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    • 专利摘要:
    The method and apparatus are for the elimination of micropollutants in a liquid (2), such as waste water or drinking water, by adsorption on an adsorbent (3), preferably granulated activated carbon (GAK), in a reactor (14), one with at least one A contact zone (14A), in which the adsorbent (3) is provided, and above the contact zone (14A) has a projection zone (14C) with at least one outlet opening (15A, 15B) from which the micropollutants are liberated Liquid (2) emerges. According to the invention, the liquid (2) which flows through the reactor (14) from the contact zone (14A) to the supernatant zone (14C) is conveyed through the reactor (14) in at least two process phases (ph1, ph2), wherein in a feed phase ( ph1) for a first time period (d ph 1) liquid (2) introduced through the inlet opening (13) in the reactor (14) and in a rest phase (ph2) for a second period of time (dp h2) the transfer of the liquid (2) is reduced, stopped and / or changed in the direction by the inlet opening (13).
    公开号:CH715046A2
    申请号:CH10672018
    申请日:2018-09-07
    公开日:2019-11-29
    发明作者:Meyer David
    申请人:Meyer David；
    IPC主号:
    专利说明:

    Description: The present invention relates to a method and a device for eliminating micropollutants in aqueous liquids, such as waste water or drinking water.
    Daily residues of organic chemicals - such as medicines, cleaning agents, rust inhibitors, pesticides or the like - get into the water after their use as micropollutants. Here they can adversely affect aquatic life and pollute drinking water resources. Diffuse sources, such as agricultural sources, also play a role in the entry of such trace substances, but medicines and other chemicals largely come from the wastewater of the municipal sewage treatment plants. Conventional wastewater treatment plants (ARA) can hardly eliminate such residues, which is why retrofitting of these plants is in progress (see [1], “Micropollutants from municipal wastewater, processes for extensive elimination in sewage treatment plants”, published by the Federal Office for the Environment FOEN, Bern 2012.
    Known methods for eliminating micropollutants in aqueous liquids implement e.g. ozonation (see [1], chapter 8), adsorption on powdered activated carbon (PAH) (see [1], chapter 9) and adsorption on granulated activated carbon (GAK) (see [1], chapter 10). The aqueous liquid is usually water that is to be treated as drinking water or wastewater that is to be cleaned.
    The use of granulated activated carbon (GAK) as an adsorbent differs from the use of powdered activated carbon (PAK) as an adsorbent essentially in two ways.
    On the one hand, the GAK adsorption is carried out in fixed bed adsorbers, i.e. the wastewater flows through a filter zone filled with activated carbon, the activated carbon itself is not transported and should remain in the filter zone. As a result, no further separation is required and the activated carbon can be replaced and regenerated after the adsorption capacity has been exhausted.
    On the other hand, GAK grain sizes in the range of a few mm, e.g. used in a range of 100 pm-2000 µm, while the PAH grains have a diameter in the range of a few µm, e.g. 3 pm-100 μm. The specific surface of GAK is therefore much smaller than that of PAK.
    Filtration with granulated activated carbon (GAK) is also described in [2], DE 2 410 007 A1; [3], WO 2006 013 235 A1; [4], WO 2014 184 371 A1, and [5], AQUA & GAS, No. 7, 2017. According to the process disclosed in [5], the waste water flows through a coal bed with granulated activated carbon in a treatment step from bottom to top. In order to keep the activated carbon layer with a particle size in the range of 200 pm-900 μm in suspension, the flow rate is selected in a range of 7 m / h-15 m / h depending on the coal product. The flow rate is maintained by an internal recirculation when there is little waste water. The average time the activated carbon stays in the system is 80 to 100 days. Fresh coal is not added continuously, as is usual with PAH systems, but periodically (daily or several times a week) and the loaded GAK is withdrawn from the system and kept for regeneration. When fresh coal is added, fine particles are separated beforehand so that they do not get into the receiving water via the drain. In the case of increased solids loads in the feed to the GAK system, this causes the activated carbon bed to expand more, which is undesirable and the system must then be backwashed. Furthermore, the height or expansion of the carbon bed is continuously monitored.
    In comparison, the PAK method and the GAK method have individual advantages and disadvantages. The GAK process has a reduced efficiency due to the lower specific surface area of GAK, i.e. a lower adsorption of micropollutants per unit of time. Furthermore, in the GAK process, the flow rate of the liquid to be cleaned is limited in order to prevent the granules from flowing off.
    The present invention is therefore based on the object to provide an improved method and an improved device for eliminating micropollutants by means of an adsorbent in aqueous liquids.
    In particular, the method should lead to a faster elimination of micropollutants when using an adsorbent. The process is said to have a higher efficiency per volume and to increase the yield of purified liquid, in particular clear water.
    The device according to the invention created for carrying out the method according to the invention should, as far as possible, require little or no additional construction. The design effort should preferably be reduced if possible.
    This object is achieved with a method according to claim 1 and a device according to claim 10. Advantageous embodiments of the invention are specified in the dependent claims.
    The method and the device are used to eliminate micropollutants - such as medications, cleaning agents, rust inhibitors, pesticides or the like, typically in trace concentrations - in a liquid, such as waste water or drinking water, by adsorption on an adsorbent as a powder or granules, preferably granulated Activated carbon (GAK), in a reactor which has a contact zone provided with at least one inlet opening,
    CH 715 046 A2 in which the adsorbent is provided and above the contact zone has a supernatant zone with at least one outlet opening from which the liquid or clear water freed from the micro-contaminants emerges.
    According to the invention, the liquid which flows through the reactor from the contact zone to the supernatant zone is conveyed through the reactor in at least two process phases, liquid being introduced through the inlet opening into the reactor for a first period of time and in a resting phase for one second period of time the transfer of the liquid through the inlet opening is reduced, stopped and / or changed or inverted in the direction.
    In the reactor, a bed with adsorbent material, preferably granulated activated carbon (GAK), is charged at intervals in the upward flow with the aqueous liquid to be treated, a resting phase being provided between each charging phase. The resting phase is used for lowering, possibly sedimentation of the adsorption material in the reactor, so that the supernatant is formed as purified clear water, which is largely freed of micro-impurities and also of adsorbent and can be removed.
    During the charging phase, the aqueous liquid to be cleaned is added from below in the reactor foot in the reactor in such a way that an upward flow is generated, and preferably at a rate of rise at which the adsorbent material is whirled up in the reactor. During this process, the supernatant zone is filled with liquid from the contact zone below it and, due to the high rate of climb, with whirled up adsorbent, which is why it must be prevented that it reaches the open outlet opening. The duration of the charging phase until it stops is therefore chosen such that the adsorbent is not flushed out of the top of the reactor.
    During the resting phase, the addition of the aqueous liquid is completely stopped and / or reduced and / or inverted in order to stop the upward flow of the liquid and to invert the direction of movement of the adsorbent. Stopping, reducing or inverting the liquid flow can be carried out individually or in combination during the rest phase either for selectable or fixed periods of time. The changes can be gradual or linear. For example, a reflux is first provided, after which the liquid flow is stopped or kept at a low value in one of the two flow directions. Changes in the volume flow in the loading phase and / or the resting phase can also take place ascending or descending along a curve or ramp. During the rest phase, the concentration of the adsorbent in the liquid in the contact zone is very high and thus achieves a high adsorption capacity of micropollutants within a short time, while in the cleaned liquid in the supernatant zone there is first a sinking and finally no more adsorbent. The duration of the resting phase preferably lasts until the adsorbent is completely, partially or almost completely sedimented in the reactor. As soon as the sedimentation has taken place sufficiently, the cycle starts again.
    The outflow of the cleaned liquid or the clear water takes place in the loading phase and / or in the resting phase. In the charging phase, the outflow preferably takes place continuously, primarily depending on the liquid to be cleaned supplied or on the basis of further parameters and / or on the basis of determined measured values. If using sensors e.g. if it is measured that the supernatant zone is still free of adsorbent, the discharge can take place with a higher volume flow. In the resting phase, cleaned liquid (clear water) can be removed continuously or optionally from the reactor.
    The cleaned liquid or the clear water can be derived from the reactor or pressed out by supplying pressure or gravity. The clear water can be discharged from the reactor at the top of the reactor or also lower, above the adsorbent, which may be completely sedimented. In the first case, pressure is required. In the second case, it is derived by acting gravitational forces. The clear water is not pressed out of the reactor at the top in the supernatant zone during or towards the end of the resting phase, but instead is discharged from the reactor through the outlet level, which is located slightly above the upper edge of the contact zone. For this, sufficient time must be allowed for sufficient or complete sedimentation of the adsorbent before the draining can be started. The advantage here is the reduced energy requirement because the liquid does not have to be pressed out at the upper outlet opening on the reactor head, but instead runs out of the reactor by the action of gravity. On the other hand, an extended resting phase is typically required so that there is sufficient sedimentation of the adsorbent.
    The inventive method and the device have significant advantages. With the method according to the invention, a higher concentration of adsorbent material in the contact zone and thus a more intensive interaction between the liquid to be cleaned and the adsorbent is achieved without the adsorbent material clumping or clogging. The higher concentration of the adsorbent makes it possible to reduce the volume required for the treatment of the liquid. This enables a reduction in the volume of the reactors and a shorter cleaning time for a given desired elimination rate of micropollutants in the liquid. Furthermore, a larger flow or a higher yield of purified liquid can be achieved. Smaller reactor volumes allow the plant to be designed in such a way that the water does not have to be pushed up as high, which results in significant energy savings. If pumps are used to overcome the height, they experience less wear thanks to the lower pump height and are therefore less expensive to maintain.
    CH 715 046 A2 In a preferred embodiment of the invention, an intermediate phase is provided between the loading phase and the resting phase, the volume flow of the liquid is specifically controlled and the liquid e.g. is preferably returned to the outside through the inlet opening in one or more pulses. In this way, the movement of the adsorbent is stopped abruptly and sedimentation is achieved within a shorter time.
    [0023] The liquid to be cleaned can be conveyed to the at least one inlet opening by means of a pre-pressure and, if appropriate, via an inlet valve or by means of a feed pump and optionally via an inlet valve. For example, the liquid is led from a higher storage basin to the inlet opening or to the inlet valve. By controlling the inlet valve, the flow can be set, increased, reduced or stopped. The use of a correspondingly designed feed pump allows the liquid to be introduced into the inlet opening at a higher pressure and the flow to be controlled more precisely. In addition, the feed pump allows the flow direction to be changed optionally. It is possible to introduce the liquid into the reactor in pulses or to flow through at least one counter pulse, i.e. apply a brief, intense reflux to affect the movement of the adsorbent. The inlet valve is preferably controllable in such a way that the flow can be changed or the inlet opening can be closed when the feed pump is not in operation.
    In further preferred embodiments, the expansion of the adsorbent to the supernatant zone is monitored by means of at least one sensor, the measurement signals of which are evaluated in a control unit which, according to the evaluation, preferably the feed pump and / or the inlet valve and / or an outlet valve connected to the outlet opening in particular controls such that the adsorbent is prevented from escaping through the active outlet opening.
    [0025] In preferred configurations, it is provided
    a) that the loading phase and the rest phase and, if applicable, subsequent further process phases take place cyclically; and or
    b) that the loading phase and the resting phase and, if appropriate, subsequent further process phases take place cyclically and the flow rate is preferably controlled individually in each process phase; and or
    c) that the loading phase and the rest phase and, if appropriate, subsequent further process phases run cyclically and that the time spans of the loading phase and the rest phase and, if appropriate, subsequent further process phases are individually controlled.
    In cycles that include at least one loading phase and a rest phase, individual intermediate phases can also be optionally inserted, in which the volume flow is changed. Intermediate phases can also be inserted if necessary, e.g. if impermissible conditions are determined by means of the sensors.
    Intermediate phases can also be inserted, in which e.g. is acted on the adsorbent. For example, an interim phase is inserted after 100 cycles, in which e.g. used adsorbent removed and new adsorbent is fed. These processes can also be controlled automatically.
    In a further preferred embodiment, the time period of the rest phase and / or the transfer of the liquid through the inlet opening during the rest phase is selected such that the adsorbent after the end of the rest phase is substantially below a rest level, which is preferably monitored by means of a rest sensor , As soon as the adsorbent has sedimented enough, cleaned liquid can be discharged from a lower outlet opening. Furthermore, the adsorbent or its expansion can be monitored, so that an optimization of the method or an optimized control of the loading phases and the rest phases, possibly the intermediate phases, is possible. For example, After the sedimentation has taken place, the next loading phase can be started earlier. In this way, the throughput can be increased by up to 10% or more.
    In a further preferred embodiment, the at least one outlet opening or at least one of a plurality of outlet openings is arranged at a height level that
    a) during the loading phase of the expanded adsorbent or
    b) is not reached by the resting adsorbent after the resting phase.
    The cleaned liquid can therefore flow out in both cases through the outlet opening, which is at a height level, possibly the said resting level, which is not reached by the adsorbent.
    CH 715 046 A2 In a further preferred embodiment, the liquid is introduced into the reactor through the at least one inlet opening or through a plurality of distributed inlet openings with a uniform or individual, constant or variable flow rate in such a way that the adsorbent is swirled. The inlet openings are preferably provided radially evenly distributed on the side of the reactor and / or preferably evenly distributed on the underside of the reactor. By distributing the inlet openings, the adsorbent is swirled over the entire cross section of the reactor and thus an optimized coupling or an intensified encounter of the incoming liquid and the adsorbent. Due to the distribution of the inlet openings, their diameter can also be reduced, so that it is prevented that a central water flow can reach the protruding zone practically without contacting the adsorbent. At the same time, it is prevented that adsorbent is quickly driven upwards with a large central water flow. Instead, the adsorbent remains longer on the underside of the reactor or the contact zone and swirls without being driven up quickly. In this way, the time span of the loading phase can advantageously be extended.
    In a particularly preferred embodiment, a displaceable and / or deformable filter is arranged in the reactor, preferably in the supernatant zone or in an intermediate zone lying between the contact zone and the supernatant zone, which filter in the loading phase with the adsorbent from a starting position towards a final position shifted upwards or deformed and is returned to the starting position by means of a drive or by gravitation during the resting phase. The filter that collects the adsorbent can e.g. be returned by means of an extendable piston. Alternatively, the specific weight of the filter is dimensioned in such a way that it is displaced or deformed when the liquid is introduced. In the resting phase, in the absence of a flow or with a reduced flow, however, the filter is quickly returned to the starting position by its own weight together with the adsorbent. In this way, it is advantageous to shorten the period of the rest phases. Stationary filters are usually avoided.
    The invention is explained in more detail below with reference to drawings. It shows:
    1a shows a device 1 according to the invention for eliminating micropollutants in a liquid 2 in a reactor 14, in which a liquid 2 to be cleaned in at least two process phases ph1, ph2 through a contact zone 14A provided with adsorbent 3 and through a projection zone 14C to an outlet opening 15A, 15B;
    1b shows the device 1 from FIG. 1a in a first process phase or the charging phase ph1, during which the liquid 2A to be cleaned is passed through the adsorbent 3, which subsequently expands in the direction of the supernatant zone 14C;
    1c shows the device 1 from FIG. 1a in a second process phase or the rest phase ph2, in which the adsorbent 3 migrates back towards the starting position by gravitational force;
    2a shows the device 1 from FIG. 1 in a preferred embodiment with a displaceable or deformable filter 6, which is displaced or deformed in the loading phase ph1 in the direction of the overhang zone 14C;
    FIG. 2b shows the device 1 from FIG. 2a in the resting phase ph2, in which the filter 6 is displaced or deformed in the direction of the contact zone 14A by a drive 62 or by gravity, the adsorbent 3 being pushed back in the direction of the starting position;
    3a shows a first process flow in the devices 1 from FIGS. 1a and 2a with two cyclically repeating process phases ph1, ph2 of constant length and volume flows Q1, Q21, -Q22 charged therein;
    3b shows a second process flow in the devices 1 from FIGS. 1a and 2a with two cyclically repeating process phases ph1, ph2 and volume flows charged therein, which are changed as required; and
    3c the representation of a third process course in the devices 1 from FIGS. 1a and 2a with three preferably cyclically repeating process phases ph1, ph2, the length of which is controlled as required, and volume flows charged therein, which are also changed as required.
    Fig. 1a shows a basic representation of an inventive device 1 for eliminating micropollutants in a liquid 2, such as waste water or drinking water to be treated, with a reactor 14 in which a liquid 2 to be cleaned in at least two process phases ph1, ph2 by a contact zone 14A provided with adsorbent 3 and is led through an overhang zone 14C to an outlet opening 15A, 15B.
    CH 715 046 A2 The adsorbent is preferably granulated activated carbon (GAK) However, the process according to the invention is not limited to granulated activated carbon, but can be carried out with all adsorbents which have similar relevant physical properties.
    The reactor 14 laterally has at least one inlet opening 13 through which liquid 2 to be cleaned can enter at the bottom of the reactor 14 or at the reactor foot. Preferably, a plurality of inlet openings 13 are laterally distributed radially and / or are provided on the underside of the reactor 14, so that the liquid 2 or 2A can penetrate into the contact zone 14A at different points and can contact, swirl and penetrate the adsorbent 3 over virtually the entire cross section. It is illustrated that when the absorption layer 3 penetrates over the entire cross section, the absorption medium is swirled.
    The at least one inlet opening 13 is connected via an inlet valve 12 to a feed pump 11, by means of which the liquid 2 can preferably be fed back and forth in both directions, but possibly only into the reactor. The inlet valve 12 and the feed pump 11 are connected via control lines 110, 120 to a control unit 10 in which an operating and control program 100 is implemented.
    [0038] Alternatively, other means for opening and closing the inlet opening 13 can also be provided. For example, a manually or motor-operated slide can also be provided. The liquid 2 can also be introduced into the reactor under pressure without a feed pump 11, e.g. from a higher basin. Different configurations are therefore possible.
    The supernatant zone 14C is located above the resting adsorbent 3 in the contact zone 14A. An intermediate zone 14B may be provided between the contact zone 14A and the protruding zone 14C. If provided, rules can be established for this intermediate zone 14B. For example, can be determined at which times in the process phases the adsorbent 3 may occur there. Alternatively, the state of the intermediate zone 14B, which is monitored by a sensor 18B, can be used as a decision criterion for the process control.
    In the area of the intermediate zone 14B and the protruding zone 14, outlet openings 15A, 15B and adjoining outlet valves 16A, 16B are provided, which can be optionally operated by the control unit 10 via control lines 160A, 160B in order to clean the liquid 2, 2B at the top To be discharged from the reactor 14 at the end of the reactor 14 or at the reactor head or above the contact zone 14A, in particular above the adsorbent (for example activated carbon bed) 3, in an energy-optimized manner. In order to determine whether there is no longer any adsorbent 3 at the level rn of the lower outlet opening 15B, a sensor 18D is provided.
    1a shows that four sensors 18A, 18B, 18C and 18D are provided for monitoring the process and the process phases, the measurement signals of which are transmitted via sensor lines 180A, 180B, 180C and 18 OD to the control unit 10 and evaluated there subsequently control the feed pump 11 and / or the one or more inlet valves 12 and / or the outlet valves 16A, 16B in accordance with the measured process state.
    Fig. 1a further shows symbolically the process and the device 30 for the exchange of the adsorbent 3. Preferably, adsorbent 3 saturated with micropollutants is automatically removed from the reactor 14 and new adsorbent 3 is also automatically reintroduced into the reactor 14. The process is preferably controlled by the control unit 10 via a control line 300.
    Fig. 1b shows the device 1 of Fig. 1a in a first process phase or in the loading phase ph1, during which the liquid to be cleaned 2, 2A is introduced through the inlet opening 13 into the reactor 14 and in the contact zone 14A through the Adsorbent 3 is passed through, which swirls in succession and expands towards the supernatant zone 14C. The liquid 2, 2A to be cleaned is passed under pressure, optionally conveyed through the feed pump 11 and / or optionally through the inlet valve 12, to which at least one inlet opening 13 is fed.
    In the reactor 14, the aqueous liquid 2 to be treated comes into contact with the adsorbent 3 (e.g. activated carbon). The adsorbent 3 has the property of adsorbing micropollutants contained in the liquid 2 and thus cleaning the liquid 2.
    As described above, the flow rate and the volume of the liquid 2 supplied via the at least one inlet opening 13 are selected such that the adsorbent 3 is whirled up. The flow rate or volume flow Q (m3 / s) in the charging phase is preferably selected such that the rate of climb in the reactor 14 is between 20-200 m / h. The volume flow Q of the liquid 2 supplied is correspondingly adapted to the reactor volume. The liquid 2 moved at a relatively high rate of rise swirls up the adsorbent 3 and carries the adsorbent 3 together with the liquid 2 into the upper part of the reactor 14 or into the supernatant zone 14C. The feed time during which the liquid 2 is introduced into the reactor 14 is selected such that it only lasts until the swirled adsorbent 3 reaches the uppermost region of the supernatant zone 14C. On the other hand, care is taken to ensure that the adsorbent 3 cannot exit the reactor 14 through the outlet opening 15A.
    CH 715 046 A2 The permissible expansion of the adsorbent 3 e.g. to the intermediate zone 14B or to the middle or to the upper end of the overhang zone 14C, can be individually determined and optimized with regard to the maximum throughput of purified liquid 2, 2B. 1b shows the expansion phase.
    Fig. 1c shows the device 1 of Fig. 1a in a second process phase or the rest phase ph2, in which the adsorbent 3 moves back by gravitational force towards the starting position. In the rest phase ph2, the volume flow Q of the liquid 2 supplied is shut off, greatly reduced or, if necessary, inverted. Thereby, the device 1 is returned to the initial state and prepared for the next loading phase ph 1.
    Optionally, the volume flow Q during the rest phase ph2 is only reduced to such an extent that there is hardly any rate of climb and therefore hardly any flow in the reactor 14. A remaining minimum volume flow Q prevents adsorption material 3 from entering the inlet opening 13 due to the water pressure and clogging the feed line to the reactor 14. For this reason, a filter is preferably provided at the inlet opening 13, which prevents the adsorbent 3 from entering. If the volume flow Q is only inverted for a short time, the adsorbent 3 is held in the reactor 14. In a particularly preferred embodiment, the liquid 2, 2A to be cleaned is fed to the inlet opening 13 via a siphon 130 (shown schematically in FIG. 1b). Adsorbent 3 escaping from the inlet opening 13 therefore only reaches a rising pipe of the siphon and falls back again.
    The interruption or the corresponding reduction in the addition of liquid ends the upward flow in the reactor 14. The rest phase ph2 is designed in time so that a substantial proportion or practically all of the adsorbent 3 in the liquid 2 now at rest can sink back into the contact zone 14C , The minimum period of the rest phase ph2 depends on the grain size of the adsorbent 3 and its specific weight. In the contact zone 14A, the adsorbent 3 is sedimented in the liquid 2 in a narrow space, so that it neither hovers nor floats but lies on itself as a bed. This high concentration of the adsorbent 3 causes micropollutants to hit an adsorbent body (e.g. an activated carbon piece) more quickly, to the surface of which the micropollutants are bound. This results in a high adsorption performance with rapid elimination of high amounts of micropollutants.
    After the adsorbent 3 has sunk and is now at rest in the contact zone 14A, there is only cleaned liquid 2, 2B or clear water without micropollutants and without adsorbent 3 in the supernatant zone 14C.
    Depending on the elimination rate to be achieved and the type of micropollutation, the liquid 2, 2A to be cleaned requires longer contact with the adsorbent 3, which is why the contact time is increased if necessary. The period of the loading phase ph1 is preferably in a range from a few seconds to a few minutes, e.g. between 1 second and 2 minutes. The period of the rest phase ph2 is preferably in a range from a few seconds to 10 minutes, e.g. between 1 sec and 10 minutes. As mentioned, the time periods are preferably variable, in particular in accordance with the state of the device 1 and the amount of the liquid 2 to be treated, optionally also taking into account the state of the adsorbent 3.
    The cleaned liquid 2 can be discharged from the reactor 14 in the feed phase ph1 and / or in the rest phase ph2 in various ways. As has been described, the cleaned liquid 2, 2B can be pressed out of the upper outlet opening 15A during the loading phase ph1, which is symbolized in FIG. 1b by an arrow.
    In the resting phase ph2, after all adsorbent 3 is sedimented, the cleaned liquid can advantageously be discharged from the reactor, just above the surface of the resting adsorbent 3, from the second outlet opening 15B, as is symbolized in FIG. 1c by an arrow , This has the advantage that less energy is required to allow the cleaned liquid 2 to flow out of the reactor 14 because it flows out of the reactor 14 in the free mirror. The period of the rest phase ph2 must be dimensioned in accordance with the height of the second outlet opening 15B so that the required sedimentation of the adsorbent 3 occurs. This operating mode is preferably selected when the water to be cleaned is sufficiently below the maximum dimensioning amount of the reactor 14 and there is sufficient time for the rest phase ph2.
    In further preferred embodiments, a retention device is provided in the protrusion zone 14C, preferably at the upper end below the outlet opening 15A, or a filter is provided which allows the liquid 2 to pass through, but which retains the adsorbent 3. In this way, the time span of the loading phase ph 1 and the volume flow Q of the cleaned liquid 2, 2B can be increased.
    Fig. 2a shows the device 1 of Fig. 1a in a preferred embodiment with a displaceable or deformable filter 6, which is shifted or deformed in the loading phase ph1 in the direction of the projection zone 14C. In this way, the movement of the adsorbent 3 is inhibited at an early stage. The concentration of the adsorbent 3 and thus the intensive interaction between the liquid 2 and the adsorbent 3 are retained for a longer period of time, which is why not only can the period of the charging phase ph 1 be advantageously extended, but at the same time an increased absorption capacity also occurs. FIG. 2a shows that the displacement or deformation of the filter 6, which occurs, for example, in the interior of the reactor 14
    CH 715 046 A2 installed ring flange 61 has already been carried out beyond the intermediate zone 14B into the overhang zone 14C.
    Fig. 2b shows the device 1 of Fig. 2a in the rest phase ph2, in which the filter 6 is displaced or deformed by a drive 62 or by gravity in the direction of the contact zone 14A, the adsorbent 3 in the direction of the starting position is pushed back. In the rest phase ph2, this has the advantage that the adsorbent 3 is returned to the starting position more quickly and the period of time for the rest phase ph2 can be shortened. The use of the filter 6 therefore gives advantages both in the loading phase ph 1 and in the rest phase ph2. The corresponding parameters, the time spans and volume flows are optimized accordingly.
    Guide rails oriented vertically or parallel to the longitudinal axis of the reactor 14 can also be provided on the inside of the reactor 14, along which a sieve or filter 6 can be displaced.
    3a shows the representation of a first process in the devices 1 of FIGS. 1a and 2a with two cyclically repeating process phases ph1, ph2 and volume flows Q1, Q21, -Q22 occurring therein. At time t1, the first cycle begins with a loading phase ph1, which ends at time t2. During the loading phase ph 1, a volume flow Q1 is set for the liquid 2, which is reset to the value Q21 or alternatively to Q20 at the time t2 at the beginning of the resting phase ph2. That is, no volume flow Q20 or only a minimum volume flow Q21 is maintained in the idle phase ph1. At time t3, the next cycle begins with a further loading phase ph1. The cycles are repeated as long as new liquid 2 to be cleaned is added. The time periods d ph i of the loading phase ph1 and the time periods d ph 2 of the rest phase ph2 are constant and are selected in accordance with the specifications described above. The bold solid line shows preferred parameters. The volume flow Q20 is at zero. The volume flow Q21 in the rest phases ph2 is at a constant value close to zero. The inflow of a small amount of liquid prevents liquid 2 with adsorbent 3 from flowing back through the inlet opening 13. Dash-dotted lines show that the volume flow in the rest phase ph2 can also be reduced to lower values or even inverted. With a negative volume flow -022, preferably close to zero or a fraction of the volume flow Q1 in the loading phase ph 1, the sedimentation of the adsorbent 3 is accelerated. In this case, the at least one inlet opening 13 is preferably provided with a filter which prevents adsorbent 3 from escaping. Even more advantageous is the arrangement of a siphon or a pipe bypass, which ensures that the returned adsorbent 3 is led into a riser in which it falls down due to gravity and at the latest at the beginning of the next charging phase ph1 neither into the reactor 14 or into a collecting container becomes. The siphon or riser can be used to dispense with the filter, which could become dirty.
    3b shows that the process parameters, in particular the volume flows in the loading phases ph1 and the rest phases ph2, the time periods d ph i, d P h2 of the loading phases ph1 and the rest phases ph2 as well as the connection of further process phases ph3 with corresponding process parameters dPh3 are preferably individually selectable and can be individually optimized. The control and optimization is carried out by means of sensors 18, the control unit 10, the actuators 62, valves 12, 16, pumps 11 and the control program 100, which processes the data and can preferably access a database 1000 (see FIG. 2a). Rules and empirical values are preferably stored in the database, which allow the processes to be optimized.
    Fig. 3b shows the representation of a second process flow in the devices 1 of Fig. 1a and Fig. 2a with two cyclically repeating process phases ph1, ph2 of constant length and volume flows occurring therein, which are individually controlled to optimize the process ,
    3c shows the representation of a third process course in the devices 1 from FIGS. 1a and 2a with three preferably cyclically repeating process phases ph1, ph2, ph3 and volume flows occurring therein. The time periods d ph i, d P h2 of the loading phases ph1 and the rest phases ph2 and the volume flows in the loading phases ph 1 are controlled as required. In addition, an intermediate phase ph3 is inserted after the loading phase ph1. In this intermediate phase ph'3, a small quantity of liquid 2 is preferably refluxed in order to accelerate the process of sedimentation of the adsorbent 3.
    Bibliography [0062] [1] “Micropollutants from municipal wastewater, process for extensive elimination in sewage treatment plants”, published by the Federal Office for the Environment FOEN, Bern 2012 [2] DE 2 410 007 A1 [3] WO 2006 013 235 A1 [4] WO 2014 184 371 A1 [5] AQUA & GAS, No. 7, 2017
    CH 715 046 A2
    权利要求:
    Claims (15)
    [1]
    claims
    1. A method for eliminating micropollutants in a liquid (2), such as waste water or drinking water, by adsorption on an adsorbent (3), preferably granulated activated carbon (GAK), in a reactor (14), which has one with at least one inlet opening (13 ) provided contact zone (14A), in which the adsorbent (3) is provided, and above the contact zone (14A) has a protruding zone (14C) with at least one outlet opening (15A, 15B) from which the liquid (2 ) emerges, characterized in that the liquid (2) which flows through the reactor (14) from the contact zone (14A) to the supernatant zone (14C) is conveyed through the reactor (14) in at least two process phases (ph1, ph2) , wherein in a loading phase (ph1) for a first time period (d ph i) the liquid (2) is introduced through the inlet opening (13) into the reactor (14) and in a rest phase (ph2) for a second time period ne (d P h2) the transfer of the liquid (2) through the inlet opening (13) is reduced, stopped and / or changed in the direction.
    [2]
    2. The method according to claim 1, characterized in that an intermediate phase (ph3) is provided between the loading phase (ph1) and the rest phase (ph2), in which the volume flow in its direction and intensity is preferably either controllable or fixed to a value.
    [3]
    3. The method according to claim 1 or 2, characterized in that the liquid is conveyed to the inlet opening (13) by means of a pre-pressure and optionally via an inlet valve (12) or by means of a feed pump (11) and optionally via an inlet valve (12).
    [4]
    4. The method according to claim 3, characterized in that the expansion of the adsorbent (3) to the protruding zone (14C) is monitored by means of at least one sensor (18A, 18B, 18C), the measurement signals of which are evaluated in a control unit (10), which, according to the evaluation, controls the feed pump (11) and / or the inlet valve (12) and / or an outlet valve (16A, 15B) connected to the outlet opening (15A, 15B) such that the adsorbent (3) exits through the outlet opening (15A, 15B) is prevented.
    [5]
    5. The method according to any one of claims 1 to 4, characterized in
    a) that the loading phase (ph1) and the rest phase (ph2) and, if applicable, subsequent process phases (ph3, ...) are cyclical; and or
    b) that the loading phase (ph1) and the rest phase (ph2) and, if applicable, subsequent process phases (ph3, ...) are cyclical and that the flow rate is preferably controlled individually in each process phase (ph1, ph2, ph3, ...) ; and or
    c) that the loading phase (ph1) and the rest phase (ph2) and, if applicable, subsequent process phases (ph3, ...) are cyclical and that the time spans (d ph i, d P h2, d ph3 ) of the loading phase (ph1) and the rest phase (ph2) and, if necessary, subsequent process phases (ph3, ...) are individually controlled; wherein the parameters of the loading phase (ph1) and / or the resting phase (ph3) are selected such that the adsorbent (3) does not reach the opened outlet opening (15A).
    [6]
    6. The method according to any one of claims 1 to 5, characterized in that the time period (d ph 2) of the rest phase (ph2) and / or the transfer of the liquid (2) through the inlet opening (13) during the rest phase (ph2) in this way are selected so that the adsorbent (3) after the end of the rest phase (ph2) is substantially below a rest level (rn), which is preferably monitored by means of a rest sensor (18D).
    [7]
    7. The method according to any one of claims 1 to 6, characterized in that the at least one outlet opening (15A) or at least one of a plurality of outlet openings (15A, 15B) is arranged at a level which during the loading phase (ph1) from the expanded adsorbent ( 3) or after the resting phase (ph2) is not reached by the stationary adsorbent (3), so that cleaned liquid (2) can flow through the outlet opening (15A; 15B) which is not reached by the adsorbent (3).
    [8]
    8. The method according to any one of claims 1 to 7, characterized in that the liquid (2) through the at least one inlet opening (13) or through several distributed inlet openings (13) with a uniform or individual, constant or variable flow rate in the reactor (14) is introduced that swirling of the adsorbent (3) results.
    [9]
    9. The method according to any one of claims 1 to 8, characterized in that in the reactor (14), preferably in the supernatant zone (14C) or in an intermediate zone (14B) between the contact zone (14A) and the supernatant zone (14C) is a stationary one A filter (6) or a displaceable or deformable filter (6) is arranged, which in the loading phase (ph 1) with the adsorbent (3) is shifted or deformed from a starting position towards an end position and during the rest phase (ph2) a drive (62) or by gravity is returned to the starting position.
    [10]
    10. Device (1) for eliminating micropollutants in a liquid (2), such as waste water or drinking water, by adsorption on an adsorbent (3)), preferably granulated activated carbon (GAK), according to the method according to one of claims 1 to 9, with a reactor (14) which has a contact zone (14A) provided with at least one inlet opening (13), in which the adsorbent (3) is provided, and above the contact zone (14A)
    CH 715 046 A2 has a protrusion zone (14C) with at least one outlet opening (15A, 15B) from which the liquid (2) freed from the micro-impurities can exit.
    [11]
    11. The device (1) according to claim 10, characterized in that a control unit (10) provided with a control program (100) is provided, by means of which a feed pump (11) connected to the inlet opening (13) and / or one connected to the inlet opening (13) connected inlet valve (12) is controllable and by means of which the transfer of the liquid (2) from the contact zone (14A) to the protrusion zone (14C) of the reactor (14) can be controlled in at least two process phases (ph1, ph2), that in a loading phase (ph1) for a first time period (d ph i) liquid .. (2) can be introduced into the reactor (14) through the inlet opening (13) and in a rest phase (ph2) for a second time period (d P h2 ) the transfer of the liquid (2) through the inlet opening (13) can be reduced, stopped and / or changed in the direction.
    [12]
    12. The device (1) according to claim 10 or 11, characterized in that the control unit (10) is connected to at least one sensor (18A, 18B, 18C), by means of which the expansion of the adsorbent (3) to the supernatant zone (14C) can be monitored and whose measurement signals can be evaluated by means of the control program (100), by means of which, according to the evaluation, the feed pump (11) and / or the inlet valve (12) and / or an outlet valve (16A, 15B) connected to the outlet opening (15A, 15B) ) are controllable in order to prevent the adsorbent (3) from entering the protruding zone (14C) and / or from the exit opening (15A, 15B).
    [13]
    13. The device (1) according to claim 10, 11 or 12, characterized in that the at least one outlet opening (15A) or at least one of a plurality of outlet openings (15A, 15B) is arranged at a level which during the loading phase (ph1) from expanded adsorbent (3) or after the resting phase (ph2) is not reached by the stationary adsorbent (3), so that cleaned liquid (2) can flow out through the outlet opening (15A; 15B) at the level not reached by the adsorbent (3).
    [14]
    14. Device according to one of claims 10 to 13, characterized in that liquid (2) through the one inlet openings (13) or through several distributed inlet openings (13) is introduced into the reactor (14) at a flow rate which is selected in this way that a swirling of the adsorbent (3) results and pulls it upwards.
    [15]
    15. Device according to one of claims 10 to 14, characterized in that a displaceable in the reactor (14), preferably in the protruding zone (14C) or in an intermediate zone (14B) lying between the contact zone (14A) and the protruding zone (14C) or deformable filter (6) is arranged, which in the loading phase (ph 1) with the adsorbent (3) is displaceable or deformable from a starting position in the direction of an end position and during the rest phase (ph2) by means of a drive (62) or gravity can be returned to the starting position.
    CH 715 046 A2

    CH 715 046 A2
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    同族专利:
    公开号 | 公开日
    CH715008A2|2019-11-29|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP3957608A1|2020-08-18|2022-02-23|David Meyer|Method and device for treating wastewater|
    法律状态:
    2021-04-15| AZW| Rejection (application)|
    优先权:
    申请号 | 申请日 | 专利标题
    CH6232018A|CH715008A2|2018-05-21|2018-05-21|Elimination of micropollutants in aqueous liquid on absorbent by interval water feed.|
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