FI125584B

FI125584B - A method for providing fluid circulation in membrane filtration and membrane filtration apparatus

Info

Publication number: FI125584B
Application number: FI20110261A
Authority: FI
Inventors: Esko Aulanko
Original assignee: Emp Innovations Oy
Priority date: 2011-06-21
Filing date: 2011-08-09
Publication date: 2015-12-15
Also published as: EP2723477A4; EP2723477A1; FI20110205A0; FI20110261L; FI20110205A; FI125583B; WO2012175804A1

Description

METHOD FOR LIQUID AND CYCLES: THE ORGANISATION membrane filtration membrane filtration plant

The invention relates to a membrane filtration, in particular, the invention relates to a method and the manner in which the membrane filtration is supplied and the membrane filtering device and the environment kalvosuodatukses-in facilities used. One object of the invention is not teisosmoosisuodatus-or käänteissuodatuserotus.

Membrane filters are used extensively in industry and otherwise as water treatment than for other purposes. Membrane technology is also evolving area with the emergence of new technologies and opportunities for a variety of applications and uses.

The membrane filter, which can also be called Membrane, simplifying operations can be described as follows: To be used with certain characteristics-permeable membrane is permeable permeate, for example water, and the reserves of other substances. In practice, through membrane separation is not complete, resulting in the difference between the film has passed the permeate and the concentrate obtained from filtered material or the like. Often, the permeate is for output, for example, purifying water, but the film separation can be used for the concentration of the objective substance, for example, for recovering the process chemicals or concentration of the solutions.

Commonly used liquids membrane filtration method is the so-called cross-flow (cross-flow filtering). Cross-flow filtration is used in many different types of membrane filtration methods, such as reverse osmosis, nano-ultrafiltration and microfiltration. Cross-flow filtration is known in the art, for example, the publication W0 2006020780 A2. Cleaned by crossflow filtration material is caused to flow parallel to the filter membrane surface, whereby, even if part of the substance to drain through the membrane, the substance flushed clean the membrane surface and thereby keep the permeable membrane by preventing clogging or high local Concentrate the film surface. User-force membrane filtering is probably more than the differential pressure value. Not only to overcome the resistance due to the membrane, the energy required for the various stages of the process for moving and steering fluids, as well as to raise the pressure of the fluid to the required working pressure.

Kalvosuotatinlaitteita and the components thereof are commonly available for different purposes. Membrane plants and equipment built from commercially available components and based on the generally known techniques. For example, the reverse osmosis filter is commercially available in a variety of applications, and suitably also to deal with different solutions and differentiation of a variety of materials, including salt removal filters may be optimized and also can be selected with regard to the salt content of the water being treated. Previously known from US 7695614 B2 and W0 02,055,182 Al poikittaisvirtauksellinen membrane filtration of fluid circulating solutions with closed circuit fed back to the flow is driven by a separate recycling pump, which is a main propulsion membrane module OCCURS poi the axial-flow and the pressure of the membranes through the flow required is produced by the high pressure pump, through which is also replaced leaving the rounds of the amount of liquid.

The purpose of this invention is to develop a membrane filtration and to provide a low-cost, reliable, safe and very effective solutions for membrane filtration. In particular, the invention aims at reverse osmosis, nano-, ultra- and mikrosuodatusrat-solutions, especially solutions which are suitable for use in aqueous solutions käänteisosmoosiväkevöinnissä or purification.

The invention is characterized is featured in the claims, which also is featured advantageous invention entrusted manifestations.

Preferably, the present invention shows a method for arranging the liquid circulation membrane filtering. In a preferred form-pressure source, such as a pressurized container, pump-pressure network or is derived from the pressure fluid-flow filter membrane and the filter membrane impermeable to fluid flow at least part of the compound in the fluid-pressure-source fluid flow. The preferred solution is to combine a filter membrane impermeable to fluid flow in the fully-pressure fluid source to the fluid flow. Such a procedure concentrated liquid is returned to be filtered again. The advantage obtained by the procedure in two ways, firstly, the yield can be improved, and, secondly, the forthcoming re-filtering the liquid is pre-pressure, thus raising the pressure has not incurred a cost in that regard. Preferably, the filter membrane may be permeable to both liquid flow and the filter membrane impermeable to liquid flow maintains liquid-pressure source coming fluid flow. Shaping and sizing the flow of liquid feed and fluid circulation suitably achieved a very low energy consumption, maintenance of fluid flow. Furthermore, the apparatus is simple. The invention is an energy-efficient feasible both large and small institutions without the need for a pressure exchanger or similar energy recovery devices. The invention is also attainable relatively high yields, which is of importance, for example in water purification, wherein the pre-treatment and / or the raw water has a significant proportion of total costs.

From time to time, it is preferred to rinse the filter membrane pressure more than half the cross flow flushes itself. This can be done by replacing the concentrated fluid pressure source available from the less concentrated in the liquid. At the same time, if the pressure is sufficient, a membrane over the low counter pressure - the reverse osmosis membrane, in the case of the osmotic pressure, - a fine-grained film is easily rinsed.

The invention also shows as alternative embodiments, in which the filter membrane impermeable to fluid flow pressure is controlled to count down from time to time so that the filter membrane permeated liquid stream flow direction is reversed. As such a back-flushista as the cross flow rinsing or otherwise, can the concentrate may have crusts or other distinctive impurity that should be filtered out. It is preferred to add a filter or other suitable device, such as a cyclone separator to separate the precipitate.

In some embodiments of the invention-pressure amount of nestelähtees-in liquid flow or pressure or both, or any of these change is controlled cyclically and / or at least one of the following reasons: a pressure filter membrane impermeable fluid flow, the magnitude of the filter membrane permeable liquid flow, the magnitude of the filter membrane permeable liquid flow, the concentration of one or more agents filter -permeable membrane in the liquid flow, the concentration of one or more filter membrane permeable substance in the liquid flow.

Based on the set control criterion filter membrane impermeable to fluid circulation flow of fluid at least partially replaced by the fluid-pressure source of fluid. The control criterion may be linked to the control of the volume or pressure of fluid flow or change of either, or it may be separate from these.

One manifestation of the invention is a membrane filtration equipment. In a preferred invention implements the membrane filter apparatus has at least one filter membrane, on opposite sides of the filtering film of first liquid chamber and the second nes-tetila, the filtering film arranged over the pressure differential, the first fluid space of said filter membrane directional liquid flow through the filter sheet in a first liquid state to the second fluid space pressure difference due to the fluid flow and a fluid supply to the first fluid space-pressure fluid source and the flow path, at least a portion of said filtering film direction for conducting fluid flow together with a liquid-pressure source to the liquid flow. Filter Film penetrating the filter membrane bypassing the liquid flow can lead to a whole-pressure fluid source liquid stream-taukseen merge. Particularly preferred is the solution of equipment, which both filter membrane permeable to fluid flow passing the filter membrane is arranged on the liquid flow-pressure fluid source to the fluid flow.

The preferred membrane filter device fluid flow to action of the liquid-pressure source to the liquid flow in the flow channel is structured to be formatted, for example, kar conical or funnel-shaped nozzle. A conical or funnel-shaped nozzle spray port is typically circular. The flow channel can also be shaped to optimize the efficiency. A nozzle to supply fluid to the desired direction of the supplied liquid and the rapid flow also provides the flow channel for the liquid to move.

Preferably, the flow passage for supplying the liquid nozzle being configured by its shape bit influencing the flow, wherein the nozzle effect flow is substantially supplied by the liquid flow created by the.

One aspect of the invention is to connect a flow membrane filtration of the liquid circuit from a nozzle placed in fluid-cycle use of the same source, and also the use of the nozzle to bring the membrane filtering to filter liquid and, possibly, otherwise leaving the amount of fluid replacement. The requirement then is sufficiently high flow rate and, correspondingly, a smaller nozzle outlet opening.

Within the scope of the invention other than a circular nozzle opening is possible and even preferred. For example, the slot-like nozzle opening of the nozzle to shorten the flow to the flow channel engage package holidays flow and allows at least some cases, the shorter the flow channel.

The slot-shaped nozzle is easy to make a flow passage extending pipe, which is on the side of the direction of flow Illustrative gap. Such a tube may be flattened or shaped making up the flow resistance is particularly small. Give the direction of flow of the slit does not necessarily have to be straight, it is possible to make the actual flow channel by fitting the new liquid in the supplying pipe section, for example, an annular die gap, preferably coaxially. In such a solution, optionally partially laminar flow in the flow channel tube around the edges of the annular nozzle face the flow passage a turbulent flow, mixing is effective and takes place in a very short distance.

The present invention can conveniently be performed by commercially available components and simple mounting techniques water treatment suitable membrane filter device comprising the membrane filter unit in which the input interface of the aqueous solution to derive the membrane filter unit, the first outlet connection of the permeate passing the membrane filter unit and the second outlet connection for conducting concentrate the membrane filter unit and in which the membrane filter device comprises a si-inlet join the leading flow channel to which a second outlet connection is derived, and the flow channel has a second out-of roundabouts per input interface for maintaining the flow of the actuator, for example a pump, propeller or nozzle; a flow channel for supplying high pressure water to be treated the flow channel is suitable nozzle. A preferred device solution is one in which the water to be treated flow channel supplying the nozzle is directed to feed water to be treated from the input interface. Membrane filtration device preferred embodiment is one in which one or more of the flow duct supplying nozzle is a single exclusive channel of the second flow-out of the user interface towards the direction of flow input interface for the operating means.

The invention is particularly advantageous for water treatment applications, for example, desalination, process, boiler, or water-making facility, irrigation or drinking water, and even the production of waste water treatment. The invention is also applicable for enrichment of solutes, for example, the food industry or the mining industry.

In the invention, a solution-impermeable membrane filter is recycled back to the essential samanpaineisena filter membrane. In practice, this recycling is some pressure loss, but these pressure drops are relatively small compared to the pressure difference required for membrane filtration itself. Especially käänteisosmoosisuodatuksessa pressure differential across the membrane is significant.

The invention is preferably applied to the commonly used poikittaisvirtaussuodatusperiaatteeseen. The invention has a number of forms, which are not completely coincide with each other, for example, implementing the method of the invention is not very dependent on the destination device and an apparatus for implementing the invention includes at least, or may contain elements that are not essential for carrying out the method. Manifestations and implementation methods of the invention may differ from each other.

In aspects of the invention to a characteristic of the solution is recycled to the membrane-impermeable film over substantially the filtering membrane työpaineisena. Another aspect of the invention is characterized by a fluid passage arranged, wherein the film ohivirrannutta impermeable membrane solution was transferred to a film uudelleensuodatettavaksi. In practice, kalvosuo-cross flow filter and associated vir passage is a certain pressure loss, which, however, is small compared to the film working pressure, especially when it comes to the reverse osmosis membrane. Despite this pressure drop, the impermeable film can be regarded as side pressure of the pressure losses substantially constant.

An important aspect of the invention is to apply a membrane filtration, particularly reverse osmosis membrane filtration or cal-voerotusta, purification or suolanerotukseen water.

Cross-flow filtration is used in many different types of membrane filtration methods, such as reverse osmosis, nano-, ultra- and microfiltration. In the invention, the cross flow filtering applied so that the concentrate will be returned back to be fed under pressure again and the filtering circuit is fed at the same time pressurized more than the same amount of material is removed as permeate.

The invention may also occur otherwise than as defined in the claims. In addition to manifestations defined by the claims of the invention other forms of the invention described or shown above and below.

The invention is also suitable liquids for enrichment, wherein instead of the quality or quantity of permeate or other factors of production of the permeate should be primarily kalvoero would determine the certificate in the device or process optimization, process control equipment and adapted to the best quality and production of the concentrate. For example, to seek adequate solutions to liqueur or just a certain fairly accurate set-liuosväke envisaged. It is also possible to optimize the process costs in relation to the yield.

The primary use of the invention, thought to have its application käänteisosmoosierottelussa. Many phenomena or technical solutions are in other membrane separation techniques very similar kind. Within the scope of applicability of the inventive solutions can, therefore, be extended for use in other kalvoerotusme-proce- dures, even though the description and reasoning of technical solutions vices laid out in this context, most reverse osmosis device environment.

The following is a brief justify and to understand the reverse osmosis phenomenon and related to the application of the invention, the calculation of the application of the invention, as well as optimization of functions of the invention.

The performance information is used in the following. Entities which have been reported in square brackets, use can vary, for example, may indicate% as% of or more broadly proportionate share.

p = process pressure [Pa] [bar]

Posm = osmotic pressure [Pa] [bar]

Pmioss = membrane element pressure drop [Pa] [bar]

Ppioss = pipe pressure loss [Pa] [bar] k = membrane permeability factor [m3 / (s Pa)] (depending on the transmembrane-toxin and is strongly temperature-dependent)

Q p = permeate volume flow rate [m3 / s]

Q f = feed flow volume flow [m3 / s]

Qc = concentrate volume flow [m3 / s]

Qi = the system to enter the volume flow [m3 / s] cin = raw water salt concentration [%]

Cmin = ingoing concentration of the membrane [%]

Cmout = membrane element driven coming out of the concentric io [%] cm = average concentration of the membrane element [%] cc = concentrate the salt concentration [%]

Rs = system recovery ratio (= yield) as a [%]

Rm = the membrane element recovery ratio [%]

Pro = reverse osmosis consumed by the power [W]

Pmioss = membrane element power loss [W]

Difference = reverse osmosis required specific energy [J / m3]

Ef = feed flown specific energy [J / m3]

Es = specific energy of the entire system [J / m3] ηΗΡΡ = high pump efficiency (motors) F | cp = feed flown recirculation pump efficiency motors Reverse Osmosis by the equation:

(1)

In order to reverse osmosis to occur, the pressure (operating pressure) must be greater than the osmotic pressure, otherwise, the flow reverses direction and becomes osmosis.

Formula (1) can be solved the necessary working pressure (ajopai-ne)

(2)

For example, saline pOSm = approx. 8 bar / cin%, or 1% saline solution Posm = approx. 8 bar and 3.5% saline sea water Posm = approx. 28 bar (approximate value).

It should be noted that the concentration of the membrane element increases from one end to, and the concentration was just on the surface of the film is greater than the average concentration of the solution flowing through. Turbulent feed flown task is to rinse the surface of the film as effectively as possible.

The average concentration of the membrane element is:

(3)

That is, the required minimum pressure is formed through that. In order for the flow would be positive, it is at that minimum pressure must be sufficient margin. Maksimiajopaine is determined by the maximum allowable membraaniele-ment through permeaattiflown. Maximum pressure can also be said through the membrane element determined allowable maximum pressure.

Reverse osmosis The power required = pressure * volume flow rate:

Cyclic solution, which the invention is particularly suitable for closed feed flow circulation - that is a kind of concentrate feedback again to be filtered together with the new feed, pressurized fluid only permeate flow rate (Qf = Q p).

It follows:

(4) reverse osmosis required specific energy:

(5)

That is, the minimum energy of reverse osmosis is a pressure as low as possible (the absolute minimum when p = pOSm).

Because the rate of return is, however, directly proportional to the osmotic pressure of border pressure and the permeate quality improves with increasing pressure, it is the energy dimensioning is always a compromise quality and energy costs, equipment costs, in terms of permeate.

In addition to reverse osmosis In fact, the current energy system, energy is required to permeate, concentrate and fed propelling solution and overcome the losses.

The cycle-specific pressure increasing

The required feed flow:

(6) This opposes membrane and piping losses.

The required power

(7)

The specific energy flown Feed

(8)

Given the pumps efficiencies into account, the whole system will be specific to energy:

The energy of the formula (9) is the instantaneous energy. The concentration of closed-loop recycled to grow over the cycle, in which case either the pressure increases or decreases permeaattiflow over the cycle. While keeping one of the constant changes to the other linear. The average specific energy of the system is obtained by using the calculated formula (9) is the average pressure over the cycle (when driving a constant current through) or the average flow (when driving at constant pressure).

(10)

If both of the change is integrated with the average energy point by point.

The membrane filter unit used in the invention perustoimintape-principle is known per se and the filter membranes, as well as the membrane filter units are commercially available in multiple different. Filter Membranes and membrane filter units are commercially available for multiple uses and conditions.

One aspect of the invention is to provide a two or more-cal vosuodatusaste row. The filter in each stage may be cyclic or batch process or a continuous process. There is a practical appropriate solutions are those which, after the cyclic filtration stage followed by either cyclic or continuous filtration degree of filtration. Successive grant-added production arrangements need not be identical, and filters used in them can be a recurrence with the other's different. Preferred solutions are those wherein at least the last filtration rate is based on a continuous process. The invention is also applicable to the multi-stage filtering apparatus is one or more of the prior filtration step according to prior art and one or more operating in accordance with the invention, the filtering step.

The invention is described in more detail for one of embodiments with reference to the accompanying simplified drawings, in which Figure 1 shows a simplified diagram of the invention i.e. to be served by the apparatus, Figure 2 shows an invention, the use application, Figure 3a shows schematically an invention applied laws apparatus, Figure 3b shows a modification of Figure 3a apparatus, Figure 4a and Figure 4b show a second invention, the use application, and Figure 5a shows a two-stage applying the invention solution, Figure 5b shows another two-stage applying the invention solution, Figure 5c shows yet another two-stage applying the invention solution, Figure 5d shows a further two-stage applying the invention solution, Figure 6a shows In yet another preferred fluid circulation using a nozzle flow channel rakenneperiaatteeksi-van side view and Figure 6b shows the solution of Figure 6a seen from the end of the flow channel.

In Figure 1 is schematically shown in a simplified system applying the invention. Water treatment device 101 is a membrane filter unit 1 putkistoliittymineen and the flow channel 105, which relates to purified, supplying water under pressure to the nozzle 2. The membrane filtration unit 1 is virtually pressure-proof vessel, inside which is arranged a filter membrane, for example käänteisosmoosisuodatinkalvo.

The membrane filter unit 1 has an input interface 102 aqueous solution for conducting membrane filter unit 1, the first off-the user interface 103 of the permeate passing the membrane filter unit 1 and the second outlet connection to conduct 104 concentrate of the membrane filter unit 1. Interfaces 102.103 and 104 can be thought of the membrane filter unit as being yhteiksi, which join the pipes or connections 102.103 and 104 can also be considered to comprise pipes which join the other ve denkäsittelylaitteiston parts. Water treatment device 101 to join the inlet 102 leading into the flow channel is connected to a water processing device 101, the second outlet connection, the concentrate can be recirculated. Chicken-flow Vassa 105 is a nozzle 2 for supplying new water to be treated flow channel. The nozzle 2 to enter new water to be treated fairly high speed input interface 102 a. The nozzle fed by the amount of water volume flow is the same as filtered through the membrane and ultimately leaves the first outlet junction 103. This rapid flow nozzle arranged on the surface of the cross flow membrane. At the same time the nozzle to convey the liquid film conducting state of the membrane filtration operation necessary pressure. One jet in many cases will be implemented, for example, but not very large systems with a plurality of interconnected cal-vosuodatinyksikköjä, it may be advantageous to use several nozzles as a source of the flow channel, or possibly even more of the flow channels of the flow.

Such water treatment device operation is the easiest to make a cyclic so that the equipment is filtered and alternately shifts the concentrated concentrate is removed. The membrane filter unit 1 or the second branched exhaust junction 104 is huuhteluliittymä 106, 106 ', with a valve 107, 107', via which the concentrated removed from the concentrate.

Figure 2 is an example of use of application. Figure 2, like, for example, the system is suitable for the production of an apartment or a holiday home in water or other small-scale vedenpuh-polysaccharide of. The starting point for the apparatus according to the figure is relatively low salinity of the raw water to the raw water could be, for example, tap water, well water, surface freshwaters, at least in brackish brackish water or even sea water.

The flow channel of the nozzle 2 is driven by means of esikäsi-teltyä / pre-filtered raw water to the membrane filter unit a film element 1, with a reverse osmosis membrane. Kalvoele-element one outlet for the concentrate is connected to the back-cal voelementin input interface through the flow channel. The flow duct nozzle works to use as a tool kalvoele-ment flow and through the pressurized kal-voelementille leading nestetie film element functioning of the necessary pressure.

In the future the system of Figure 2, the raw water is taken either-pressure water pipe 6, a kind of water pressure typically has 3 ... 6 bar, or a low-pressure / pressure-ciated, raw water source, such as a well, lake, river, sea. The inclusion of raw water low-pressure or not pressurized raw water source to the pump for transferring and driving the prefilter 5 raw water is often needed. If the raw water is available under pressure, then the pump 5 is not needed. If the raw water is not very salty, so is quite sufficient that the pump is 5 raises the pressure to about 6 bar. The pump 5 or the valve 6 is controlled by control 14 to enter or refrain from entering the raw water.

The raw water is passed through a pre-filter 4. The pre-filter or pre-filters selected properties of raw water and possibly other grounds. The filters may be several. When making use of water in the household or a similar prefilter 4 is typically sedimenttisuodatin (eg. 5 pm) and activated carbon filter.

The membrane filter unit 1 of filtering and rinsing the rotation can be controlled, for example, based on the attention of the amount of water passing through the system. By placing a flow meter 3 line, where raw water or this pre-filtered water is discharged from the nozzle 2 to achieve the required control information. Preferably, the data is an electronic signal. The information from the flow meter the flow rate and / or flow-through lowing the amount of water supplied to the control unit 14 for controlling the system pumps and valves. Run-through, the amount of water will be monitored in the long term, to obtain information on when filters or other parts should be serviced or replaced. The flow meter may be located ve sikierrossa before or after a pre-filter, or if the pressure pump 15 is part of the apparatus, but also in connection with a pressure pump. Pre-filtered water is conducted from the membrane filter unit to clean the water circuit 1 through the nozzle 2. The nozzle is sized, positioned and shaped so that it flows through the kinetic energy of water provides sufficient water-circulation water to be purified in a closed circuit. Before the nozzle is supplied to the water cycle pressure 2 can be purified to increase the pressure of a pump 15. The membrane filter unit 1, the film passes through a reverse osmosis pure water which is supplied to the tank 9. Since the closed cycle no water gets out by means other than through the membrane is water sisääntu-lovirtaama equal to that of pure water wastage. The membrane permeability depends on the properties of the film, salinity, temperature, and acting over the pressure of the film, which must be greater than the osmotic pressure of the water to be purified, so that the penetration occur. Salinity dirty side of the membrane increases and the membrane surface of the rinsing water circulation function is to carry the excess salt pot-concentration away from the surface of the membrane, reverse osmosis in order to continue. In a closed loop water salinity increases process continues. The membrane of the filter unit 1 the dirty water side of the pass, the incoming water, saline water is removed from the membrane filter unit 1 and is controlled by a valve 7, either to continue to cycle, or to leave the drain 8. The purified water is collected in the tank 9, where it is passed via the drive to pump 10 and valve 11. Pump 10 may be controlled by, for example, the position of the valve 11 or the exhaust pipe 10 of the pump pressure. If necessary or desired, the membrane filter unit 1 DISINFECTED water can continue to be filtered, so that the system is integrated into the post-filter 12. The final filters are typically used for activated carbon. The container 9 is the surface of the water-height measuring apparatus 13, which will inform the controller the water level falls below a certain limit or increase of more than a certain limit. Non-water height information is used to control the amount of purified water production. The salt concentration reaches a sufficient amount to the position of the valve 7 so that the circulating water is discharged from the drain circuit 8. Since the pressure then drops, the nozzle is capable of penetrating two then a greater amount of water in the water cycle and changes rapidly. The change of the water sufficiently, the valve 7 is rotated so that the drain discharge channel is closed and the water circulation channel opens. The pressure in the system increases, the reverse osmosis starts again and the water cycle continues. It should be noted that the flushing of the membrane pressure dropped below the osmotic pressure starts to move the osmosis treated water back through the film. This will substantially improve the membrane purification. To this were to happen, must ensure that the clean water side of the back-flow of water is possible and this is using, even though the required amount is not large. For example, to ensure that the future kalvosuodatinyksiköltä 1 exhaust pipe is always under water in the tank 9.

The device aims at a certain degree of, for example, 80 ... 90% yield. I'm getting zero means the ratio of purified water and the water used. Eg. 90% yield of 90% of the amount of raw water taken from purified reaches 10% and the use concentration folio drain. The desired yield depends on the quality of raw water, raw water burden appears to be of the available pressure, the membrane element characteristics, energy costs etc., and it is set to a predetermined desired.

The simplest control ensures the desired yield by using a flow meter 3. When a closed water circulation device volume Vo is known, measure the amount of water used for rinsing roughly the same level as that volume Vo. During the cleaning process is measured by the amount of water supplied to the device Vi. The control calculates the ratio Vi / (Vo + Vi) and when the desired value is reached, initiating a flush.

When directing the basis of the need for water control 14 starts the pump 5, or open valve 6 and if the system has pressure pump 15, so start the pressure pump 15 when the reservoir 9, the level is set at the lower limit and accordingly stops the pumps and closes the valve when the level cap has been reached. Control is responsible for controlling the valve 7. Hardware when standing idle for long periods of time, can control to do on a regular basis the extraordinary the flush-lukierron.

Figure 3a is a schematic illustration of an apparatus of the present invention is applied. In simple basic structure can be considered similar to the apparatus of Figure 1 - however, differs from the apparatus of Figure 1. The arrangement of Figure 3 can be applied to many, for example, to clean the tap water in small so-called "kitchen sink devices" or other devices with small acquisition is particularly relevant. Similarly, the system is suitable for upper secondary cleaning device, for example, to clean up once purified water even cleaner. Figure 3 apparatus is a continuous process, wherein the valve controls are not required, but the cleaning is done by constant adjustments.

Water treatment device 199 is a membrane filter unit of one put-kistoliittymineen and the flow channel 105, which relates to purified, supplying water under pressure to the nozzle 2. The membrane filter is a one-unit of a pressure-proof vessel practice, inside which is arranged a filter membrane, for example käänteisos-moosisuodatinkalvo.

The membrane filter unit 1 has an input interface 102 aqueous solution for conducting membrane filter unit 1, the first off-the user interface 103 of the permeate passing the membrane filter unit 1 and the second outlet connection to conduct 104 concentrate of the membrane filter unit 1. Interfaces 102.103 and 104 can be thought of the membrane filter unit as being yhteiksi, which join the pipes or connections 102.103 and 104 can also be considered to comprise pipes, which relate to other parts of the water treatment plant. Water treatment device 199 to join the inlet 102 leading into the flow channel is connected to a water processing device 101, the second outlet connection, the concentrate can be recirculated. Chicken-flow Vassa 105 is a nozzle 2 for supplying new water to be treated under pressure to the flow passage. The nozzle 2 to enter new water to be treated fairly high speed input interface 102 a. The nozzle fed by the amount of water volume flow is somewhat higher than filtered through the membrane and ultimately leaves the first outlet junction 103. This rapid flow nozzle arranged on the surface of the film. The nozzles may, if necessary, be more than one, especially if the apparatus has a plurality of parallel filter units of the film.

Such water treatment device is a going concern. The amount of water has to input the number of exiting the permeate plus the amount of the concentrate, which is allowed to leak back-kytkentähaarasta via the outlet connection 198. Poistoliittymäs to-gether 198 is limited in the flow throttling so that yhteeltä 104, starting the feedback pressure drop significantly. The flow limiting poistoliittymänä is suitably, for example, a needle valve or other means, to the amount of flow can be set.

Figure 3a is supplied to the apparatus from a nozzle membrane unit feed stream, the incoming volume flow rate Qin, the pressure p of the power p * Qin. The concentrate is recycled in the recycling and the pipe is controlled leak. Konsentraattivuoto throttled so as to achieve the desired yield, R, e.g. 90%. In this case, permeaattivirtaama is Qp = R * Qi and leaking konsentraattivirtaama Qc = (R) * Qin.

The device is a continuous and run the desired recovery ratiol-la, which thus can therefore be quite high. Thus, if R = 90%, leaving the concentrate is accompanied by the loss of energy as 10%, and the apparatus can be run continuously maksimipaineel-la.

If the incoming water salt concentration, or other substance is relatively small, not the minimum and maximum differential pressure is not large, on the order of 5 ... 10%, wherein the device, which should be optimized with respect to energy consumption to a minimum, compared with losses of only around 15 ... 20% higher. In such a device, the energy consumption due to pressure losses when energy consumption is not necessarily significant additional costs, at least not if the system activates the mains water supply pressure. The practice reached more than 90% of the yield is clearly better than those of many commercial "kitchen sink devices" that are able to take advantage of less than half its raw water. A simple composition and operation of the equipment are a great advantage.

Figure 3b shows the apparatus of Figure 3a of the present modified apparatus. Figure 3b apparatus 197 the starting point is to provide a simple and easy-action "kitchen sink device" or the like for household use. Machine operation is controlled tulovesiventtiilillä 195. The water supply pipe 194 is a 2 between the water supply valve 195 and the nozzle is flush cistern 196. The cistern fills up and empties a lesser pressure than the membrane filter unit 1 passes through the filter membrane and penetrates significantly. Preferably, the rinsing tank 196 is built on a flexible rubber bag or the like, which fills and expands very small pressure, for example less than 0. 5bar, which pressure is also greatly below the water line supplying the pressure. Thus the rinsing tank 196 is full, the valve 195 is opened, and the membrane filter apparatus 197 begins to operate the apparatus as shown in Figure 3a. When the valve 195 is closed, the pressure begins to fade and the hardware section of the permeate inlet outlet junction 103 stops. Back pressure decreases coupled continues to flow under pressure from the flush tank 196 and spilling through the constriction 198 for a while. At the same time pushes the back-flush the membrane adhering to the impurities back to the concentrate to permeate the film itself is saturated. The same function can be used for flexibility in system components such as pipes, filters, or other containers, instead of a separate cistern.

Figures 4a and 4b are applied schematic representation of the invention is the water treatment device 101, having a plurality of membrane filter units 1 putkistoliittymineen and the flow channel 105, which relates to clean water under pressure to the feeding nozzle 2. In this embodiment, the number of membrane filter units 1, each comprising a pressure-proof vessel in which the inside is provided membrane filter, for example, the reverse osmosis membrane filter, the water is arranged to pass the common flow channel 105, or alternatively common flow channels.

The common flow channel 105 is passed 204 through piping second outlet Accession 104 concentrate and the common flow channel 105 into the concentrate, which mixes input nozzle 2 not yet treated aqueous solution, distribution piping 202 membrane filter units 1 si-inlet interfaces 102. The membrane filter units one first outlet connections 103 of the permeate passing kalvosuodatinyk- coker 1 is connected one poistoputkituksella 203. Vir-passage 105 can be separate from the actuator 222, such as a pump or propeller, or flow is maintained in the nozzle 2 a directed high-pressure water supply flow channel 105.

102.103 interfaces 104 and may be thought of the membrane filter unit as being one-yhteiksi, which join the pipes or connections 102.103 and 104 can also be considered to comprise pipes for joining with other water treatment plant piping layout, 202, 203, 204.

Water treatment device 101 is made the working pressure of the pump 215 for supplying water to the inlet 2 via the interface 102 leading into the flow channel of the nozzle. The nozzle 2 fed by the amount of water volume flow is the same as the film filtered and ultimately leaves the first outlet accession poistoputkitukseen 203. One nozzle will in many cases do so, but, for example, very large systems with a plurality of interconnected membrane filter-unit, a may be advantageous to use more nozzles of the flow channel, or possibly even more virtauska-channels the flow source.

Water treatment device operation is the easiest to make a cyclic so that the equipment is filtered and alternately shifts the concentrated concentrate is removed. Flow channel 105 or the associated piping layout, 202, 204 is connected to the discharge valve 207 for the removal of the concentrated network-concentrate.

Figures 5a, 5b, 5c, 5d is a schematic illustration of the present exemplary membrane separation / filter membrane systems, the membrane filter with two points 501, 502 are connected in series. Kal-vosuodatinyksiköiden engagement different solutions, depending on the selected operational mode. The first pump 503 to make the first filtration stage filter unit 501, or in some cases, the entire series-connected filtering units in one-chain. The second pump 504 is feeding the second grant-cure step suotatinyksikköä 502. For larger plants in each filter stage can be more filter units in parallel and the necessary liquid to the number of pumps, either so that adjacent filter units of water supplies are connected to each other or so that each of the filtering degree of the filtering unit has its own only this suodatusyk-priming pump unit.

In the solution of Figure 5a is arranged in the first stage of the filtration cycle and the second step is carried out continuously. In the first cleaning stage pump 503 to make the water to be purified through the nozzle 507 toward the flow channel 506, causing the flow of filter unit 501, which per-meaatti from the storage tank 505, and the concentrate back into the flow channel. This cycle is maintained, of course, concentrated in the concentrate, until the basis of the selected circuit ohjauskritee-exchanged concentrate is entirely or almost entirely a new water to be purified. Changeover occurs valve device 512, which is directed to the concentrate to dissolve the drain line of a dashed line down, rather than concentrate is recirculated be led suodatinyksiköl-le 501. At the same time the valve is opened nestetie device 512, which is passed back to clean the pump 503 to replace the water removed from the concentrate. When the concentrate has been replaced by the valve device 512 is controlled to close its coming through the feed water to be purified and led back to the concentrate flow channel. In a second purification stage pump 504 pump-end of the container 505 of the first stage permeate to the second stage of further refining. The flow duct 508 becomes the pressure feeding the nozzle 509 through the flow as well as maintenance. The second filter unit 502 can be very pure permeate, the arrow to the right. The second phase of the concentrate is partially recycled to the throttle valve 508 and partially through the flow channel 511 of the first stage of refining. The pressure ratios are easily adjustable wall upgraded so that the throttle valve 511 through the recycle second phase of the concentrate is fed into the front of the pump 503. Alternatively, the solution of Figure 5a may be omitted tank 505 and the pump 504 and to connect the first filter unit 501 permeaattiulostulo directly enter the second stage permeate through the nozzle 509, wherein the second phase of the cyclic operation of the first stage. Such an option would require, of course, fitting 503 of the pump and pressure conditions.

In the solution of Figure 5b has both the first and second filtering stage arranged to cyclic. In the first cleaning stage, the pump 503 to make the water to be purified through the nozzle 507 toward the flow channel 506, causing the flow of filter unit 501, which permeate is led to a storage tank 505, and the concentrate back into the flow channel. First the nal stage of the concentrate was replaced by a new cycle of the water to be purified in the same manner as in the apparatus of Figure 5a. In a second purification stage pump 504 to pump the reservoir 505 of the first stage permeate to the second stage of further refining. The second phase is also controlled to operate cyclically. The flow duct 508 becomes the pressure feeding the nozzle 509 through the flow as well as maintenance. The second filter unit 502 can be very pure permeate, the arrow to the right. The second phase of the concentrate was recycled back to the flow channel 508.

Figure 5b the second cleaning stage supplied by the circulation pump 504 is maintained until the control criterion based on the selected gear of the second phase of the concentrate is completely or almost completely new to a first stage permeate. Changeover occurs valve device 513, which is controlled by decode the second phase of the concentrate of the first stage pump 503 in front, instead of the concentrate be led to circulate back to the filter unit 502. At the same time opens the valve device 513 nestetie, which is led past the pump 504 in place of the concentrate I first stage permeate from the second stage to be removed.

FIGURE 5c solution has both first and second-stage filtrations carried out as continuous, and each step is action-nettu own pumpuillaan. In the first cleaning stage pump 503 to make the water to be purified through the nozzle 507 the flow channel 506, causing a flow of units of the give-501, which permeate is led to a storage tank 505 and the back part of the concentrate flow channel and partially through the throttle valve 510 drains. In a second purification stage pump 504 to pump the reservoir 505 of the first stage permeate to the second stage of further refining. The flow duct 508 becomes the pressure feeding the nozzle 509 through the flow as well as maintenance. The second filter unit 502 can be very pure permeate, the arrow to the right. The second phase is partially recycled to the concentrate flow channel 508 and in part through a throttling valve 511 of the first stage of refining.

FIGURE 5d solution has both first and second-stage filtrations carried out as continuous and jointly the two phases of operation as a pump. Figure 5d solution similar to the Figure 5c solution, with the difference that the first grant permeaattiulostulo-filter unit 501 is adapted to directly enter the second stage permeate through the nozzle 509.

Figures 6a and 6b show the present preferred to use a membrane filter device fluid circulation nozzle design concept. The flow channel 61 is disposed inside the nozzle 62, which on the side facing in the direction of the flow channel slot 63. Figure 6a shows the nozzle flow channel incoming direction of fluid flow as well as the flow direction of the fluid flow channel is implicitly addressed by means of arrows. Due to the turbulence and the fact that the future of the nozzle jet tends to open, flows directions put forward by the arrows are by no means exact.

Those skilled in the art it is obvious that the invention is not limited to the above examples but can be varied in the following claims and the specification and shown in the drawings within the framework.

The invention may also occur, for example, 1-12 compatible with the following paragraphs, or to affect one or more of the above aspect of the invention, and one of the following positions 1-12 in combination.

1. In a method for arranging the liquid circulation kalvosuodatukses-in, in which method the fluid-pressure source in fluid flow filter membrane and the filter membrane impermeable to fluid flow, at least part of the compound to the fluid-pressure source of fluid flow.

2. The appropriate method of item 1, wherein the filter membrane impermeable to liquid flow connected to the liquid-pressure source to the fluid flow.

3. The appropriate item 1 or 2 as a method in which both the filter membrane permeable to fluid flow and the filter membrane impermeable to liquid flow is maintained in the fluid-pressure source coming fluid flow.

4. A under paragraph 1-3 as a method in which the amount and / or pressure or at least one of the-pressure fluid source to the fluid flow of the transformation is controlled cyclically and / or at least one of the following reasons: a pressure filter membrane impermeable fluid flow, the magnitude of the filter membrane permeable liquid flow, the magnitude of the filter membrane impermeable to fluid flow, the concentration of one or more filter membrane impermeable substance in a fluid flow, the concentration of one or more filter membrane permeable substance fluid flow.

5. In accordance with paragraph 4 method, which stipulated on the basis ohjauskri-sedentary filter membrane impermeable nestekier-ron flow of liquid at least partially replaced by the fluid-pressure source of fluid.

6. A method of point 1-5, wherein the filter membrane impermeable to fluid flow pressure is reduced down times so that the filter membrane permeated liquid stream flow direction is reversed.

7. Kalvosuodatinlaitteistona, wherein the at least one filter membrane, the filtration membrane on opposite sides of the first liquid chamber and the second liquid chamber, arranged over said filter membrane a pressure difference, the first fluid space of said filtering film-way fluid flow from the first fluid space in the second fluid space pressure differential due to fluid flow and fluid supply a first fluid space-pressure fluid source, and the membrane filter apparatus has a flow path parallel to at least a portion of said fluid flow passing the filter membrane with a back-pressure liquid source to the liquid flow.

8. In accordance with paragraph 7 in hardware, wherein the filter membrane without passing the filter membrane bypassing the liquid flow is derived from the fluid-pressure source, the flow of liquid to merge.

9. appropriate item 7 or 8 in hardware, and wherein the filter membrane permeable to fluid flow passing the filter membrane is arranged on the liquid flow-pressure fluid source to the fluid flow.

10. The membrane filter device, which includes kalvosuodatinyksik-unit, wherein the input interface of the aqueous solution deriving cal-vosuodatinyksikköön, the first outlet connection of the permeate passing the membrane filter unit and the second outlet connection for conducting concentrate the membrane filter unit and a water processing device comprises the input to join the leading flow channel and the second outlet connection is derived from the flow channel and the flow channel is a second interface towards the discharge flow connection in the flow of maintaining the actuator, such as a pump, propeller or nozzle, and that the present high-pressure water flow channel for supplying (105) the flow conduit is a nozzle.

11. The membrane filter device, which includes kalvosuodatinyksik-unit, wherein the input interface of the aqueous solution deriving cal-vosuodatinyksikköön, the first outlet connection of the permeate passing the membrane filter unit and the second outlet connection for conducting concentrate the membrane filter unit and a water processing device comprises the input to join the leading flow channel and the second outlet connection is derived from the flow channel and the flow channel is a nozzle for supplying water to be treated flow channel and the nozzle is arranged to supply treated water to pass towards the exit.

12. The appropriate 10 or 11 of the membrane filter device, wherein the nozzle exclusive or more flow channel for supplying a nozzle together is the exclusive flow passage of the second poistoliitty-system interface towards the direction of the feed flow in the drive means.

Claims

A method by which the liquid circulation is arranged in membrane filtration by flow over a membrane (crossflow filtration), in which a liquid flow from a pressurized liquid source via a flow channel (105) is fed to a filter membrane, characterized in that at least part of the liquid flow which does not penetrate the filter membrane in the flow channel (105) is associated with the fluid flow from the pressurized liquid source and that both the liquid flow which penetrates the filter membrane and the liquid flow which does not penetrate the filter membrane is maintained by means of the liquid flow which is fed from the pressurized fluid into the mouth of the pressurized liquid.

2. A method according to claim 1, characterized in that the amount and / or pressure of the liquid source flowing from the pressurized liquid source is controlled cyclically and / or on the basis of at least one of the following: the pressure in the liquid flow which does not penetrate the filter membrane, the size of the liquid flow that penetrates the filter membrane, the size of the liquid flow that does not penetrate the filter membrane, the concentration of one or more substances in the liquid flow that does not penetrate the filter membrane, the concentration of one or more substances in the liquid flow that penetrates the filter membrane, the selected control criterion the liquid in the liquid flow that does not penetrate the filter membrane is at least partially replaced by the liquid from the pressurized source of fluid.

Method according to one of the preceding claims, characterized in that the pressure in the liquid flow which does not penetrate the filter membrane is at times lowered so much that the flow direction of the liquid flow penetrating the filter membrane is reversed.

4. A membrane filter device, provided with at least one filter membrane, on opposite sides of the filter membrane a first liquid space and a second liquid space, a pressure difference acting over the filter membrane, second liquid space and supply of liquid from the pressurized liquid source via the flow channel (105) to the first liquid space and the filter membrane, characterized in that at least a portion of the liquid flow which does not penetrate the filter membrane in the flow source (105) is connected to the liquid flow from the fluid flow (105). both the fluid flow penetrating the filter membrane and the fluid flow passing past the filter membrane are arranged by means of the fluid flow which is fed from the pressurized fluid source with a nozzle into the liquid circulation.

A membrane filter device (101), comprising a membrane filter unit (1) having an input connection (102) which conducts the aqueous solution to the membrane filter unit (1), a first output connection (103) which conducts the permeate from the membrane filter unit (1) and a second output connection (104) conducting the concentrate from the membrane filter unit (1), and which water treatment apparatus (101) comprises a flow channel (105) leading to the input terminal (102), characterized in that the second output terminal (104) is directed to the flow channel (105) and the flow channel (105) is provided with a nozzle (2) directed from the second output terminal (104) towards the input terminal (102), which is arranged to conduct the high-pressure water to be treated to the flow channel (105), and the folded nozzle ( 2) is a drive for the flow directed in the flow channel from the second output terminal (104) to the input terminal (102).

A membrane filter device (101), comprising a membrane filter unit (1) having an input connection (102) which conducts water solution to the membrane filter unit (1), a first output connection (103) which conducts the permeate from the membrane filter unit (1) and a second an output terminal (104) conducting the concentrate from the membrane filter unit (1), and the water treatment apparatus (101) comprising a flow channel (105) leading to the input terminal (102), characterized in that the second output terminal (104) is directed to the flow channel (105) and the flow channel (105) is provided with a nozzle (2) directed towards the inlet connection, which conducts the water to be treated to the flow channel (105), and that the nozzle (2) is arranged to supply the water to be treated against the inlet connection (102) and the fold nozzle (2) is the drive for the flow directed in the flow channel from the second output terminal (104) to the input terminal (102).

Membrane filter device according to claim 5 or 6, characterized in that the nozzle (2) alone or several nozzles which together feed to the flow channel (105) is the only driving device for the flow in the flow channel from the second output connection (104) to the input terminal (102). flow.