离腔； 筒体 211 上部以及其上具有圆拱型的筒盖 201构成静置分离腔，筒体 211下部内则设有由聚集分离 器所构成的波纹叠盘油污水流道分离腔。在筒体 211的筒腔内从上至下依次相邻地设置有 第一聚集分离器 204和第二聚集分离器 207两组聚集分离器，该两组聚集分离器分别位于 导流孔板 206的上、下两侧； 导流孔板 206呈圆盘状结构， 其导流孔板 206的中间位置设 置有导流通孔， 以便使油污水从第一聚集分离器 204流入第二聚集分离器 207。 导流孔板 206的周边通过筒内的焊接支撑圈封闭地固定安装于筒体 211的内壁 上， 以阻挡油污水 从第一聚焦分离器 204的外侧和筒体内壁 间进入筒体的下部空间， 而引导油污水汇集后 从导流孔板 206的导流通孔进入第二聚集分离器 207。
在第一聚集分离器 204的顶端部设有顶部盖板 203，该顶部盖板 203呈平底圆盘状结 构，其周边与筒体 211的内壁间留间隙， 以迫使油污水从第一聚集分离器 204的外侧周边 均匀地沿径向进入第一聚集分离器 204的波纹分离盘 215间的油污水分离流道，而后再汇 集到位于其中间的导流通孔内。该顶部盖板 203则通过支撑螺杆 205与导流孔板 206固定 支撑连接。
在第二聚焦分离器 207的底部固定地设有导流盲板 208，该导流盲板 208也呈平底圆 盘状结构， 它通过位于中间导流通孔内的连接螺杆 212与导流孔板 206及顶部盖板 203 相互固定连接。导流盲板 208阻挡从聚焦分离器中间导流通孔流入的油污水继续沿该通孔 流出，而迫使其均匀上倾地沿径向进入第二聚集分离器 207的波纹分离盘 215构成的油水 分离流道内。经两组聚集分离器分离的分离水已经相当洁净，该分离水沿第二聚集分离器 的周边间隙进入到筒体 211的底腔， 最终经分离水排放口 209排出。
第一聚集分离器 204和第二聚集分离器 207均由若干波纹分离盘 215相互层叠而构 成。 图 4示出了一组聚集分离器的示意结构（以第一聚集分离器为例， 第二聚集分离器具 有相同的结构）。 该结构的聚集分离器包括有若干相互层叠的波纹分离盘 215， 各波纹分 离盘 215呈中间带有导流通孔 216的圆锥形盘状结构，且该锥盘的盘面呈波纹面，该盘面 波纹沿盘面的周向延伸。各波纹分离盘 215以其盘面的波纹峰谷相互交错叠置，从而在相 互错开对置的谷峰间形成径向的油污水分离流道， 由于该油污水流道沿周向（流道宽度方 向） 的高度是从零到最大再至零变化的， 该油污水流道的最大高度应控制为 9mm〜25mm 范围内。该油污水流道径向 （流道长度方向）的截面积从其中心向外侧逐渐变大， 或者从 外侧向中心逐渐变小。
在分离器的外周边可以设置有若干根支撑耳，以便对分离器的固定支撑。 在该结构的 分离器中， 由于采用了波纹盘结构， 各波纹管分离盘 215相互连接十分稳固， 且不需要其 他固定件， 其相互间的间距或分离流道的截面尺寸取决于自身的波纹结构尺寸。
图 5、 图 6示出了分离器中单只波纹分离盘 215的结构示意图。波纹分离盘 215的盘 面锥角 β为 20°，当然根据介质分离条件、具体工作状况， 该盘面锥角 β可以在 15°〜30°之 间进行优选。如图示上述的盘面锥角 β为盘面倾斜母线与水平线间的夹角。该波纹分离盘 215的盘板材料由盘板基材以及覆于该基材上的疏油层构成， 本实施例中， 盘板基材以钢 板为材料，盘板基材上的疏油层涂层材料为现有的疏水油纳米材料，也可以采用聚 4氧化 乙烯等相应的疏油材料。
图 7示出了另一种结构的重力分离器 2，在该重力分离器中， 除筒体 211内的聚集分 离器的组数及与之相关的安装方式与图 2 所示结构有所不同外， 其他结构相同。 在图 7 所示结构中， 在第二聚集分离器 207底侧位置仍设有导流盲板 208， 第三聚集分离器 217 则位于导流盲板 208 的下侧面。 该导流盲板 208仍为呈平底圆盘状的结构， 其周边与筒 体 211的内壁间留有间隙， 以便阻挡水流经分离器的中间通道流入第三聚集分离器 217， 而迫使其从第三聚集分离器 217的外侧向其中间流动。第三聚集分离器 217的底部设有底 部导流孔板 218， 该底部导流孔板 218呈中间带有导流通孔的圆盘状结构， 该底部导流孔 板 218 的周边通过焊接方式封闭地固定安装于筒体 211 的内壁上。 第三聚集分离器 217 进一步分离的分离水经其中间导流通孔流入筒体 211 的下部腔室后， 再经分离水排出口 209排出。
在图 8、 图 9及图 10所示的膜处理器中， 该膜处理器 6包括膜组件 605和金属筒体 610； 膜组件 605有间隙地置于金属筒体 610内， 该膜组件 605包括膜组件外壳 606和滤 膜 607， 它采用超滤膜组件， 当然也可以是微滤膜组件等。 金属筒体 610采用管状结构， 其上、下两端均设有连接法兰盘，材料为 Q 2 3 5。在膜组件 605的顶部套接有顶罩 611， 顶罩 611采用杯形结构， 它倒扣于膜组件 605 的顶部， 且通过连接法兰与金属筒体 610 固定连接，该顶罩 611的上顶端设有渗透水出口 601，其侧面则设有浓縮液引出口 604。该 顶罩 611的内壁与膜组件 605顶部外侧面之间从上向下依次设置有顶端上密封圈 612和顶 端下密封圈 613，顶端上密封圈 612和顶端下密封圈 613均采用二道 0形密封圈。 在膜组 件 605顶部位置的侧面设有膜组件浓縮液出口 602，顶端上密封圈 612和顶端下密封圈 613 位于膜组件浓縮液出口 602的上、下两侧，从而使之与膜组件外壳 606及顶罩 611围成环 形腔 603。 浓縮液引出口 604位于顶罩 611上的环形腔 603位置， 膜组件浓縮液出口 602 通过该环形腔 603与浓縮液引出口 604相连通。 在膜组件 605的底部套接有底罩 609，该 底罩 609的内壁与膜组件 605底部外侧面之间设有底端密封圈 614，该底端密封圈 614采 用二道 0形密封圈。底罩 609也采用杯形结构， 它套扣于膜组件 605的底端部， 且通过连 接法兰与金属筒体 610固定连接， 该底罩 609的底端部位设有过滤水入口 608。底端密封 圈 614阻止过滤水进入膜组件 605与金属筒体 610之间的空间。
在图 10所示的膜组件中， 膜组件 605采用通用件， 但在顶部位置的侧面均匀地增设 了若干膜组件浓縮液出口 602，膜组件浓縮液出口 602等距地设置于膜组件外壳 606的同 一截面上。本实施例中，在膜组件 605上端同一截面上均布有 6个膜组件浓縮液出口 602。 当然该膜组件浓縮液出口 6 数量应根据使用条件、 选用的膜组件规格型号等具体情况在 2〜 1 0个选用， 根据有限次的试验分析该膜组件浓縮液出口 6的数量最好选择为 4〜 8 个。在膜组件浓縮液出口 602所在横截面的上、 下侧还增设了上、 下密封槽， 以便安装密 封圈。 在膜组件 605的底端外侧面也增设有密封槽。
图 1 1示出了本发明的另一种实施方式， 除滤料过滤器 5的结构与上述实施例不同 外， 其他结构相同。在本实施例中， 其滤料过滤器 5采用两级过滤， 滤芯吸附材料仍采用 聚丙烯纤维等高分子纤维， 但一级滤料过滤器 5 1的滤芯过滤孔径为 50 μ πι， 而二级滤料 过滤器 5 2的滤芯过滤孔径为 30 μ πι; 两级滤料过滤器 5 的水力停留时间均设计为 0. 4min〜2min之间， 滤料表面流速负荷均应设计为 3mm3/mm2. s〜 4 mmVmm2. s。 经一级滤料 过滤器 51过滤后的过滤水满足排放要求时打开过滤水排放阀 I 27， 过滤水经过滤水排放 阀 I 27、 防虹吸管 9及通海阀 10排至舷外。 当过滤水不满足排放要求时关闭过滤水排放 阀 I 27， 经一级滤料过滤器 51过滤的过滤水进入到二级滤料过滤器 52， 经二级过滤的过 滤水再通过水排放阀 28输送至膜处理器 6中进行膜分离处理。

Claims

权利要求书
1、 一种船用油污水分离处理方法， 其特征是该分离处理方法包括以下步骤： 首先对 舱底油污水进行预加热处理， 使其预加热至 48°C〜58°C ; 再将预加热后的油污水送到重 力分离装置， 使油污水流过该重力分离装置中的若干层油污水流道， 进行油滴聚集和油水 重力分离而分离出废油和分离水；该重力分离装置中的油污水流道最大高度为 9mm〜25mm， 油污水在重力分离装置中的水力停留时间为 15min〜25min; 经重力分离装置分离后的废 油排出， 分离水则再经输送管道输送至滤料过滤装置； 分离水在所述滤料过滤装置中的水 力停留时间为 0. 4min〜2min， 滤料表面流速负荷为 3mm3/mm2. s〜 4 mmVmm2. s ; 经滤料过滤 装置过滤后的过滤水再经输送管道输送至膜分离处理装置， 将膜分离处理装置 15%〜25% 处理量的浓縮液继续送回舱底油污水站， 余下浓縮液回收， 膜分离处理装置的渗透水排出 舱外。
2、 根据权利要求 1所述的船用油污水分离处理方法， 其特征是： 所述油污水预热处 理采用蒸汽加热， 并通过蒸汽将油污水预加热到 52°C〜56°C。
3、 根据权利要求 1所述的船用油污水分离处理方法， 其特征是： 所述重力分离装置 中油污水流道最大高度为 16mm〜20mm， 油污水在重力分离装置中的水力停留时间为 18mir！〜 22min。
4、 根据权利要求 1所述的船用油污水分离处理方法， 其特征是： 所述膜分离处理装 置中的膜组件采用外压式超滤膜组件， 将 1 8 %〜22%处理量的浓縮液送回舱底油污水站。
5、 一种实现权利要求 1所述油污水分离处理方法的船用油污水处理装置， 其特征是 该油污水处理装置包括加热器 （ 1 )、 重力分离器 （ 2 )、 抽吸泵 （ 3 )、 滤料过滤器 （ 5 ) 以及膜处理器（ 6 )，所述加热器（ 1 )、重力分离器（ 2 )、抽吸泵（ 3 )、滤料过滤器（ 5 ) 以及膜处理器 （ 6 )通过管道依序相连通； 所述加热器 （ 1 ) 的油污水通入口连向舱底油 污水站 （ 2 3 )， 所述膜处理器 （ 6 ) 的渗透水出口与通海阀 （ 1 0 ) 相连通； 所述抽吸 泵（ 3 )位于连通重力分离器（ 2 )和滤料过滤器（ 5 ) 的管道上； 在所述膜处理器（ 6 ) 的油污水入口处还并连有气体反冲阀 （ 1 6 )。
6、 根据权利要求 5所述的船用油污水处理装置， 其特征是： 所述加热器 （ 1 ) 包括 加热器壳体（101 )， 该加热器壳体 （101 ) 上设置有油污水通入管 （103 )和加热油污水排 出管 （108 ); 油污水通入管 （103 ) 和加热油污水排出管 （108 ) 与加热器壳体 （101 ) 筒 腔相连通； 所述加热器壳体（101)筒腔内设置有蒸汽加热管（102)， 该蒸汽加热管（102) 两端分别通向蒸汽通入管 （105) 和蒸汽排出管 （106)。
7、 根据权利要求 5所述的船用油污水处理装置， 其特征是： 所述重力分离器 （ 2 )， 包括筒体 （211) 以及设置于筒体 （211) 上的油污水进入口 （213)、 废油排放口 （214) 和分离水排出口 （209); 在所述筒体 （211) 内至少设置有第一聚集分离器（204)和第二 聚焦分离器（207)， 该第一聚集分离器 （204)和第二聚集分离器（207) 分别位于导流孔 板 （206) 的上、 下两侧， 该导流孔板 （206) 的周边封闭地固定安装于筒体 （211) 的内 壁上， 导流孔板 （206) 的中间位置设有导流通孔； 所述第一聚集分离器（204) 的顶端设 有顶部盖板 （203)， 该顶部盖板 （203) 的周边与筒体 （211) 内壁间留有间隙； 所述第二 聚集分离器 （207) 的底部设有导流盲板 （208)， 该导流盲板 （208) 的周边与筒体 （211) 的内壁间留有间隙； 第一聚集分离器 （204) 和 /或第二聚集分离器 （207) 包括若干相互 叠置的波纹分离盘 （215)， 该波纹分离盘 （215) 呈锥盘状且盘面为波纹面， 相邻波纹分 离盘 （215) 以其波纹峰谷相错叠而形成径向的油污水流道， 该油污水流道的最大高度为 9mn！〜 25mm。
8、 根据权利要求 7所述的船用油污水处理装置， 其特征是： 所述波纹分离盘 （215) 的波纹沿盘面周向延伸， 该波纹锥形盘 （215) 的中间设有通孔； 波纹分离盘 （215) 的盘 面锥角 β =15°〜30°。
9、 根据权利要求 5所述的船用油污水处理装置， 其特征是： 所述膜处理器 （ 6 ) 包 括膜组件 （605)， 该膜组件 （605) 设置于金属筒体 （610) 内， 金属筒体 （610) 的上、 下两端分别固定连接有底罩 （609)和顶罩 （611); 在所述膜组件（605) 同一端至少设置 有二个膜组件浓縮液出口 （602)， 该膜组件浓縮液出口 （602) 与浓縮液引出口 （604)相 连通。
10、 根据权利要求 5— 9中任一项权利要求所述船用油污水处理装置， 其特征是： 所 述滤料过滤器（ 5 ) 的过滤水出口与相互并接的膜处理器 （ 6 ) 过滤水入口 （ 6 0 8 )和 通海阀 （ 1 Q ) 相连通。
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