HU205045B - Process and equipment for the biological-physical purification of sewages - Google Patents

Process and equipment for the biological-physical purification of sewages Download PDF

Info

Publication number
HU205045B
HU205045B HU884A HU488A HU205045B HU 205045 B HU205045 B HU 205045B HU 884 A HU884 A HU 884A HU 488 A HU488 A HU 488A HU 205045 B HU205045 B HU 205045B
Authority
HU
Hungary
Prior art keywords
aeration
sludge
flocculation
wastewater
minutes
Prior art date
Application number
HU884A
Other languages
Hungarian (hu)
Other versions
HUT57164A (en
Inventor
Tamas Bakos
Laszlo Balladas
Attila Garai
Otto Lukonits
Lajos Nagy
Sandor Nemeth
Lajos Polgar
Laszlo Szende
Original Assignee
Eszakdunantuli Regionalis Vizm
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Eszakdunantuli Regionalis Vizm filed Critical Eszakdunantuli Regionalis Vizm
Priority to HU884A priority Critical patent/HU205045B/en
Publication of HUT57164A publication Critical patent/HUT57164A/en
Publication of HU205045B publication Critical patent/HU205045B/en

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic processes
    • C02F3/12Activated sludge processes
    • C02F3/1205Particular type of activated sludge processes
    • C02F3/1221Particular type of activated sludge processes comprising treatment of the recirculated sludge
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic processes
    • C02F3/04Aerobic processes using trickle filters
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage

Abstract

In the process according to the invention, the waste water (effluent) - if necessary mechanically prepurified - is treated by biological trickling filter purication, if necessary aerated, flocculated and allowed to sediment, then the sedimented sludge or a part thereof - preferably mixed with waste water - with or without aeration is returned upstream of certain operations - with the exception of sedimentation - and the residual sludge and the purified water are discharged from the process. The process is characterised in that the flocculation is carried out, separately from the other operations with respect to time and place, up to a period of 5-30 minutes, preferably 15-20 minutes, at an average velocity gradient of 10-70 s<-1>, preferably 20-50 s<-1>, and furthermore the waste water and/or the sludge are/is aerated for a period of 5-40 minutes, preferably 10-15 minutes, based on the inflowing waste water rate. The process is characterised according to the invention in that it [lacuna] purifier (1) furnished with trickling filter, if necessary aeration and sludge aeration space (2, 5) and aeration apparatus (6.2, 6.5), settler (4), if necessary recirculation circuits (18, 17.1, 17.2) for the purified waste water and/or the sedimented sludge, and upstream of the settler... Original abstract incomplete. <IMAGE>

Description

BACKGROUND OF THE INVENTION The present invention relates to a process and apparatus for the biological-physical treatment of wastewater using a combination of drip, activated sludge and flocculation system.
For a long time, drip bodies dominated by wastewater treatment practices are increasingly being replaced by activated sludge systems. The reduction of drip bodies can be explained partly by the increase in the pollution of wastewater and partly by the stricter requirements for the quality of the discharged water. Drip bodies are not able to work with cleaning efficiencies for certain water quality categories at all times of the year. On the other hand, activated sludge systems can meet water quality requirements, but are much more expensive than drip systems in terms of both investment and operating costs. Recently, efforts have been made in two directions to develop procedures to improve water quality and reduce costs.
One direction considered the drip body as a starting point and wanted to improve the quality of the effluent water with activated sludge after-treatment. DD (PS) 216 228 discloses such a process for post-purification of water from a drip body. The solution is to pump mud from the bottom of the settler into the sedimentation inlet cylinder by means of a mammoth pump. As a result of the sludge recirculation and aeration, the settler creates a small activated sludge system that further purifies the treated wastewater discharged from the drip body.
The other trend was to reduce the size of the activated sludge system by using a drip solution as a pre-cleaner.
Attempts have been successful in both directions, and today there have been countless variations on combined systems. See the full review in Journal WPCF Volume 56, Volume 10, page 10731079.
A common feature of wastewater treatment on drip bodies is that when properly dimensioned or not overloaded, the dissolved water content of the treated water is low compared to the impurities present in colloidal and suspended solids. Because colloidal and suspended solids are generally not completely removed by sedimentation, the sedimented water from the purification system remains contaminated with colloidal and suspended solids. The effluent from the drip bodies is in direct contact with the biological membrane for a short period of time, usually only a few minutes, so that some of the colloidal and suspended solids cannot be trapped on the surface of the biofilm. With activated sludge cleaning solutions, wastewater will spend a longer period of time, usually from a few hours to 1-1.5 days, in the aeration basin. This time is sufficient for the colloidal and suspended solids content to be adsorbed, trapped, and biodegraded within the flake. Because these materials settle in the settler along with the sludge flakes, the water discharged from the settler therefore contains much less undissolved impurities than the dripping method. The operation of the combined drip-activated sludge biological purification system is based on the removal of all or part of the sewage sludge contaminant in the drip, while the removal of the colloidal and suspended solids is left to a activated sludge system. The variants differ in the cleaning ratio of the dripping body in the cleaning process.
In one of the basic cases of combined systems, a relatively large, multi-hour residence time activated sludge pool is pre-dripped. Because the drip body is heavily loaded, only a portion of the dissolved impurities are decomposed here, cleaning is essentially done in the activated sludge basin. The activated sludge from the settler is usually recirculated to the aeration basin. The disadvantage of this process is that it is advantageous for a limited amount and only for wastewater where a large proportion of the dissolved impurity is present. A further disadvantage is that it dismantles a large portion of the dissolved contamination in the aeration basin, whereby the development and operating costs due to the large volume pool and the aeration equipment are substantially lower than in the case of activated sludge systems.
In the other case of combined systems, the drip body system promotes the production of activated sludge flakes and thus improves the efficiency of the removal of undissolved impurities. The simplest option is to recirculate the settled sludge from the post-settler in front of the drip body. A common disadvantage of the solutions is that the drip bodies for activated sludge flakes cannot be optimized for efficient cleaning. The contact time between the recycled activated sludge flakes and the undissolved impurities is very small, so only a small proportion of the undissolved impurities can be removed.
In the third version of the combined solutions, the dissolved impurities are removed using a drip body. From there, the water enters an aeration basin where decomposition of any remaining contaminants takes place and the incorporation of colloidal and suspended impurities into the flakes begins, which is a prerequisite for their biodegradation. The sludge is recirculated from the settler either directly or via a sludge pre-aeration pool to the
EN 205 045 B into the steam pool. If the water discharged from the dripping body has a higher proportion of dissolved impurities, it is not necessary to pre-aeration the recirculating sludge. And if the undissolved dirt predominates, the aeration pool may be missed. The role of sludge pre-aeration is to increase the adsorption capacity of the sludge when aerobic when compared to non-pre-aeration sludge. A summary of these systems can be found in the June 1983 issue of WATER / Engineering & Manegement (pages 28-52).
The advantages of this variant are obvious over the previous ones. It decomposes most of the pollutant content of wastewater in a drip tray, which is advantageous mainly because of its operating cost. By choosing the size of the recirculation sludge pre-aeration and aeration basin, you can flexibly adapt to the properties of a wide variety of wastewater. The typical residence time of the pools ranges from a few minutes to an hour, which in turn has a very favorable effect on the investment costs and energy requirements of the activated sludge section. However, the drawbacks of the process compared to the activated sludge solution and the first version of the combined systems are that the colloidal mainly is not able to remove the suspended impurities to the same extent as those systems. This is because parallel processes in the aeration basin create conflicting requirements for the hydraulic conditions of the basin. The basin undergoes both a biodegradation and an adsorption process. (Note that for the purposes of the present invention, adsorption is the process by which the suspended solids and colloidal materials of sewage are incorporated into activated sludge flakes, either during growth of the flakes, merging, or at existing flakes. The biological load of the aeration basin is high. With a residence time of 5 hours and a water discharge from the dripping body of 2.4 g BOD / m 3 xd based on 50 g BOD 5 / m 3 impurity, approximately one and a half times the total biological purification of non-nitrifying activated sludge systems (MI-10127 / 5 The value specified by OVH technical guidelines is 1.8 kg ΒΌΙ5 / Π1 3 xd). As the biodegradation process requires the supply of oxygen, the amount of oxygen introduced into the unit volume should be increased proportionally. This is only possible by increasing the mechanical capacity of the aeration unit per unit volume, which increases faster than the amount of oxygen introduced per unit volume. Thus, dissipated energy per unit volume of the pool will be approximately 2 to 3 times that of a conventional activated sludge system with a typical value of 70 W / m 3 for surface aeration (MI-10 127/5 page 25). Based on this, the average velocity gradient can be calculated (Camp, TR: Flocculation and Flocculation Basins, San. Eng. Dir. 79 [1] 283 / 1-18, 1954), where:
ε: average value of energy dissipated per unit volume over time (W / m 3 ) μ: dynamic viscosity of the liquid (kg / mxs)
Experience has shown that in turbulent flows, the effective dissipated energy is 10-20% of the total dissipated energy, so instead of ε it is assumed to be 10-20%. The average velocity gradient of aeration basin hydraulic conditions with the above data:
G = 145-180s' !
This value is unfavorable for parallel adsorption processes, since experience shows that G = 1050 s' 1 is desirable for flocculation in non-biological systems. For aeration systems in activated sludge systems, this value is G = 30-100 s 1 (calculated from MI 10 12715) for surface aeration. Under these conditions, the small volume, high-load aeration basin breaks down the collapsible flakes, producing a large number of tiny flakes, which is detrimental to sedimentation. This phenomenon was also observed in the experiment described below.
This system cannot create optimal conditions for the two processes running in parallel. The average velocity gradient can only be reduced to an acceptable value for adsorption by increasing the volume of the aeration pool. The residence time is now over 1 hour, which would greatly reduce the benefits of the solution described.
Flocculation problems have been known to operators of such systems and there have been some attempts to solve them. It is commonly believed that the portion around the inlet of the Dora-type setters is removed from the settling chamber, the flow breaker plates, the plates removed, and the resulting mixing facilitates flocculation and thus improved adsorption. The disadvantage of this solution is that it remodels the most sensitive part of a wastewater treatment system, the post-settler, by changing its flow conditions, thereby impairing the efficiency of sedimentation. On the other hand, the space created in this way does not have the optimum conditions for the incorporation of colloidal and suspended materials into activated sludges, since they cannot control and control the resulting flow conditions. This solution is not applicable to overloaded wastewater treatment systems.
It is an object and object of the present invention to provide a method and apparatus which, while retaining the benefits of combined sewage treatment systems, namely, performs the greatest amount of biodegradation in a drip body and utilizes small, short-stay pools at the activated sludge, eliminates or significantly thus, it increases the adsorption capacity of activated sludge flakes, and promotes the removal of undissolved impurities
EN 205 045 Β better incorporation into activated sludge flakes and does not impair the settling efficiency of the post-setters. It is also an objective that the process is capable of increasing capacity and / or improving the quality of the effluent discharged in the case of overloaded systems, without the need for substantial modification of existing equipment or works of art.
The present invention is based on the recognition that the quality of the purified water is substantially influenced by both post-drip biodegradation processes and flocculation processes. If conditions are unfavorable for any of them, the quality of the purified water will deteriorate. In a small volume aeration pool with a short residence time of less than one hour, providing the oxygen demand of biological processes cannot simultaneously create the conditions for the reduction of undissolved impurities and the growth or stable survival of the resulting fine flakes. And if we create favorable conditions for flocculation, we cannot cover the oxygen demand of biological processes, thereby impairing the adsorption capacity of activated sludge flakes and thus indirectly flocculation. We have realized that the process of biodegradation and flocculation should not be carried out simultaneously but in succession.
By separating the process of biodegradation processes and the incorporation of undissolved impurities in activated sludge and further growth of flakes, the total volume of the pool compartments required for the purification process is significantly smaller than in a system where biological and flocculation processes occur in a single space, if the same requirements apply to running water. At equal volumes, the quality of the water discharged will be better in the system in which the processes are separated in space.
If the sewage sludge mixture is transferred to a pre-settling flocculator or flocculation chamber after a short aeration, and while maintaining the given adsorption capacity of the flakes, sufficiently favorable conditions can be created for meeting the undissolved impurities and the flakes. adsorption and further growth of the flakes. These conditions are significantly different from those prevailing in the aeration basin and are much more favorable than the flocculation conditions provided in the settler. It is essential in our process to provide optimum conditions for flocculation, both in terms of improving hydraulic conditions and enhancing the adsorption capacity of the flakes. Accordingly, the removal of undissolved impurities is most effectively enhanced not by increasing the residence time in the aeration pool, but by short-term aeration by treatment in a flocculator. It is further recognized that the mode of aeration also influences the adsorption capacity of the flakes. It is advantageous to use aeration devices, both for pre-aeration of the recirculating sludge and in the aeration pool, which mechanically work the flakes and mix them intimately with intense turbulence. Such an effect is preferably provided by the aerators acting on the injector principle.
In the process of the present invention, biological and physical treatment of wastewater is treated, if necessary mechanically pretreated, with biological dripping, aeration, flocculation and sedimentation, if desired, and then sludge, or a portion thereof, mixed with the effluent. except for sedimentation, any residual sludge and purified sewage are removed from the process. Typically, the flocculation is carried out separated from the other operations in space and time and with a mean velocity gradient of 5 to 30, preferably 15 to 20 minutes, and 10 to 70, preferably 20 to 50 s' 1 , and that the waste water and / or the sludge is aerated for a period of 5 to 40, preferably 1015 minutes, based on the amount of waste water entering.
The apparatus according to the invention is characterized by a drip pan cleaner, if necessary aeration and sludge aeration chamber and aeration device, as well as a settler, a recirculation circuit for the purified sewage and / or sedimented sludge, as well as a flocculating space arranged before the settler. The flocculating space has a mechanical agitator and / or aeration device and / or a sludge dispensing circuit.
It is typical that the biodegradable fraction of dissolved organic contamination is completely or nearly completely degraded by the drip cleaner, the decomposition of residual dissolved contamination in the aeration chamber and the incorporation and hydrolysis of a portion of the undissolved contaminant in the activated sludge flakes. almost all of the undissolved impurities are adsorbed by the flakes, hydrolysis continues, while in the sludge aeration space the aerosolization of the recirculated sludge takes place and the adsorption capacity is increased.
It is advantageous to maintain the adsorption capacity of the activated sludge flakes by mixing with or without the introduction of air in the flocculator. In a preferred embodiment of the process, the activated sludge wastewater mixture and / or the recirculating sludge is aerated by means of an injector element to increase the adsorption capacity of the sludge flakes.
A cleaning technology advantage is provided by recirculating a portion of the water from the drip body directly onto the drip body in the case of a plastic drip body filler, since the flushing threshold is essential for proper functioning of the drip body despite fluctuations in the amount of waste water discharged. The advantage of this direct recirculation is that it does not hydraulically load either the pre-settler or the post-settler, as opposed to the conventional small-loop or large-loop recirculation that hydraulically loads the post-settler or pre-settler.
HU 205 045 Β
The invention is exemplified! Embodiments and solutions thereof will be described in more detail on the basis of the accompanying drawings. Figure 1 is an exemplary embodiment of the process in which, after the drip cleaner, both dissolved and colloidal and floating impurities are removed. Figure 2 illustrates a variation of the process of biodegradation of dissolved impurities on a drip cleaner and the subsequent process step of decomposing undissolved impurities.
Figure 3 shows a variant where the incoming waste water is primarily of a high dissolved solids content and the main purpose is to remove it, of course, along with removing most of the undissolved contaminants.
The apparatus according to the invention will be described in detail with reference to FIG. For the biological and physical purification of mechanically treated wastewater (1), a drip pan cleaning, (2) aeration space, (3) flocculating space, (4) settling and (5) sludge aeration space are sequentially connected. An aeration unit (6.2) is provided in the aeration space (2), aeration device (3) in the flocculation space (6.3) and a mixer (7) in the aeration space (6.5). The apparatus also has two recirculation circuits, the recirculation circuit (18) for the waste water (12) leaving the dripping plant (1) and the recirculation circuit (16) for sludge (17.1-17.3) deposited in the settler (4).
The operation of the device according to the invention shown in Figure 1 is as follows. The wastewater (11) is mechanically cleaned, and the bulk of the dissolved contaminants is biodegraded through the dripping body (1). The cleaning efficiency of the unit is increased by returning a portion of the wastewater (12) treated in the unit to the drip cleaner (1) through the recirculation circuit (18) to compensate for hydraulic load fluctuations and to provide a flushing threshold. Most of the purified wastewater (12) enters the aeration space (2). The activated sludge flakes in the aeration space (2), recycled there, use the oxygen supplied by the aeration device (6.2) to biodegrade the remaining dissolved impurities. At the same time, part of the colloidal and suspended solids begins to be incorporated into the flakes, which is a prerequisite for starting the first phase of biodegradation of these substances. Due to the oxygen supply in the aeration space (2) and the avoidance of sedimentation, the hydrodynamic conditions are not optimal for the incorporation of colloidal and suspended solids, a well-flocculated pond. Therefore, this process will only be successful if the residence time is, as a rule, at least 3-4 hours. However, the residence time according to the invention can be significantly reduced by 0.1 to 1 hour if the biologically purified wastewater (13) flowing from the aeration space (2) into a flocculating space (3) separated from the other operations in space and time introduced. By means of the mixing device (7) and / or aeration device (6.3) provided here, the optimum conditions for flocculation are obtained, and thus almost complete incorporation of the colloidal and suspended solids is carried out for 5-30 min. between hours. Flocculation is made up of complex biological, chemical and physical sub-processes and requires special hydrodynamic conditions. the purified waste water (15) flows from the settler (4). The sedimented sludge (16) enters the sludge aeration space (5), whereby the aeration unit (6.5) enters an active, aerobic state which significantly increases the adsorption capacity of the sludge flakes. The pre-aerated sludge (17) enters the drip cleaner (1), the aeration space (2) and the flocculating space (3) via a recirculation circuit (17.1, 17.2 and 17.3).
It accelerates or renders the processes in the flocculation space (3) faster and more efficient when the aeration units (6.2 and 6.5) operate on any injection principle. Thus, while mechanically working the sludge flakes, they are in intimate contact with the supply air, thereby further increasing the activity and adsorption capacity of the flakes.
In the variant of the process shown in Figure 2, the biodegradation of the dissolved impurities on the drip cleaner (1) is achieved to such an extent that the aeration space (2) and the recirculation circuit (17.2) resulting from the previous version are not required.
In the variant of the process shown in Fig. 3, the natural activity of the sedimented sludge (16) of the settler (4) is also sufficient for the desired purification. This variant is used in wastewater where biodegradation of predominantly dissolved impurities is required. Thus, the sludge aeration space (5) described in the previous versions may be omitted. The sludge (16) enters the aeration space (2) and the drip pan (1) at the recirculation (16.2) and (16.1).
The process is also suitable for expanding the capacity of existing drip or activated sludge treatment plants and / or for improving the quality of the effluent water, leaving the existing artefacts in their function to supplement the artefacts required by the process according to the invention.
Advantages of the process of the invention have also been demonstrated by experiments conducted under laboratory and semi-industrial control conditions. It was advantageous for the experiment that the dewatering system and the activated sludge system operate in parallel at the Tatabánya wastewater treatment plant, in which the sewerage systems share a common manhole, thus treating the same quality wastewater. During the experiment, water from one of the drip bodies was sampled and divided into three equal portions. One sample was sedimented for 30 minutes without any treatment, then the upper clarified portion was aspirated and the resulting No. 1 sample was removed. sample was analyzed. This sample represented the purified wastewater of the drip body.
The sewage treatment plant is mentioned as activated sludge
The activated sludge was removed from the HU 205 045 Β system, separated from the waste water by filtration, and after washing and aeration for 30 minutes and repeated filtration was added to the second and third samples taken from the dripping body. The sludge concentration in the resulting mixture was about 1 g / l. The second sample was then aerated for 20 to 60 minutes and then sedimented for 30 minutes. After sedimentation, the upper, clean part was aspirated and the resultant No. 2 was removed. sample was analyzed. This sample represented the purified wastewater of the already known drip-activated sludge combined process. The third sample was flocculated with slow agitation for 10 to 20 minutes after aeration for 5 to 15 minutes, followed by settling for another 30 minutes. No. 3 removed after settling sample 3 is the purified water of the variant of the process of the invention described in FIG.
During the settling of the samples, the following were observed: In sample 1, large biofilm pieces detached from the drip body quickly settled. However, even after 30 minutes, the water was extremely cloudy and contained a large amount of tiny, non- or slightly sedimented suspended solids. No. 2 sedimentation in the sample was initially quite rapid, but later decelerated. The turbidity of the water had almost disappeared, but many of the tiny, left-over activated sludge flakes floated in the water. No. 3 In our sample, mud flakes of much larger size than number 2 were observed and their settling was fast. The turbidity of the water had disappeared and there was little, if any, flocculation, which had not settled, and there was little in the water.
Various aeration and flocculation times within the ranges given have hardly been modified in these experiences. No. 2 in the sample, the amount of flakes remaining on settling was slightly reduced when the aeration time was 30-60 minutes. No. 3 sample aeration! the increase in time did not produce a noticeable change, the residence time of 15-20 minutes was more favorable for flocculation with an average velocity gradient of G = 30-50 s 1 . Typical results are summarized in the following table:
No. 1 sample No. 2 sample No. 3 sample
aeration time (minutes) - 30 10
flocculation time (minutes) - - 20
settling time (minutes) 30 30 30
total COD,) 97 g / m 3 74 g / m 3 54 g / m 3
filtered COD d 64 g / m 3 39 g / m 3 30 g / m 3
The above specific results clearly prove that the, sufficiently efficient flocculation is carried out according to the present invention a key and significant, all relative to refocus (No.2. Sample) COD d was 27%, the filtered COD d value in turn of 23% water quality results in improvement.
The process according to the invention has the following main advantages.
1. The quality of the treated effluent discharged reaches a well-functioning activated sludge system.
2. Most of the biological treatment is done by a low-cost, low-energy drip cleaner, which reduces both operating costs and development costs compared to an activated sludge plant with the same capacity.
3. Recognizing the key role of the flocculation process, the introduction of a flocculation space may in some cases eliminate or significantly reduce the aeration pool of conventional systems. This may also be a significant factor in reducing the cost of development.
4. The purification process can be flexibly adapted to a wide variety of wastewater according to the ratio of dissolved to undissolved impurities.
5. Operational experience has shown that the present invention is relatively insensitive to shock loads.
6. The application of the present invention provides a simple, inexpensive and efficient method of extending the treatment capacity of existing waste water treatment plants and / or improving the quality of the treated waste water discharged.
7. Management tasks and knowledge do not represent a significant surplus over conventional and known systems.

Claims (6)

  1. A process for biological and physical purification of wastewater, comprising treating the wastewater, where necessary mechanically pretreated, with biological dripping, aeration, flocculation and settling, if desired, and then, if appropriate, mixing the sludge or sediment therefrom. with aeration, it is recycled to any of the operations except for sedimentation, and the remaining sludge and purified waste water are removed from the process, characterized in that the flocculation is separated from the other operations and for 5-30, preferably 15-20 minutes, , is preferably carried out at from 20 to 50 and one average velocity, and that the wastewater and / or sludge relative to the influent sewage volume of 5-40, preferably 10-15 aerated mins.
  2. 2. The process of claim 1, wherein the sedimented sludge is mixed with the effluent in an active aerobic condition.
  3. Method according to claim 1 or 2, characterized in that the fluid is moved mechanically and / or pneumatically during flocculation.
  4. 4. A method according to any one of claims 1 to 3, characterized in that it is aerated by means of an injector air inlet.
  5. 5. A method according to any one of claims 1 to 4,
    EN 205 045 Β characterized in that a portion of the biological dewatering effluent is returned to dispatch.
  6. 6. Apparatus according to claims 1-5. A process according to any one of claims 1 to 4, characterized in that it has a drip pan cleaner (1), if necessary aeration unit (6.2,6.5) of the aeration and / or sludge aeration unit (2,5), and also a settler (4), purified wastewater and / or the recirculation circuit for sedimented sludge as required (18, 17.1, 17.2), and. It has a flocculating space (3) located in front of the settler, which has 5 mechanical stirrers (7) and / or aeration device (6.3) and / or a sludge circulation circuit (17.3).
HU884A 1988-01-04 1988-01-04 Process and equipment for the biological-physical purification of sewages HU205045B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
HU884A HU205045B (en) 1988-01-04 1988-01-04 Process and equipment for the biological-physical purification of sewages

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
HU884A HU205045B (en) 1988-01-04 1988-01-04 Process and equipment for the biological-physical purification of sewages
DE19893900153 DE3900153A1 (en) 1988-01-04 1989-01-04 Process and apparatus for the biological and physical purification of waste waters

Publications (2)

Publication Number Publication Date
HUT57164A HUT57164A (en) 1991-11-28
HU205045B true HU205045B (en) 1992-03-30

Family

ID=10947438

Family Applications (1)

Application Number Title Priority Date Filing Date
HU884A HU205045B (en) 1988-01-04 1988-01-04 Process and equipment for the biological-physical purification of sewages

Country Status (2)

Country Link
DE (1) DE3900153A1 (en)
HU (1) HU205045B (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5316668A (en) * 1992-12-22 1994-05-31 Jet, Inc. Wastewater treatment plant and apparatus
US5484524A (en) * 1993-02-01 1996-01-16 Jet, Inc. Wastewater treatment apparatus
FR2789987B1 (en) * 1999-02-18 2001-04-20 Degremont IMPROVEMENTS IN THE TREATMENT OF RESIDUAL WATER BY ACTIVATED SLUDGE
CN106145405B (en) * 2014-11-27 2021-06-15 杜也兵 Connection method of maintenance module and filtering channel for control component of water purifier
CN109293169A (en) * 2018-11-22 2019-02-01 广东中迅新型材料有限公司 A kind of sewage disposal system

Also Published As

Publication number Publication date
DE3900153A1 (en) 1989-07-13
HUT57164A (en) 1991-11-28

Similar Documents

Publication Publication Date Title
US4073722A (en) Process for the purification of waste water
KR960013341B1 (en) Two-stage water treatment
US20070119763A1 (en) Floating sequencing batch reactor and method for wastewater treatment
CA2625798A1 (en) Water treating method and arrangement integrating a fixed-bacteria biological treatment and flocculation-decantation
US4721570A (en) RBC with solids contact zone
HU205045B (en) Process and equipment for the biological-physical purification of sewages
US2492486A (en) Separating solids from a liquid
KR100446141B1 (en) The waster water treatment system and method
SK24798A3 (en) Process for purifying waste water
KR20130022073A (en) Apparatus for wastewater treatment and method for phosphorus removal from wastewater
JPH02293093A (en) Sewage treating device by hollow-fiber membrane bundle
RU2060967C1 (en) Method and aggregate for deep biochemical sewage purification
KR100385417B1 (en) Apparatus for Advanced Treatment of BOD in Sewage and Dirty Water
KR0175710B1 (en) Sludge pressurized flotation device by pipeline type floc reinforcement device
JPH0661550B2 (en) Organic wastewater treatment method
KR100244536B1 (en) Device for removing high concentration of organism and nitrogen using biological membrane
KR20030048735A (en) A disposal method of food garbage drainage
KR0140185B1 (en) Bulking preventing waste water treatment equipment
KR100465908B1 (en) Method for processing livestock sewage without sludge
KR100239805B1 (en) Biofilter apparatus for treating waste water without backwashing using floating media
JPH06198295A (en) Biological treatment of organic sewage
KR910004128B1 (en) Concentrated organic waste water treating method
KR19980084220A (en) High concentration organic wastewater treatment method and apparatus
KR200257962Y1 (en) processing livestock sewage without sludge
KR200268478Y1 (en) wastewater disposal plant

Legal Events

Date Code Title Description
HMM4 Cancellation of final prot. due to non-payment of fee
HNF4 Restoration of lapsed final prot.
HPC4 Succession in title of patentee

Owner name: VITAQUA-MONT GYARTO, SZERELOE, KIVITELEZOE KFT., H

HMM4 Cancellation of final prot. due to non-payment of fee