DE19527410A1 - Process for treating waste water - Google Patents

Abstract

A method of treating wastewater containing particulate matter and free oil, which method comprises removing free oil from the wastewater, passing the wastewater through a first filtration medium having an effective pore rating of about 200 mu m or less, subjecting the wastewater to dynamic filtration utilizing a second filtration medium having an effective pore rating of about 5 mu m or less, and contacting the wastewater with an adsorbent bed to form a purified water stream. An apparatus which can be used to carry out the method is described.

Description

The invention relates to a method for treating Ab water according to the preamble of claim 1, and a device for performing such a method.

For the prior art, reference is made to DE 43 25 335 A1 sen.

First of all, it has the invention with a Fluidbe procedures to do. In particular, it relates an improved process for treating wastewater, especially gray water to withdraw purified water win, and reduce wastewater runoff. Finally The invention also relates to a device for performing such a wastewater treatment.

Treatment of waste water to reduce unwanted Drains and for the recovery or recirculation of usable water is a matter of the utmost Importance in the context of general efforts to reduce pollution and water save up. The handling of is of particular interest Gray water on board ships and boats, for example Sea gray water. Greywater is defined as the com Bound wastewater outflows from ships Cooking kitchens, washing-up kitchens, dishwashers, laundry  travel, showers, sinks and sinks (including feet floor drains in work areas such as Ma machine rooms and medical areas). Both Pollutants are usually food particles up to considerable dimensions (for example Food slices), animal fats, vegetable oils, be fen, detergents, body oils, human hair, metal particles from washing-up kitchens and machine rooms, solutions medium and small items of clothing (e.g. Soc ken) that make their way through the laundry system have found. Greywater is usually used by both Black water distinguished, which one on salt water based collection of body waste and paper materials alien is from collection rooms located on ships, so like bilge water, which is based on salt water accumulation of all other waste water on board is and ent chemical solvents and the like ent can hold.

Although in its extent as in its con highly variable in concentration and type of contaminants, is gray water to an average extent of et wa 55 to 75 l (15 to 20 gallons) per person per day Generated on board a ship. For example, the Gray water production on the order of about 15,000 l / day (4000 gal / day) on a marine frigate with a crew of 200, up to about 450,000 l / day (120,000 gal / day), on an aircraft carrier with a load statute of 6000. Average greywater Flow speeds on board such ships can from about 10 l / min (2.8 gal / min) to about 315 l / min (83.3 gal / min) range, with top speeds of  about 32 l / min (8.4 gal / min) to about 950 l / min (250 gal / min) can be enough.

Conventional coalescence and centrifugal separators are unsuitable for the treatment and cleaning of gray water net because, for example, the viscosities and surfaces tensions of soaps and water too close together to allow satisfactory separation. Lots Ships leave gray water in directly without treatment navigable waters, including lakes and bodies of water near the coast. Some ships have a concentra tion, retention and transfer tanks for the purpose of a Storage of gray water equipped until it is in one ha sanitary system can be pumped. These Ships use the concentration, retention and Transfer tanks with the intention of draining gray avoid water in lakes and bodies of water in coastal areas, however, routinely leave gray water on the high seas or when the tanks are full, ship to others bare waters. In the increasingly larger areas in which draining gray water is prohibited find expensive and cumbersome tools at for example, the discharge of stored gray water Tanker, application, or the prohibitions become simple ignored.

Thus, there remains a need for an effective and efficient one economic means to reduce waste water runoff, especially to reduce gray water drainage on ships.

It is an object of the invention to provide means for such Specify treatment.  

Furthermore, it is an object of the present invention, Ab Concentrate water spills to keep them spilled making it easier to access and process so ultimately cleaned, re-used from wastewater to make the water available. It is further a concern of the present invention, means for loading treatment of wastewater, especially greywater hen, with the help of which domestic water is recirculated and thus Water can be saved. These and other objectives and advantages of the invention as well as additional invention Features result from the description below.

The invention mediates a method and devices for the treatment of waste water. The procedure and the pre directions are particularly suitable for the treatment of ab water containing material from macro particles and free oil, especially greywater as it occurs at sea.

The process according to the invention for treating waste water containing macro particles and free oil The following steps: Remove the free oil from the Ab water, passing the waste water through a first fil Term medium with an effective pore size of approximately 200 µm or less, subjecting wastewater to dynamic Filtration using a second filter medium with an effective pore size of about 5 µm or less, and contacting the wastewater with an adsorption bed, so as to form a purified water stream.

An inventive device for the treatment of Ab water containing macro particles Substances and free oil include the following characteristics: (a)  Means for removing free oil from waste water; (b) means for passing the waste water after the ent removing the free oil from a first filter medium; (c) a first filter medium with an effective pore size of about 200 µm or less; (d) means of passage of waste water after passing through the first filter medium in a dynamic filter apparatus; (e) a dy Named filtration arrangement with a second filter meter dium, which has an effective pore size of about 5 microns or owns less; (f) means for passing the waste water sers after passing through the second filter medium in an adsorption bed; and (g) an adsorption bed.

The present invention is based on the finding that Waste water can be treated so that contaminants in the Wastewater can be concentrated and that there is a current nigt water results in that the waste water for the purpose subject to removal of larger particles and free oil is that the wastewater of a dynamic filtration is subjected to a filter medium with an effec tive pore size of about 5 µm or less is used, and that then the wastewater with a suitable adsorpti on bed is contacted to remove residual dirt remove fabrics. The cleaned water flow can finally treated according to the circumstances, rezirku be gated and / or drained while the concentrate streams also treated or for the purpose of further Disposal can be retained.

Although the invention is particularly for the treatment of Gray water, especially gray water occurring at sea, the method according to the invention is suitable  and also use the device according to the invention to treat other types of wastewater. Other advantageous te applications of the invention include the treatment of Waste water from factories in the food industry, at for example breweries, bakeries, dairy farms, briken, in which sweet potato starch is treated, Ge wing processing plants, laundries, textile factories, pharmaceutical factories and the like. The invention is discussed below in connection with the treatment of the gray water occurring at sea, the specialist knows, however, that the invention has other uses suitable is.

The invention is intended when applied to the loading treatment of waste water at sea the quantity and / or the concentrations of different contaminants Levels are returned that are below normal values for absorbing water, namely those natural Waters into which the gray water from a ship emptied can be left. The typical characteristics of greywater and absorbing water are given below.

The total solids (TS) are the sum of the suspended Total solids (TSS) and total dissolved solids. The total solids are the rest after evaporation would remain. Biochemical oxygen demand (BOD) represents the amount of dissolved oxygen that is rend stabilizing the decomposable organic Ma terials through aerobic biochemical action in the Water is required. The chemical oxygen demand (COD) is a measure of the amount of water present NEN oxidizable components.

The invention is therefore particularly suitable for loading treatment of waste water containing: at least about 150 mg / l total solids, at least about 100 mg / l sus oscillated total solids, at least about 100 mg / l BOD, at least about 200 mg / l COD and / or at least about 15 mg / l oils and fats. Such wastewater can also cola-like faecal germs, for example in one Concentration up to about 10⁶, 10⁸ or more germs per 100 ml. The wastewater can also contain residual chlorine, for example in a concentration up to about 20 mg / l or more  hold, as well as less than about 5 mg / l of dissolved acid substance, but possibly essentially none dissolved oxygen. The pH of such waste water can generally have any value, depending on the Stability of the equipment used, even though it is available de Invention advantageously at pH values of about 5 to 12 is applied.

Treatment of waste water in accordance with the Er invention partially closes the gradual separation particles from the wastewater stream. While a sol cher separation process when removing suspended par particles from the wastewater can be effective, it becomes habitual Lich wished to prefer the wastewater in this way treat that free oil is removed, and then then treat the draining water further so that other contaminants are removed. The preferred Embodiment of the invention includes such pre and Post-treatments.

Waste water is preferred by the present invention treated in such a way that the stream of purified what ser less than about 150 mg / l, preferably less than about 30 mg / l total solids, less than about 100 mg / l, preferably less than about 30 mg / l of suspen total solids, less than about 100 mg / l preferably less than about 30 mg / l of BOD, less than et wa 100 mg / l, preferably less than about 90 mg / l of COD, and contains less than about 15 mg / l of oils and fats. The cleaned water stream also preferably has less than about 14 coli-like faecal germs per 100 ml less than about 0.0002 mg / l residual chlorine and at least about  5 mg / l of dissolved oxygen. The pH of the cleaned Water flow is preferably about 6 to 9, in particular especially around 6.5 to 8.5. With the particularly preferred The embodiment of the invention is suitable for use Reduced water flow for draining in limited intake capable waters in accordance with US requirements sen, d. H. the purified water stream contains less than about 30 mg / l total suspended solids, less than about 30 mg / l BOD, less than about 14 coli-like faeces germs per 100 ml, less than about 0.0002 mg / l residual chlorine and at least about 5 mg / l of dissolved oxygen in egg pH of about 6.5 to 8.5.

The pretreatment of the wastewater before it becomes a dyna Mixing filtration is preferably included the removal of free oil. Then the wastewater passed through a first filter medium. Free oil can run out the waste water in any suitable manner be removed, preferably by contacting the waste water sers with a material such as cotton preferably in the form of terry cloth, which is free oil absorb. The first filter medium preferably has one effective pore size of about 200 microns or less, esp especially about 160 µm or less. The removal of free Oil and relatively large particles from wastewater, before it is subjected to dynamic filtration, is carried out so that a suitable mode of operation of the guarantee subsequent dynamic filtration process is steady, with premature contamination ("digestion") the filter medium is avoided, which in the dynami filtering application.  

To continue the effective treatment of wastewater lighter, it is preferably through before the passage the first filter medium (and preferably also before Ent removal of the free oil, although this is not absolutely necessary derlich) is passed through a sieve. Anyone can suitable sieves are used, for example a dop pel strainer. The sieve is designed so that it has larger, particulate materials (e.g. hair, laundry counter stands and the like) removed. For example, it can a perforated plate or in particular also act as a mesh screen. A suitable stitch Sieve can have any suitable configuration, it however, preferably has about 4 to 20 wires per (line arem) centimeters (10 to 50 wires per linear inch) each the direction, with each matching wire diameter, for example about 50 to 500 µm (0.002 to 0.02 inches) in Question is coming. In particular, such a mesh screen has approximately 8 to 16 wires per (linear) centimeter (about 20 to 40 Wires per linear inch), preferably about 20 wires per (linear) centimeter (about 30 wires per linear inch), and in any direction, passing any suitable wire knife, for example about 50 to 500 µm (about 0.002 to 0.02 inch), especially about 125 to 250 µm (about 0.005 up to 0.01 inch) can be selected. The strainer is removed preferably particles with a diameter larger than little least about 1000 microns, especially larger than at least et wa 600 µm.

The sieve is preferably dimensioned so that the stoppage frequency is reduced while at the same time so much Macro particles are retained as possible, especially macro particles, which have a satisfactory operating mode  se of the first filter medium. Around To ensure continuous operation, will be done preferably used a switchable twin wire in such a way that if a sieve becomes blocked, it will stop working taken and the current switched to the second sieve becomes. The decommissioned sieve is then used washed back of a suitable agent, for example with the help of a relatively small amount of sieved water or purified water or by air impulse device exercises. In this way, the sieve is used for the purpose cleaned after later recommissioning. Some drain can be directed into a concentrate tank and later Use can be supplied. Backwashing can also be carried out automatically in order to avoid the necessity avoid having an operator in the process takes hold.

Furthermore, the waste water is preferably also returned holding tank passed before it passed through the first filter medium runs through (and preferably also before it exists if the sieve passes or before free oil is removed, although again this is not absolutely necessary is). The retention tank is preferably constructed so that from the wastewater carried high density materials fall and settle on the bottom of the tank where through effective separation from wastewater. At for example, the retention tank can also be baffle plates or the like, and / or the tank outlet can with close distance, e.g. B. several centimeters above Tank bottom be arranged so that entrained in the waste water High density materials stick to the bottom of the tank can settle. In this regard, the bottom of the  Retention tanks have a removable lid to keep the ge Occasional periodic removal of high contaminants To facilitate density. The sieve and / or the means for Removal of free oil can include in the retention tank be what the preferred embodiment of the invention is. In particular, the retention tank preferably contains sloping surfaces such that the wastewater is old must flow natively upwards and downwards, whereby these Sloping surfaces not only the removal of materials ho density from the wastewater also support contribute to separating free oil from waste water.

In addition to facilitating the removal of higher density The retention tank conveys materials from the wastewater also a compensation for the waste water. The Vo lumen and the concentration of pollutants in the waste water during the day in special cases, at for example on board ships, vary. Consequently subsequent treatment gives better results, if the variations in flow velocity and con concentration by the retention tank to a certain Average or balanced. A sol Compensation can also have a special effect ways in the outlet of BOD, pH and other parameters to have. Furthermore, in many applications, in particular on board ships, the retention tank advantageously dimensioned so that it accumulates and retains a volume, which is a peak current for a reasonable period of time is equivalent, for example about an hour to a few Hours so as to ensure that the treatment system not during periods of excessive wastewater production is overwhelmed (although the retention tank volume is smaller  or larger, depending on the specific wastewater generation and the capacity of the treatment system).

At any point in the pretreatment process, preferably before the waste water passes through the first filter me dium and preferably after passing through a ge dedicated retention tank for removing high-density materials alien, the wastewater can have any suitable action which are the size of the particles in the Ab reduced water, for example contact with rotie wings or blades, so the distance lighter particles without the subsequent To adversely affect filter media in an impermissible manner rivers. The means by which the particle size is reduced is adorned can also be the means by which Help remove the wastewater from the retention tank and to Is passed downstream for further treatment purposes, for example to the sieve or the first filter medium. So can e.g. B. the outlet of the retention tank using a suitable fluid line with a maceration pump be bound. The maceration pump pulls out waste water from the retention tank, reduces solid materials smaller particles and delivers the pressure with which the Ab water is pushed through the rest of the treatment system. The maceration pump can be outside the retention tank or be arranged within the same. If a Ma zerations pump is used, it is preferably on an integral inlet strainer attached, which in the Retention tank is used and allowed that ange collected dirt to the bottom of the retention tank for the purpose a subsequent distance can. The inlet sieve is preferably dimensioned such that  the cleaning frequency is reduced while at the same time all particles of sufficient size, which are otherwise due to the maceration pump could get through will.

Appropriate Che microorganisms are introduced into the wastewater, although this generally there is no need. Such chemi It is possible to discharge waste water with the help of directions are added, for example with the help of Chemical delivery systems. Such a chemical feed system preferably comprises a piston pump and an elec tronic control device such that downstream in installed sensors are able to send signals to the elec to submit tronic control or control device with whose help automatically increases the amount of chemical intake is regulated. The chemical feed pumps can directly connected to storage containers or liquid balloons be, which ent the means to be added to the wastewater hold. The feed can, for example, bend with the help suction hoses. In particular, the waste water acid are added to neutralize it. In addition, the addition of coagulants to the waste water This is done to reduce the separation efficiency of the dynamic To improve filtration arrangement.

After the pretreatment of the wastewater it becomes dynamic subjected to filtration, using a second filter medium with an effective pore size of about 5 µm or less. The dynamic filtration Process is supposed to serve, essentially everything else, from Macro particles to remove existing material in the wastewater  NEN, preferably without the need for another fil tration, for example an ultrafiltration.

At this stage of filtration it turned out to be one effective and practicable gray water treatment system on board a ship that is effective Filtration only using a dynamic Filtra tion can be accomplished. Strictly speaking, näm Lich the effective pore sizes of the filter media are so small and limits the effective areas of the filter media so that both a blockage of the filter media pores and the Formation of cake layers near the filter media surface itself can prove to be problems if ge usual blocking type filter elements are used.

In the case of gray water treatment, there is a forced run block filtration not for a variety of reasons satisfactory like dynamic filtration. Some of them This is due to the fact that the volumes and dirt substance concentrations in general with regard to the Use of pass filters are too high that an effective backwash system would be prohibitively large and that a pre-coating, which is required to compress sensitive or sticky contaminants from the filter medium to keep away from introducing additional chemicals would eventually require that with the conc incinerated waste would have to be disposed of.

Dynamic filtration is an extension of the cross electricity filtration concept. The principle of operation is based on this on, a filter medium free from clogging or digestion hold, by repelling particulate matter  than from the filter element and by interrupting the formation of cake layers near the filter medium. These Results can be achieved with sufficiently quick movements supply of the medium to be filtered relative to the filter medium um, so high shear rates as well as high stroke to exert forces on the particles, for example by Application of rotation, oscillation, vibration or other reciprocating means. The shear force the interface of the fluid filter medium is almost independent dependent on any cross-flow medium velocity, different from tangential or cross filtration techniques (which suffer from other problems, for example early filter clogging due to mass adsorption tion and high and non-uniform pressure drops, ver bound at high tangential speeds along the Filter length, which may cause a backflow through the Filtration medium and a reduction in filtration causes).

Dynamic filtration offers a number of out exercise benefits in connection with the present invention dung. There can be very high shear ratios in the Generate dynamic filtration arrangement to create a ver improved lift to repel small particles averages and / or high flow rates lichen. Increases in flow rate he proved to be approximately linear in some systems with the increased shear force. This means that the required filter areas compared to other filters resources can be drastically reduced. Because a shear force applied uniformly across the system can be practiced, evenly high flow rates  reach speed and across the system maintained so that a progressive fouling process elimi ned and extended filtration times can be realized can. In addition, when using the dyna mix filtration high concentrations of agglomerated Reach particles that ent from the treated medium can be removed.

A dynamic filtration unit has the property that it handles a wide range of contaminants can be adjusted to a noticeably high concentration retained solids to reach over long Periods without the need for filter aids and / or backwashing are operated continuously and a uniformly high filter efficiency to achieve, with the help of the total size of the system can be kept to a minimum. The dynamic filtering direction can have any suitable configuration and usually includes a housing that houses a filter unit with one or more filter media contains as well a means of achieving a relative movement between the filter medium and the waste water. The filter media of the Filter unit and the means to achieve a relative movement between the filtered medium and the filter media dium can each be one of a wide variety neter configurations. Furthermore, a great deal Fold suitable movement means can be used to to exercise the relative movement mentioned, for example Rotati ons, oscillations, vibrations or others back and forth outgoing facilities.

The dynamic filtration arrangement can be any pas  transmit device. Suitable cylindrical dyna Mix filtration systems are in the US patents 3,797,662, 4,066,554, 4,093,552, 4,427,552, 4,900,440 and 4,956, 102. Usable rotating disc system for dynamic filtration are in the US patent specification ten 3,997,447 and 5,037,562 as well as in U.S. patent application dung Serial No. 07 / 812,123. Usable Oszil Lation, reciprocating or vibration arrangements for dynamic filtration are generally described in US Pat Descriptions 4,872,988, 4,952,317 and 5,014,564 ben. Other dynamic filtration devices are shown in Murkes "Fundamentals of Crossflow Filtration", separation and Purification Methods, 19 (1), 1-29 (1990). There are also numerous dynamic filtration options regulations available in stores. To such suitable dyna Mix filtration units include: Pall BDF-LAB, ASEA Brown Bovery rotation CROT filter and New Logic V-SEP. Although the desired particle removal by any suitable dynamic filtration arrangement can be achieved may have been found to use dynamic Vibration filtration, which is what New Logic V-SEP is generally used for Example is in connection with the present inven is particularly suitable.

Dynamic filtration desirably generates shear forces of at least about 20,000 sec ^-1 , preferably at least about 100,000 sec ^-1 . Optimal filtration speeds are achieved at high shear ratios, and since shear damage to the concentrate does not play a role in waste water treatment, maximum use of shear force within practical limits is preferred.

In the dynamic filtration arrangement, any ge suitable filter medium can be used. In general filter media with finer effective pore sizes prefers the need for post-treatment of the Ab to keep water to a minimum or to avoid it entirely. Consequently has an effective pore size of about 5 µm or less, preferably the filter medium an effective pore size of about 1 µm or less preferably about 0.5 µm or less. The dynamic filter medium has in the particularly preferred embodiment the invention has a molecular weight limit of about 200 Dal tone or less. A dynami is particularly desirable filter medium with a reverse osmosis membrane, which is capable of at least 97% salt rejection (what as Equivalent to a membrane with a molecular limit weight of about 50 daltons). The reverse osmo se membrane leading to a salt rejection of at least 97% capable, is the membrane with the finest pores size associated with the present invention of practical usability. After passing through the Ab water due to the dynamic filtration arrangement the wastewater desirably no further fil under passage through a filter medium only needs an ad sorption bed (and possibly other post-filtration treatments such as ozonization and UV bes radiation) to be exposed to any contamination gene to remove.

The dynamic filtration structure is suitable Connect the medium line to a suitable concentrate tank the. The concentrated pollutants from the dynamic  Filtration devices are preferably periodically in drained the concentrate tank. Any suitable Means can be applied to the dynamic Filtra tion arrangement to control, for example also suitable Self-regulation means. Preferably find self-rain Feedback or feedback controls in connection with the Dynamic Filtration Assembly Motor Mechanism On application to sense the need for increased torque, that with the increased viscosity of the concentrated Contamination is connected, and to control valves too press so that concentrated impurities automa can be dispensed into the concentrate tank. At wastewater treatment removes the dynamic fil tration arrangement a lot of particulate load. Ins special removes the dynamic filtration arrangement with vast majority the entire suspended festival substances and reduces the amount associated with the particles part of BOD and COD. The dynamic filtration device also preferably removes unwanted molecules and Ag glomerates, for example those with molecular weights of at least about 500 daltons (up to about 30,000 daltons or more), especially those with molecular weights of at least about 200 daltons, and more preferably Such as those with molecular weights of at least about 50 Dalton. When treating wastewater, the dyna is removed Mix filtration arrangement preferably numerous small nere organic compounds, especially those that are bound in soap micelles. This has the effect of ner reduction of BOD and a lowering of the pH value to the extent that high pH is caused by soap solutions is caused. The dynamic filtration arrangement has preferably also the effect that almost the entire sus  oscillated solids and cola-like faecal germs elimi be kidneyed.

While the concentrate from the dynamic filtration finally arranged in a suitable medium line a suitable concentrate tank, this can also happen Be accomplished after the concentrate for the purpose further concentration is recirculated. Since the dynami filtration process due to higher fluid velocities which tend to be lazy To reduce the speed of the filter medium, it will be prefers that the dynamic filtration arrangement a Re circulating pump has a suction from the outlet end the dynamic filtration arrangement and an output in to make the inlet end of this arrangement. Recirculation ons speeds between one and ten times the Outlet flow rates are preferred, with ho here recirculation flow velocities at Be treatment of heavily contaminated media is particularly preferred are. Two or more dynamic filtration arrangements can be branched in a multiplex system used to switch to a fresh dy Namely filtration unit to be able to make if the other unit is "lazy" (dirty).

The filtrate from the dynamic filtration arrangement can be essentially sanitized water, depending on the exact nature and amount of contaminants in the Wastewater and the special pore size of the dynamic Filtration arrangement. The dynamic filtration arrangement can bacteria, yeast, fungi and the like from the wastewater remove and may reduce endotoxins if not  also remove. While the filtrate from the dynami filtration arrangement is not necessarily one it will need further treatment but preferably further processed to residual microorgan nisms, virus types and organic and inorganic ver reduce ties and preferably even remove them nen. Therefore, the wastewater after it is dynamic Filtration was subjected to a suitable adsorb bed brought into contact with everyone else, possible existing contaminants in the wastewater remove, especially organic and inorganic Pollutants, such as chlorine and metal ions (ins special arsenic, which is on board ships as rats poison is used and its way into the wastewater of the Ship), as well as certain microbial Pollutants, which are the dynamic filtration medium may have happened.

The adsorption bed can have one or more suitable adsorp tion materials, preferably one or more Components from the group: carbon-containing adsorpti onsmittel, active aluminum oxide, silicium dioxide hydrogel, Zeolite and metallic components, which metallic Generate cations. The carbon-containing adsorption with tel can be based on coal, as well as fruit peels, for example coconut shells, wood-based, on acti fourth carbons, which in turn are based on petroleum, synthetic carbon products and mixtures here of. Preferably, the carbonaceous adsorption medium activated carbon. The metallic components, which generate metallic cations, are preferably copper, Zinc, brass, manganese and / or silver and mixtures of this. Brass particles are particularly preferred.  

Because the exact nature of the sewage will be unknown and from Can vary from day to day, the adsorption bed is before preferably a mixed adsorption bed, which is a variety contains adsorbent materials that are capable of treat a variety of possible contaminants. On such a preferred mixed adsorption bed can, for example have the following composition: about 40 to 80% by weight carbon-containing adsorbent, about 5 to 20% by weight active aluminum oxide, about 5 to 20% by weight silicon dioxide hydrogel, about 5 to 20 wt% zeolite and about 0 to 10 wt% metallic components, which metallic cations testify. The adsorption bed particularly includes preferred embodiment activated carbon, active aluminum oxide, silicon dioxide hydrogel, zeolite and / or brass par article. Preferred adsorption beds are for example in U.S. Patent 5,178,768 and U.S. Patent Application Serial No. 08 / 118,998. After the Adsorpti onbed with contaminants is so loaded that its Ability to remove further contaminants, disadvantage lig is influenced, the adsorption bed can be replaced or preferably regenerated and reused. The ad sorption bed can be regenerated in that geeig Nete means are used, for example water of about 93 ° C (200 ° F) according to that in U.S. Patent 5,281,344 described method.

Although the filtrate comes from the dynamic filtration device tion preferably with the help of a suitable medium line straight to the adsorption bed, it can if also via a suitable medium line to one Ozonation system to be conducted before the wastewater is brought into contact with the adsorption bed. The ozo  nization system generates ozone for "polishing" the ge filtered waste water insofar as ozone is capable, Ab to make water sterile and numerous organic ver oxidize bonds as well as microorganisms and viruses to kill who passed the previous filters. Such a hygienic action can usually be done with an ozone concentration of at least about 0.5 mg / l preferably at least about 1 mg / l in the water leads. The ozone has no adverse side effects te and quickly disappears from the treated Water. The ozone can be removed by any suitable means directions are fed.

The ozonization system preferably includes pressure vibration adsorption air dryer, an ozone generator, one Ozone contactor and particularly preferably a UV light source and another ozone contactor. The ozone gene rator can be any suitable device at for example, a conventional apparatus which ozone through Acceleration of electrons between two electrodes produced. The feed to the ozone generator is either filtered dry air or oxygen. An oxygen feed provides more ozone and a higher concentration on. The concentrations usually range from 1 to 8% by weight, 2% by weight for an air feed and 3% by weight are typical for an oxygen feed.

In the case of an air supply, compressed air is supplied by a Pressure swing adsorption air dryer with double bed dries. Together with suitable filters, this delivers Unit air of the required quality through treatment of air, preferably compressed air, which is passed through a pas  send inlet to the pressure swing adsorption air dryer ge reaches. In the event of an oxygen injection, the sow material in compressed air through a cleaning adsorber con centered. One such system is the pressure swing adsorp tion air dryer similar, except details of Adsorbent and the cycle. The use of a Oxygen feed systems require a lot more air and one larger adsorption system, which is why the air feed system is preferred. The pressure swing adsorption air dryer is used to keep the air at a low dew point to clean and dry, e.g. B. a dew point at about -57 ° C (-70 ° F), so the ozone generator filtered, very dry air maintains to last for long periods of time to work without problems and to achieve high ozone concentration testify.

The ozone contactor provides contact time for the reak tion of an organic residue in the filtered wastewater the ozone generated by the ozone generator. Ozone is in the gas phase generated and must ge in the filtered wastewater be solved. There are numerous methods of transfer and available for contact to resolve the To reach ozone in wastewater. For example, that Using ozone in the form of bubbles through a column of waste water or passed through without packing material. The Ozone can also be injected into the sewage pipe will. The transfer of the ozone into the waste water leaves by using a scarf in the pipe improved motionless mixer.

The wastewater treatment system preferably also closes a second ozone contactor with a UV light source  on. Ultraviolet light, especially with a wave length of 254 nm, produces Hy in the ozonized water droxyl radicals, which interact with the ozone and which oxidize most organic compounds. The second Ozone contactor with UV light source ensures that each de desirable or necessary oxidation by ozone in the Ab water is completed.

Residual ozone can cause natural decomposition to sow material because its half-life in what water at 21 ° C (70 ° F) is about 20 minutes. The decomposition The heating of the ozone can be accelerated. An alternative method, which benefits other than the above has discussed is the use of radiation with UV light. An adsorption bed can also be used for this to remove ozone, especially because the surface surface of the adsorption bed a place to decompose the Can deliver ozone. Therefore, as far as the wastewater takes place Such ozone is brought into contact before preferably before contacting the wastewater with the ad sorption bed instead. An ozone analyzer can be used for this be the treated wastewater or the discharged Gas to analyze the complete removal of the gas Check ozone from the water. The treated waste water It is then removed from the treatment system via a suitable outlet discharged as a purified water stream.

A concentrate tank can be designed to do that concentrate obtained during the treatment process for removal at a later, appropriate time has ready. For example, with regard to on board the concentrate of a ship's gray water  be pumped out of the ship when it is in the dock and on Appropriate facilities are available on shore, or if Boats are available for pumping, or at sea outside of water with corresponding restrictions.

The treated wastewater can continue in an appropriate manner treated, recirculated and / or drained. The Treatment system is preferably constructed so that Gray water is cleaned to an extent that an Ablas in waters that are otherwise restricted subject to.

The effectiveness of the treatment system is such that it no larger dimensions than about 6 m (20 ft) in the Length, about 3 m (10 ft) in width and about 3 m (10 ft) in height and is still able to up to about 19 l (5 gallons) of greywater per minute on board one Treat the ship with minimal maintenance.

Any suitable device can be used Practice the method of the present invention. In all generally includes such a device for the treatment of Waste water containing particulate matter and free oil (a) means to remove the free oil the waste water, (b) means for passing the waste water through after removing the free oil to a first filter medium, (c) a first filter medium with an effective Pore size of about 200 microns or less, (d) means for Transfer of wastewater after passage through the first filter medium for a dynamic filtration direction, (e) a dynamic filtration arrangement with egg nem second filter medium, which has an effective pore size  of about 5 µm or less, (f) transfer means of waste water after passing through the second filter medium to an adsorption bed and (g) an adsorption bed.

The device preferably further comprises a sieve, through which the wastewater before it passes through the first filter medium is passed through. Such a sieve is preferably a mesh screen as related above described with the inventive method. The first Filter medium preferably has an effective pore size of about 160 µm or less. The means of removal free Oils preferably comprise contacting devices of the waste water with a material that absorbs free oil beers, for example cotton, especially terry cloth fe.

As explained in detail in connection with the method according to the invention, the dynamic Filtrationsanord voltage is preferably capable of generating shear forces of at least about 20,000 sec ^-1 , preferably of at least about 100,000 sec ^-1 . The dynamic Filtrationsan arrangement is in the preferred embodiment, a dynamic vibration filtration device. The second filter medium preferably has a molecular weight limit of about 200 daltons or less, and in particular a reverse osmosis membrane capable of salt rejection of at least 97%.

As also in detail above with reference to the explained method according to the invention, the adsorpti any suitable adsorbent materials  hold, remove the contaminants, which may se could penetrate the dynamic filter medium. The Adsorption bed preferably includes carbonaceous Adsorbent (especially activated carbon), active aluminum minium oxide, silicon dioxide hydrogel, zeolite and metalli components that generate metallic ions (at for example copper, zinc, brass, manganese, silver and silver of these, especially brass particles).

The device can also be an ozone contactor grasp the waste water before contact with the adsorpti to bring in contact with the adsorption bed can be used to remove residual ozone and / or to facilitate its decomposition as well as any To remove reaction products. The device can fer a radiation source for ultraviolet light close to the ozonized wastewater radiation subject to ultraviolet light, preferably before the wastewater comes into contact with the adsorption bed.

In most use cases, as also above in connection with the inventive method wrote, the device still has a retention tank, which allows high density material, which from Wastewater is carried, settles on the tank bottom, before the waste water is passed through the sieve. The before direction can also be means for reducing the particles Include size in the wastewater before passing through it ste filter medium is passed. The device comprises normally also suitable valves for controlling the Wastewater stream, a concentrate tank for temporary storage  Protection of concentrate, degassing equipment, at for example a carbon degassing filter for Deodori the gases from the waste water retention tank and be drained from the concentrate tank, as well as further in directions as they are in the relevant technology itself are known.

Examples

The following examples serve to explain further tion of the invention, in particular the use of a dy Named filtration in the treatment of fluids. These Of course, the invention is in no way intended to provide examples restrict.

example 1

Two barrels containing approximately 210 liters (55 gallons) of gray water were made from the David Taylor Research Center and nearby Naval Academy related. The gray water came as far as he was obviously, about 45% from shower and sink, 33% from Cooking and washing-up kitchens and 22% from the laundry. The Exam was completed within 72 hours of receiving the Trial completed. The sample closed as received obviously no large particles. Approximately 210 liters (55 gallons) of greywater was passed through a sieve made of stainless steel passed through with the dimensions 24 × 24 × 0.014 (wires per linear inch × wires per li near inch × wire diameter in inches; what about 9 wires per linear centimeter in both directions and one wire  corresponds to a diameter of approximately 356 µm). A household Garbage shredder was used to resize which large particles to further reduce. About 57 l (about 15 gallons) of the sieved water was filtered, with a dynamic microfilter BDF-LAB from Pall Corporation was used. The filter element was a balanced Zy linder - Pall S050-3 PSS class H, series S made of porous stainless steel with an absolute pore size of 5 µm.

Half of the outlet stream was concentrate and half the outlet stream was filtrate. The filter was started using clear water to the operating parameters ter to set. The inlet was then switched to gray water switched and the operating parameters were reasonable set in a way. The flow velocities were kept constant during the experiment, the Be driving pressure increased slightly in the course of the experiment was gert. Although the filter only works during a short zen time was tested, it was obvious that he did not become contaminated ("became lazy") as quickly as a Normal filter. Obviously the cloudiness was in the filtrate noticeably less than that in the inflowing medium, while the turbidity of the concentrate is higher than that of the inflowing medium. The penetration currents speeds and ring pressures at 10 and 30 minutes The test was as follows:

About 8 liters (2 gallons) of the filtrate was removed during 200 mi grooves ozonized. The ozonizer used has required a recirculation loop of approximately 9.1 m (30 feet) Copper pipe. An ozone generator, the Clean Air Corporation, with a delivery capacity of ozone of approx. 30 l / h (8 g / h) was used to deliver ozone. An aspirator served to introduce ozone. A turbulence of around 180 to 240 cm / min (8 ft / min) mediated the contact and the mixing of the ozonized air with the water.

The characteristics of the gray water in the different treatments Levels are listed below:

Although total suspended solids (TSS) after Filtration were not measured, it is believed that dynamic filtration for effecting reduction TSS was solely responsible from 26 mg / l to 6 mg / l. Of the BOD increase from filtered water through ozonization was probably the result of Ozoni's conversion sation of non-biodegradable material in bio logically decomposable material. After 200 minutes of ozonization The water remained frothy, which indicated that Be had not left. The pH remained through the dynamic filtration and ozonization unaffected.

From the test it was clear that ozone is reducing of the COD of gray water was effective. Although only one a small amount of ozone was applied, a noticeable reduction in COD. Ozone was concentrated tration of 72 ppm added over 20 minutes. While at that time samples were taken from the reservoir where by reducing the total volume of gray water and the concentration of ozone in each new period rise. At the end of the experiment, the concentration would be of the ozone was 43 mg / l if none during the reaction Ozone would have been consumed. If all ozone applied would have reacted with COD connections, the COD would be over 43 mg / l was reduced. The COD level was, however, by 490 mg / l decreased to 360 mg / l, a decrease of Corresponds to 130 mg / l. This drop is three times greater than the reduction in COD, which is the effect of ozone al could be attributed to.

The ozone was released into the water by an air stream carry. There was almost three times as much oxygen in the air  like containing ozone. The oxygen would be in the oxidation of these compounds, which are easily oxidized, been effective, and the air flowing through the water could peel off volatile organic compounds. This Mechanism could increase the effectiveness of the Ozonization process will be charged.

Although ozone in the reduction of COD and a lot BOD also proved to be effective, it is clear that a significant amount of ozone would be required to COD and BOD to reduce to acceptable levels after only dynamic filtration using a filter meter diums with a pore size of 5 microns took place. Although the this experiment the feasibility of a dynamic Filtra tion and ozonization in the treatment of gray water demonstrated, this attempt also showed the desirable dynamic filtration using a Filter medium with a pore size smaller than about 5 µm.

Example 2

A barrel with approximately 210 liters (55 gallons) of gray water was removed from the David Taylor Research Center related and with a range filtered by filters that ge by decreasing pore size were marked. The first filter was a knitted one Mesh screen, which should simulate a common screen. The second, third and fourth filters simulated the Filtration through the dynamic filtration arrangement. The the second filter was an absolute filter with a pore size of 3 µm Ultipor GF (Ultipor is a registered product Pall Corporation; the third filter was  a hygienic filter with a nylon membrane and a Pore size of 0.04 μm from Pall Corporation; the fourth filter was an ultrafilter (registered goods model) Model VIP-3017 (Asahi) with a limit molecule Lar weight of 6000 daltons.

The fourth filter was absolutely deionized with 3 µm Rinsed water for about 20 hours and then before Test attempt emptied. The barrel of the gray water was opened about 34 kPa (5 psig) pressurized with air, causing the gray water with a flow rate of we less than about 1.9 l / m (0.5 gallons per meter) through the Filter was pushed through. The Concentrate Flow Ge speed from the fourth filter was approximately a quarter of the flow rate of the filtrate (ge purified water). Samples of the filtrate were collected on three and taken from different places in the test system: (i) after the first filter, (ii) after the second and third Filter and (iii) after the fourth filter. The filtrate was able to take 30 seconds from the first two sampling taps flow out long before the samples are taken. The fourth filter was treated with treatment me for 10 minutes dium flushed before the samples were collected.

The filtration system improved the clarity of the gray water in a defined way. Smell and foaming of the Greywater was also reduced. The flow ge speed gradually decreased in the course of the experiment, while maintaining constant pressure in the barrel de. An examination of the system indicated that either the second or third filter or both of them clogging up started. The use of a real dynamic Filtra  tion arrangement rules out such constipation. The Examination of the concentrate in the housing of the second fil ters revealed that it was much darker than the original Greywater medium was. The test results are next listed below:

The test results indicate that the combination of the different filters the requirements regarding suspen dated total solids and cola-like faecal germs len, while the addition of an acid feed is required can become necessary to the strongly alkaline state correct. The upstream use of a Koagu liermittel would the filtration effect, as it through the dynamic filtration is achieved, improve. The Ver Search results also indicate that ozone and a Irradiation with UV light to further reduce the BOD Levels would be useful.  

Example 3

Two barrels containing approximately 210 liters (55 gallons) of gray water were made from the U.S. Naval Academy in Annapolis, Maryland, bezo Each gray water barrel contained approximately 102 liters (27 gallons) Laundry water, about 68 liters (18 gallons) of kitchen water and about 19 liters (5 gallons) of shower water.

The greywater was drained using a barrel pump a sieve with the dimensions 30 × 30 × 0.0065 (wires / Li near inches × wires / linear inches × wire diameter in inches; about 12 wires per linear centimeter in both directions with a wire diameter of about 165 µm) in buckets pumps to remove coarse waste. The distant Ab waste consisted of hair, thick, tough material, Flakes and other soft media. The floor area of each Gray water barrel contained up to a height of about 5 to 8 cm (2 to 3 inches) a thick, black oily substance.

The gray water was then removed from the tubs by a Metal sieve filter cast with a pore size of 160 microns. The gray water filtered in this way was opaque tig, ink black and contained no traces of soap or Soap solutions. From the freshly poured gray water emanated a strong, pungent smell, but it was internal subsided in half a few hours.

The gray water then became a dynamic fil tration using a dynamic vibration fil arrangement PALL-SEP VMF series L of the Pall Corpora tion subjected, with either a Na nofiltration membrane with a molecular weight limit of  200 (with an 80% minimal salt repellent classification tion) or a reverse osmosis membrane with 97% salt content white classification was used. The operating relationship The dynamic filtration arrangement was as follows:

When using the nanofiltration membrane during 300 l (80 gallons) over a three week period Greywater treated. At the end of this period 99.31% of the medium from the system as a transit medium away. The total accumulated transit medium, namely 287.53 L (75.91 gallons) showed a loss of 13.3 l (3.52 gallons) of greywater. The loss at Greywater became the evaporation of volatile organi connections attributed to that in a noticeable way occurred, and the exit of water vapor. The total recorded amounts of gray water were reduced by 4.4%, to account for the loss of evaporation. At the fort  the percentage ratio of through medium / The total gray water dropped to 99.31% speed of the through medium from about 73 ml / min to about From 47 ml / min. When using the reverse osmosis membrane which treated about 72 l of gray water, whereby one Recovery of through medium of about 68 l or about 94.31% resulted. While the percentage ratio of Through medium / treated total gray water of about 89% the flow rate fell to about 94% of the through medium from about 24.4 ml / min to about 21.3 ml / min. The characteristics of the gray water before and after the next step is to carry out the dynamic filtration indicated:

The passage obtained from the nanofiltration membrane medium (permeate) had a mild, pungent smell and a very light yellow hue. That from the Reverse The passage medium obtained from mose membrane was crystal clear and didn't emit any smell. Both through media conformed to the US requirements for an open drain water; that obtained from the reverse osmosis membrane The transmission medium was generally contaminated more freely than that obtained from the nanofiltration membrane Transit medium. The ge of the nanofiltration membrane won through medium would preferably be in the way treated further that the permeate with a suitable Adsorbent bed contacted to match to ensure the applicable indulgences. The through medium obtained from the reverse osmosis membrane would possibly not receive such further treatment require.

Claims (24)

1. A method for treating waste water containing particulate matter and free oil, characterized in that the free oil is removed from the waste water, the waste water is passed through a first filter medium with an effective pore size of about 200 microns or less, the Subjects wastewater to dynamic filtration using a second filter medium with an effective pore size of about 5 µm or less, and finally contacts the wastewater with an adsorption bed and forms a cleaned wastewater stream. 2. The method according to claim 1, characterized in that the waste water before it is led through it filter medium is passed through a sieve. 3. The method according to claim 2, characterized in that the sieve is a mesh sieve with about 4 to 20 wires per linear cm in each direction and a wire diameter is from about 50 to 500 microns. 4. The method according to any one of claims 1 to 3, characterized characterized in that the first filter medium is effective same pore size of about 160 microns or less.   5. The method according to any one of claims 1 to 4, characterized characterized in that free oil from the waste water thereby that the wastewater is removed with a free oil absorbent material is brought into contact. 6. The method according to any one of claims 1 to 5, characterized characterized in that the dynamic filtration a dy Namely vibration filtration is. 7. The method according to any one of claims 1 to 6, characterized characterized in that the second filter medium is a mole Ocular limit weight of about 200 daltons or less Has. 8. The method according to claim 7, characterized in that the second filter medium with a reverse osmosis membrane is capable of at least 97% salt repellency. 9. The method according to any one of claims 1 to 8, characterized characterized in that the adsorption bed one or more other components of the material group below summarizes: carbon-containing adsorbent, active Aluminum oxide, silicon dioxide hydrogel, zeolite and me metallic components, which metallic cations produce.   10. The method according to any one of claims 1 to 9, characterized characterized that the wastewater before it passed through line through the screen into a retention tank becomes. 11. The method according to any one of claims 1 to 10, characterized characterized that the wastewater before it passed through line through the first filter medium of an action which is the size of the particles in the Ab water reduced. 12. The method according to any one of claims 1 to 11, characterized characterized in that the wastewater was incurred on ships is gray water. 13. The method according to any one of claims 1 to 12, characterized characterized in that the waste water at least about 150 mg / l total solids, at least about 100 mg / l total suspended solids, at least about 100 mg / l of BOD, at least about 200 mg / l of COD, at least about 15 mg / l oils and fats, coli-like Faecal germs and residual chlorine and / or less than about Contains 5 mg / l dissolved oxygen. 14. The method according to any one of claims 1 to 13, characterized characterized in that the purified water flow less than about 150 mg / l total solids, less than about 100 mg / l total suspended solids, less than  about 100 mg / l of BOD, less than about 200 mg / l COD, less than about 15 mg / l oils and fats, less than about 14 cola-like faecal germs per 100 mg / l, weni less than about 0.0002 mg / l residual chlorine and at least about Contains 5 mg / l dissolved oxygen. 15. Device for carrying out the method according to one of the preceding claims, characterized by the following features:

• a) means for removing free oil from the waste water;
• b) means for introducing the waste water after the removal of the free oil into a first filter medium;
• c) a first filter medium with an effective pore size of about 200 microns or less;
• d) means for introducing the waste water after passing through the first filter medium into a dynamic filtration apparatus;
• e) a dynamic filtration arrangement with a second filter medium which has an effective pore size of approximately 5 μm or less;
• f) means for introducing the wastewater after passing through the second filter medium into an adsorption bed; and
• g) an adsorption bed.

16. The apparatus according to claim 15, characterized in that it further comprises a sieve through which the Waste water before it passes through the first filter medium is passed through, the sieve a Ma  sieve is with about 4 to 20 wires per linear cm in each direction and with a wire diameter from about 50 to 500 µm. 17. The apparatus of claim 15 or 16, characterized records that the first filter medium an effective Po ren size of about 160 microns or less. 18. Device according to one of claims 15 to 17, there characterized in that the means for removal of free oil means for contacting the waste water with a material that absorbs free oil beer. 19. Device according to one of claims 15 to 18, there characterized in that the dynamic filtration arrangement a dynamic vibration filtration arrangement is. 20. Device according to one of claims 15 to 19, there characterized in that the second filter medium Molecular weight limit of about 200 daltons or less ger has.   21. The apparatus according to claim 20, characterized in that the second filter medium is a reverse osmosis membrane which leads to an at least 97% salt repellency is empowered. 22. Device according to one of claims 15 to 21, there characterized in that the adsorption bed a or several parts of the list below includes: activated carbon adsorbent Aluminum oxide, silicon dioxide hydrogel, zeolite and me metallic components, which metallic cations produce. 23. Device according to one of claims 15 to 22, there characterized in that they continue to have an ozone con clock for contacting the wastewater with ozone its contact with the adsorption bed and an ul traviolet radiation source includes for submission the ozonized wastewater from an irradiation with ul traviolet light. 24. Device according to one of claims 15 to 23, there characterized in that they continue to hold back tetank, which is a settling of materials high density carried in the wastewater the bottom of the tank before the waste water passes through the sieve enables, as well as a means of reduction the particle size in the waste water before passing through of the waste water through the first filter medium.