WO2011032464A1

WO2011032464A1 - Method for separating and disposing oily wastewater in ship and disposing device thereof

Info

Publication number: WO2011032464A1
Application number: PCT/CN2010/076650
Authority: WO
Inventors: 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
Priority date: 2009-09-17
Filing date: 2010-09-06
Publication date: 2011-03-24
Also published as: CN101654150B; CN101654150A

Abstract

Disclosed is a method for separating and disposing oily wastewater in ship, which comprises the following steps: preheating bilge water to 48-58 degrees Centigrade; separating the bilge water into a waste oil and separated water through oil drop aggregation and oil-water gravity separation; filtering the separated water into a filtered water by a filter-material filter and sending the filtered water into a membrane processor; and recovering the concentrated solution and discharging the infiltration water outside cabin. Disclosed is also a device for disposing oily wastewater in ship, which comprises a heater (1), a gravity separator (2), a suction pump (3), a filter-material filter (5) and a membrane processor (6) communicated with each other sequentially. An oily water inlet of the heater (1) is connected to a bilge water station (23), and an infiltration water outlet of the membrane processor (6) is communicated with a sea valve (9) by a anti-siphon pipe (10). The device for disposing oily wastewater in ship of the present invention not only can separate high-density residual oil from the oily wastewater, but also can effectively separate emulsion from the oily wastewater.

Description

Instruction manual

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

With the rapid development of the world shipping industry and the rapid increase of ship tonnage, improper discharge of ship bilge oil has become the most important form of marine pollution caused by ships. After the ship's oily sewage is discharged into the marine water body, a very thin oil film is formed on the surface of the water body. According to the data analysis, 1 ton of oil is discharged to the water surface, and 5 × 10W oil film pollution can be formed. This oil film directly hinders the atmosphere. Oxygen is transferred to the water body, causing the water body to be deprived of oxygen, and the aquatic organisms die due to lack of oxygen; the oil products also have certain toxicity, especially for juvenile fish and fish eggs. In addition, a large number of oil films may even cause fires and affect water. traffic. The discharge of bilge oil from ships has brought enormous threats to marine environmental protection.

To this end, the International Maritime Organization and governments have successively issued a series of maritime laws and regulations to minimize the problem of ship pollution. The IMO Maritime Environmental Protection Committee also discharges the oil content of bilge water in coastal areas and special areas. The regulation of not exceeding 15ppm has been extended to all sea areas, and the marine oil sewage treatment plant has become a mandatory ship discharge treatment device. MEPC. 107 (49), adopted by the International Maritime Organization on July 18, 2003, puts more stringent standards on 15ppm bilge oil sewers and alarms, and raises the density of separation heavy oil from 940kg/m ³ to 980kg. /m ³ or more, and increased the treatment requirements for emulsified oil; oily sewage containing emulsified oil, especially chemical emulsified oil containing surfactant, has always been a major problem in the field of oily wastewater treatment, so the previous correlation Neither the regulations nor the emission standards have proposed the treatment requirements for emulsified oils and the test requirements for treatment equipment.

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. However, the density of the residue with a density above 980 kg/m ³ is relatively high. In addition to the presence of 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. 107 (49), 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.

Although people pass the separation of gravity by mechanical separation of the oil droplet aggregator, and then through the membrane filtration separation, In theory, this separation method can realize the separation treatment of the emulsified oil. However, since the separation membrane is trapped in the emulsified oil, the accumulation of the retentate on the surface of the membrane will produce a thin layer of the gel layer on the surface of the membrane, resulting in separation. Membrane fouling is more serious because the separation membrane is usually lipophilic. During the separation process, the oil droplets, solids and water in the oil wastewater cannot be completely separated due to the previous treatment method. During the membrane separation process, the rapid flow of the liquid makes the oil droplets And the solid impurities quickly enter the dense pores, causing internal clogging of the membrane, contamination of the membrane surface and clogging of the membrane pores so that water molecules cannot pass through the dense micropores in the side pressure and enter the other side of the membrane. Tests have shown that the membrane flux of this structure is significantly reduced in just a few weeks or even days, and the membrane flux generally decreases exponentially with time, so it is only from the separation device. Removing the separation membrane for cleaning or renewing the separation membrane not only significantly increases the operating cost of the separation device, but is also very difficult under conditions where the ship space is very limited.

Because the existing oil and sewage separation treatment device is limited by the separation structure and the separation method in the gravity separation stage, it is impossible to separate the residue wastewater containing high density, and can not effectively eliminate the oil droplet component and solid in the oil sewage. Impurities, and the burden of the membrane separation stage, causes the membrane separation to quickly fail, and the functional separation of the separation stages of the separation treatment device occurs, which cannot be blamed, and eventually the entire device cannot work normally. Summary of the invention

In view of the above-mentioned deficiencies of the prior art, 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.

In order to solve the above technical problem, 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! ~ _25min; separated oil is discharged by gravity separation means, the separation of water through the pipeline and then conveyed to the filter media means; HRT in the filter material in the filter apparatus for the separation of water 0. 4min~2min, filtered The material surface flow rate load is 3mm ³ /mm ² . s~ 4 mmVmm ² . s ; the filtered water filtered by the filter material filtering device is transported to the membrane separation processing device through the conveying pipeline, and the membrane separation processing device is 15%~25% The treated amount of concentrated liquid is continuously returned to the bilge oil sewage station, and the remaining concentrated liquid is recovered, and the permeated water of the membrane separation processing device is discharged outside the tank.

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 .

Secondly, due to the gravity separation method of the flow channel with multiple layers of oily sewage channels, 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. At the same time, reasonable channel height and hydraulic retention time are used, which also ensures the continuous and stable operation of the separation device. Although 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.

Thirdly, since 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.

Fourth, 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.

Fifth, a partial reflux of the concentrate is used in the membrane separation to avoid dead end operation of the separation membrane. Considering the cleaning of the membrane surface and the membrane treatment efficiency, 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.

In the separation process of the present invention, 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.

In a preferred embodiment of the present invention, 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.

In order to realize the marine oil sewage separation treatment method of the present invention, 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.

In the oily sewage treatment device of the present invention, after the above structure is adopted, since the heater, the gravity separator, the suction pump, the filter filter, and the membrane processor are sequentially connected, 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 emulsified oil, and the membrane treatment The device can perform airflow backwashing immediately in use, which stabilizes the flux of the membrane module. Therefore, in the processing apparatus of the present invention, the process equipment of each step is arranged reasonably and the functions are complementary, and the oil sewage containing the higher density residue, the suspended solid impurities and the emulsion is efficiently and efficiently separated and processed.

In a preferred embodiment of the present invention, 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.

In the above structure, since 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. Moreover, since the steam heating pipe located in the cavity of the heater casing is made of saturated water vapor as a heating medium for the oil sewage, 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.

According to still another preferred embodiment of the present invention, 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 Above, 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 comprises a plurality of corrugated separating plates stacked on each other The corrugated separating disc has a cone-shaped shape and the disc surface is a corrugated surface, and the adjacent corrugated separating discs form a radial oily sewage flow channel with the corrugated peaks and valleys being stacked, and the maximum height of the oily sewage flow channel is 9 mm to 25 mm.

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. In this case, 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. Always in high efficiency separation. At the same time, 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. In particular, 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. A multiple of the number of discs. Moreover, since 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. The 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. On the other hand, 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. Further, since the maximum height of the oily sewage passage is designed to be 9 mm to 25 mm, 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; Although 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. At the same time, 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.

According to still another preferred embodiment of the present invention, 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. DRAWINGS

The present invention will be further described in detail below in conjunction with the drawings and specific embodiments.

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;

Figure 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;

Figure 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

As shown in FIG. 1, 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. Under the action of the suction pump 3, the oil sewage in the bilge oil sewage station 23 enters the heater 1 through the oil sewage input valve 26, and 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 corrugated stacked oil oil sewage channel separation chamber. 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 suction pump 3 and the primary filter screen 4 enter the filter filter 5, and the primary filter screen 4 uses a mesh plate or orifice plate of 30 mesh to 45 mesh. The filter medium filter 5 adopts a common filter element filtering device. In the embodiment, 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. Of course, the filter element material may also be a common material such as wood or activated carbon. Considering the actual filtration efficiency and filtration effect of the filter material filter 5, 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 . s (the number of millimeters of filtered water passing through the surface of the filter material per square millimeter per second). When the filtered water filtered by the filter filter 5 has met the discharge standard, the filtered water passes through the filter discharge valve II 1 9 , the anti-siphon 9 and the through-sea valve 10 to the outboard. When the filtered water does not meet the discharge standard and still contains the suspended oil such as emulsified oil and dissolved oil, 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.

During the filtration process of the membrane processor 6, there is always a throughput of 15% - 25% of the concentrate returned to the bilge sump sewage station 23 via the return valve 11; after repeated trials, the bilge is returned The concentrate of the oil sewage station is controlled to have a better membrane anti-pollution effect between 18% and 22% of the treatment volume. 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. 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. In the lower portion of the cylindrical cylindrical heater housing 101, 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.

In the gravity separator 2 shown in FIG. 3, 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. 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 (the length of the flow path) 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. In 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.

5 and 6 show a schematic view of the structure of a single corrugated separating disc 215 in the separator. The disc surface taper angle β 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 β can be between 15° and 30°. It is preferred to carry out between. As shown in the figure, the disk surface taper angle β 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. In the configuration shown in Fig. 7, 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.

In the film processor shown in FIGS. 8, 9, and 10, 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. 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.

In the membrane module shown in Fig. 10, 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. In this embodiment, six membrane module concentrate outlets 602 are evenly distributed on the same section of the upper end of the membrane module 605. Of course, 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. Choose from 4 to 8. 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. In the present embodiment, 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 μπι, and The filtration filter diameter of the filter element of the filter material of the grade 2 filter is 30 μ πι _; 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 . s~ 4 mmVmm ² . s. When the filtered water filtered by the primary filter filter 51 meets the discharge requirement, 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. When the filtered water does not meet the discharge requirement, 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.

Claims

Claim

A method for separating and treating marine oil sewage, characterized in that the separation treatment method comprises the following steps: First, pre-heating the bilge oil sewage to preheat it to 48 ° C to 58 ° C; The oily sewage is sent to the gravity separation device, so that the oil sewage flows through several layers of the oil sewage flow channel 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 in the gravity separation device The maximum height of the water channel is 9mm~25mm, and the hydraulic retention time of the oil sewage in the gravity separation device is 15min~25min; the waste oil separated by the gravity separation device is discharged, and the separated water is transported to the filter material filtering device through the conveying pipeline; The water retention time of the separated water in the filter material filtering device is 0. 4min~2min, and the surface flow load of the filter material is 3mm ³ /mm ² . s~ 4 mmVmm ² . s ; filtered by the filter device The water is transported to the membrane separation treatment device through the pipeline, and the 15%~25% of the concentrate of the membrane separation treatment device is continuously sent back to the bilge oil sewage station, and the remaining concentrate is recovered. Permeated water discharge processing apparatus EVA.

2. The method for separating and treating marine oily sewage according to claim 1, wherein: the oil sewage preheating treatment is performed by steam heating, and the oil sewage is preheated to 52 ° C to 56 ° C by steam.

3. The method for separating and treating marine oily sewage according to claim 1, wherein: the maximum height of the oily sewage passage in the gravity separation device is 16 mm to 20 mm, and the hydraulic retention time of the oil sewage in the gravity separation device is 18 mir! ~ 22min.

The method for separating and treating marine oily sewage according to claim 1, wherein: the membrane module in the membrane separation processing device adopts an external pressure type ultrafiltration membrane module, and the treatment amount is 18%~22%. The liquid is returned to the bilge oil sewage station.

A marine oil sewage treatment device for realizing the oil sewage separation treatment method according to claim 1, characterized in that the oil sewage treatment device comprises a heater (1), a gravity separator (2), a suction pump (3) a filter filter (5) and a membrane processor (6), the heater (1), a gravity separator (2), a suction pump (3), a filter filter (5), and a membrane processor ( 6) sequentially connected through the pipeline; the oil sewage inlet of the heater (1) is connected to the bilge oil sewage station (23), the permeate water outlet of the membrane processor (6) and the sea valve (1) 0) connected; the suction pump (3) is located on a pipe connecting the gravity separator (2) and the filter filter (5); and is further connected at the oil sewage inlet of the membrane processor (6) There is a gas recoil valve (16).

The marine oil sewage treatment device according to claim 5, wherein the heater (1) comprises a heater casing (101), and the heater casing (101) is provided with an oil sewage inlet pipe (103) and heating oil sewage discharge pipe (108); oil sewage inlet pipe (103) and heating oil sewage discharge pipe (108) and heater casing (101) The cavity of the heater housing (101) is provided with a steam heating pipe (102), and the two ends of the steam heating pipe (102) respectively lead to a steam inlet pipe (105) and a steam discharge pipe (106) .

7. The marine oil sewage treatment device according to claim 5, wherein: the gravity separator (2) comprises a cylinder (211) and an oil sewage inlet port (213) disposed on the cylinder (211). a waste oil discharge port (214) and a separation water discharge port (209); at least a first collecting separator (204) and a second focus separator (207) are disposed in the cylindrical body (211), the first A collecting separator (204) and a second collecting separator (207) are respectively located on upper and lower sides of the guiding orifice plate (206), and the periphery of the guiding orifice plate (206) is fixedly fixedly mounted to the cylinder body ( The inner wall of the 211) is provided with a flow-through hole at an intermediate position of the flow guide plate (206); a top cover plate (203) is disposed at a top end of the first gatherer (204), and the top cover plate (203) There is a gap between the periphery of the cylinder and the inner wall of the cylinder (211); a bottom of the second gathering separator (207) is provided with a guiding blind plate (208), and the periphery of the guiding blind plate (208) and the cylinder body ( 211) leaving a gap between the inner walls; a first collecting separator (204) and/or a second collecting separator (2) 07) comprising a plurality of corrugated separating discs (215) stacked on each other, the corrugated separating discs (215) having a truncated disc shape and a disk surface having a corrugated surface, and the adjacent corrugated separating discs (215) being formed by overlapping the corrugated peaks and valleys Radial oily sewage channel, the maximum height of the oily sewage channel is 9mn! ~ 25mm.

The marine oil sewage treatment device according to claim 7, wherein: the corrugation separation disk (215) has a corrugation extending in a circumferential direction of the disk surface, and a through hole is formed in the middle of the corrugated conical disk (215); The disk cone angle of the corrugated separating disc (215) is β = 15 ° ~ 30 °.

9. The marine oil wastewater treatment apparatus according to claim 5, wherein: the membrane processor (6) comprises a membrane module (605), and the membrane module (605) is disposed in the metal cylinder (610). A bottom cover (609) and a top cover (611) are fixedly connected to the upper and lower ends of the metal cylinder (610); at least two membrane module concentrate outlets are disposed at the same end of the membrane module (605) ( 602), the membrane module concentrate outlet (602) is in communication with the concentrate outlet (604).

The marine oil sewage treatment device according to any one of claims 5-9, characterized in that: the filtered water outlet of the filter filter (5) and the membrane processor (6) connected to each other The filtered water inlet (600) is connected to the seawater valve (1Q).