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    • 专利摘要:
    WASTE WATER TREATMENT PROCESS, AND INSTALLATION TO PERFORM THE PROCESS A process for the biological treatment of waste water, in which the performance of a conventional activated sludge system is enhanced by the addition of an aerobic granular biomass system in a process configuration hybrid in parallel. Residual biomass and suspended material from the aerobic granular biomass system are introduced to the conventional activated sludge system for this purpose. In the hybrid process configuration, the advantages of both systems are combined to produce new advantages, while the disadvantages of the individual systems are reduced to the greatest extent.
    公开号:BR112014024671B1
    申请号:R112014024671-8
    申请日:2013-04-03
    公开日:2020-11-24
    发明作者:Tom Wil Theo Peeters
    申请人:Haskoningdhv Nederland B.V.；
    IPC主号:
    专利说明:

    [0001] [001] The invention relates to an improved wastewater treatment process using a sludge reactor activated in a hybrid process, including an aerobic granular biomass reactor. HISTORIC
    [0002] [002] In common practice, wastewater treatment plants (WWTPs) include a biological process step, in which part of the wastewater containing solid matter, organic materials and suspended and soluble nutrients, is treated with activated sludge (consisting mainly of microorganisms). This process can occur in an anaerobic or aerobic manner. The most widely applied process for aerobic wastewater treatment is called the 'conventional activated sludge' (CAS) process. It involves air and oxygen being introduced into a biological treatment reactor that contains a selected sewage mixture and, sometimes, treated in a primary way or biomass for industrial and residual water purification, also referred to as 'activated sludge'. Suspended solids of mixed residual liquid (MLSS) develop in a flake containing biomass, which typically grows in soft suspended aggregates. The subsequent sedimentation tank (commonly referred to as a "final clarifier") is used to allow the biological flakes to settle, thereby separating the purification sludge from the treated water. The established sludge is recycled to the biological process as 'activated return sludge' (RAS). To keep the biomass in the treatment reactor at a desired level during the growth of the biomass, part of the RAS is periodically wasted as 'residual activated sludge' (WAS).
    [0003] [003] The CAS process is applied to a variety of configurations, comprising one or multiple tanks in parallel or sequential treatment mechanism (s). These tanks can, for example, be operated as a piston flow reactor, as a continuous agitated tank reactor (CSTR) or as a sequential batch reactor (SBR). Although the CAS process is widely used, it has several important disadvantages, such as: poor mud settling characteristics, limitation to low concentrations of MLSS, the tendency to develop floating mud and a defined mud residence time. These disadvantages are described briefly below. BAD MUD SEDIMENTATION CHARACTERISTICS
    [0004] [004] Due to the flake-like structure, the sedimentation characteristics of the activated sludge are relatively poor, even when the plant is operating well. This results in the need for large final clarifiers and, similarly, high construction costs and a large plant footprint. Many improvements in the past, therefore, have focused on achieving improved separation techniques. One is the use of microfiltration to separate the activated sludge from the treated water in a Bio Membrane Reactor (MBR). Another is the addition of chemical components to improve the biomass sedimentation characteristics. In document W096 / 14912, a method is described, which improves the sedimentation properties of the activated sludge by extracting gas and creating a higher density of biomass. The method of selective sludge removal with poor sedimentation is described in EP1627854. LIMITATION TO LOW MLSS CONCENTRATIONS
    [0005] [005] The CAS process is limited to a relatively low concentration of MLSS, typically 3-5 g of MLSS / L. Higher concentrations of MLSS lead to an unfavorable prolonged slurry suspension in the final clarifiers and, especially, during conditions with higher than average hydraulic flows, for possible sludge elimination. Prior art measures to increase the MLSS level have focused on the application of microfiltration for sludge / water separation (Bio Membrane Reactors) rather than sedimentation or the use of submerged carrier material to improve biomass concentration, such as , described in WO03 / 068694. FLOATING MUD
    [0006] [006] The CAS process coincides with a periodic occurrence of fluctuation or of being very difficult to settle 'bulky mud', a phenomenon caused by an increased growth of filamentous microorganisms in the activated mud flakes. Typical counter-action measures include chemical oxidation to mainly destroy filamentous organisms or use of special biomass selection reactors before activated sludge, in which the growth of filamentous microorganisms is reduced. DEFINED ACTIVATED MUD RESIDENCE TIME
    [0007] [007] The CAS process for nutrient removal is typically designed with an activated sludge residence time set in the system of 5-15 days. This period of time establishes a limit for the accumulation of favorable species of microorganisms with low growth rates, which cannot be maintained in the treatment system. Measures to extend residence time include the Bio Membrane Reactor, the addition of submerged loaded material for attached growth and the use of bioaddition. In these bioaddition processes, a specific microorganism population is cultivated and usually immobilized in the bioaddition reactors. The reactors are fed with specific substrate or lateral streams of integrated waste from the wastewater treatment plant and then dosed to the CAS system, as described, for example, in document EP0562466. Another example of this in-situ bioaddition process is described in WO00 / 05177: it describes an external bioaddition reactor to enrich specific organisms in the activated sludge matrix.
    [0008] [008] The disadvantages of typical CAS systems are to overcome a large extent by the aerobic granular biomass (AGB) process and system, as developed by Delft University of Technology (WO2004 / 024638). In this process, granular biomass with a typical size of 0.2-3.0 mm is cultivated, which has very different characteristics from the flakes as they grow in CAS. For example, the sedimentation speed of the applied granules is in the range of 5.0-50.0 m / h (in comparison: typical for CAS would be 0.5-1.0 m / h). The sludge volume indices (SVI) for aerobic granular biomass are 70 ml / g or less and are typically comparable in value after 5 and 30 minutes of sedimentation time. In addition, MLSS concentrations can be maintained at levels 2-4 times higher than in CAS systems, resulting in approximately 2-4 times more 'purification potency'. In addition, the layered structure of granules in aerobic, anoxic and anaerobic zones and the variation in granule sizes results in an age distribution of mud. This allows specific, favorable microorganisms with low growth rates to survive in the AGB process.
    [0009] [009] However, a disadvantage of the AGB process is the fact that the granules need to be grown in a batch feed system, in batch sequencing reactors. It has been reported that AGB can only develop and be maintained in batch operations, during which slow growing microorganisms are selected in high feed concentrations, followed by a scarcity regime during non-feed conditions (see: WO2004 / 024638). These conditions cannot, by definition, be easily established in continuously powered CAS systems.
    [0010] [010] Therefore, the technology cannot be easily used to continually retrofit CAS power systems into systems that target AGB growth. The replacement of widely used continuous CAS systems would mean a large withdrawal of capital investment. Efforts to develop a continuously fed AGB system have been reported in the literature, but have so far proved to be unviable under practical conditions. Reference is made to a study on the formation and stability of aerobic granules in a continuous system: (N. Morales, et al., Separation and Purification Technology, volume 89, page 199-205, 2012). Efforts have also been made to replace activated sludge in continuous MBR systems with aerobic granular biomass in order to reduce membrane contamination. It was investigated whether the activated sludge in continuous MBR systems could be replaced by granular biomass grown in cultivation reactors or grown in granular biomass reactors. The results showed that it was not feasible to maintain aerobic granules in the MBR system: the granules deteriorated rapidly (Reference: Xiufen et al., Characteristics of Aerobic Biogranules from Membrane Bioreactor System, Journal of Membrane Science, 287, page 294-299, 2006 ). As a consequence, in the current technique, improving the performance of existing CAS systems using aerobic granular biomass is only possible by retrofitting CAS systems in AGB reactors operated in batch sequencing.
    [0011] [011] Even if, in a hypothetical case, granular biomass were able to survive in CAS, the size and sedimentation characteristics of the granules are such that, in many CAS, the mixing intensity is not sufficient and they will settle and, as such, will become inactive for the treatment process.
    [0012] [012] An assumed disadvantage of batch-operated systems, such as the AGB system, is the sensitivity to high oscillations in hydraulic loads outside specification. This is due to all operations taking place in a tank and feeding to a tank is discontinuous. This is different from CAS systems equipped with large final clarifiers, these clarifiers can act as a compensation tank to prevent loss of mud. This disadvantage can be counteracted by installing feed compensation tanks or adjusting feed patterns across multiple AGB process tanks.
    [0013] [013] JP-A 2009-090161 discloses an aerobic wastewater treatment comprising a series (not in parallel arrangement) of aeration tanks. Granular sludge sludge is produced in an oscillating bed with carrier material in the first aerated tank and fed to the second tank. JP-A 2007-136368 discloses an aerobic wastewater treatment in which the sludge is granulated in a contact tank and the sludge is then fed to a downstream reactor; Excess granular sludge from the aerobic reactor is returned to the contact tank. WO 2007/029509 discloses an aerobic wastewater treatment process with sludge return, using a partitioned aerated tank and immobilized microorganisms in a loader in the first compartment. SUMMARY OF THE INVENTION
    [0014] [014] It was surprisingly found that the deficiencies and disadvantages of prior art processes could be overcome by adding an AGB system to a CAS system and manipulating the mud flows from the AGB system. The resulting interconnected hybrid process considerably improves the performance and flexibility of prior art wastewater treatment plants.
    [0015] [015] The invention, therefore, comprises an innovative process for biological treatment of wastewater, in which the performance of CAS systems is improved. The addition of one or more AGB reactors serves two purposes: 1) to treat part of the raw waste water and, in doing so, contribute to the overall treatment performance of the general hybrid treatment plant and 2) in doing so, to improve synergistically the performance of the existing CAS, without adding chemical components, without a complete retrofit of the CAS system for sequential batch operation, without using degassing measures or using membranes, without using submerged biomass support material and without bioaddition with special microorganisms grown or immobilized produced by external substrate. Also, hydraulic load fluctuations can be accommodated, while maintaining effective waste treatment. BRIEF DESCRIPTION OF THE DRAWINGS
    [0016] [016] In the attached drawings:
    [0017] [017] Figure 1 schematically depicts a hybrid wastewater treatment process equipment of the invention;
    [0018] [018] Figure 2 schematically depicts a variation of the hybrid wastewater treatment process of the invention, as operated in an initialization stage;
    [0019] [019] Figure 3 schematically depicts another variation of the hybrid wastewater treatment process of the invention comprising a waste sludge processing unit;
    [0020] [020] Figure 4 schematically depicts a reactor to be used for the aerobic granular process of the invention. DETAILED DESCRIPTION OF THE INVENTION
    [0021] [021] The invention therefore provides a waste water treatment process comprising subjecting a portion of the waste water supply to an activated sludge process using aerobic flake-type biomass, and feeding part of the waste water to a process of granular biomass using aerobic granular biomass, in which part of the biomass, that is, the residual biomass and suspended solids, emitted from the granular biomass process, is fed into the activated sludge process.
    [0022] [022] The activated sludge process (CAS system) and the granular biomass process (AGB reactors) are carried out in parallel, which means that the main flow of residual water is divided into a flow subject to the CAS system and a flow subject to the AGB reactor (s), and the divided flows are not substantially intermixed during the treatment process, other than in small quantities that accompany the transfer of biomass from the AGB system to the CAS system. The parallel configuration is described in more detail below. The biomass part of the granular biomass process that is fed to the activated sludge process, that is, the suspended solids, is especially the lightest part of the biomass, that is, the part that has smaller particle sizes and / or a lower settling speed (in particular, lower settling speed) than the part that is not fed to the CAS system, that is, it remains in the AGB reactor. The excess granular biomass of AGB reactors is preferably not fed to the CAS system, but will be processed or reused outside the process. Excess sludge from the CAS system is preferably not fed to the granular biomass process.
    [0023] [023] As used herein, aerobic granular biomass (AGB), to be used in the granular biomass process, and flake-type aerobic biomass, to be used in the conventional activated sludge process (CAS), are distinguished by one or more features:
    [0024] [024] (1) mud volume index (SVI30), defined as the volume in millimeters occupied by 1 g of a suspension after 30 min. sedimentation: aerobic granular biomass has an SVI30 which is less than 70 ml / g, preferably less than 60 ml / g, more preferably less than 50 ml / g, more preferably less than 40 ml / g; whereas aerobic flake-type biomass typically has an SVI30 of more than 70 ml / g, particularly more than 80 ml / g, more in particular, between 90 and 150 ml / g; a sludge biomass, as used here, can therefore be referred to as granular, if the SVI30 is less than 70 ml / g, and as a flake, if the SVI30 is greater than 70 ml / g. In addition, the corresponding SVI after 5 minutes of sedimentation, referred to as SVI5 for aerobic granular biomass is less than 150 ml / g, preferably less than 100 ml / g, more preferably less than 70 ml / g, more preferably, less that 60 ml / g; while aerobic flake-type biomass has an SVI5 of more than 150 ml / g, typically more than 250 ml / g. A sludge biomass, as used here, can therefore, alternatively or additionally, be mentioned as granular, if the SVI5 is less than 150 ml / g, and as a flake, if the SVI5 is greater than 250 ml / g.
    [0025] [025] (2) sedimentation speed, defined as the height of sludge settled per hour: aerobic granular biomass has a sedimentation speed of at least 3 m / h, preferably at least 4 m / h, more preferably between 10 and 50 m / h, while aerobic biomass of the flake type has a sedimentation speed of less than 3 m / h, particularly less than 2 m / h, more particularly, between 0.5 and 1.5 m / h ; a sludge biomass, as used here, can therefore be mentioned as granular, if the sedimentation speed is greater than 3 m / h, and as a flake, if the sedimentation speed is less than 3 m / h.
    [0026] [026] (3) average particle size: aerobic granular biomass comprises different particles that, after mechanical sieving in the laboratory, under light water washing, have an average particle size of at least 0.2 mm, preferably between 0 , 4 and 3 mm, while flake-type aerobic biomass agglomerates during mechanical sieving in the laboratory, under light water washing, has an average particle size of less than 0.2 mm, particularly less than 0.1 mm; a sludge biomass, as used here, therefore, can be mentioned as granular, if the average particle size of the sludge is greater than 0.2 mm, and as a flake, if the average particle size of the sludge is less than 0, 2 mm.
    [0027] [027] The part of the biomass emitting from the granular biomass process that is fed to the activated sludge process, typically, has characteristics that are intermediate between the characteristics of the aerobic granular biomass and the aerobic flake-type biomass, as defined above. Thus, the part of the biomass transferred from the AGB reactor (s) to the CAS system will have a sludge volume index (SVI30), as defined above, between 40 and 90 ml / g, especially between 50 and 90 ml / g, and an SVI5 between 70 and 250 ml / g, especially between 150 and 250 ml / g. Likewise, the part of the biomass transferred from the AGB reactor (s) to the CAS system will have a sedimentation speed between 1.5 and 10 m / h, especially between 3 and 10 m / h. In addition or alternatively, the part of the biomass transferred from the AGB reactor (s) to the CAS system will have an average particle size between 0.1 and 0.4 mm.
    [0028] [028] In an advantageous embodiment, the activated sludge process of the hybrid process of the invention is operated in a conventional continuous mode, in which the effluent from the activated sludge reactor is fed continuously to a clarifier, in which the effluent is separated into a liquid. clarified and a fraction of mud. The clarified liquid is preferably combined with the treated water from the emission of the granular biomass process, when desired, with additional post-treatments. Part of the undissolved material (ie, the sludge fraction) separated from the clarifier is returned to the activated sludge process and part can be discharged or further treated, as described below. Alternative embodiments, such as using a sequential batch reactor, without a final clarifier are also part of the invention.
    [0029] [029] The granular biomass process of the hybrid process of the invention is advantageously operated by batch. The granular process can be operated by alternating steps, as also described in WO2004 / 024638, as follows: (a) adding residual water to the aerobic granular biomass in a reactor, while discharging treated water from the reactor, (b) supply of oxygen-containing gas, in particular air, to the waste water added to the reactor, while maintaining the oxygen level in the waste water in the reactor between 0.2 and 5 mg / l, preferably between 0.4 and 4 mg / l, more preferably, between 1 and 3 mg / l, (c) allowing the granular biomass to settle, and (d) discharging part of the biomass (suspended solids: MLSS) from the reactor; and then return to step (a). At least part of this discharged biomass is fed to the activated sludge process. The process step (d), that is, the discharge of part of the suspended solids, does not need to be included in each and every process cycle, depending on the relative sludge requirements of the activated sludge process and the granular process. For example, step (d) can be included every second or third, etc. cycle.
    [0030] [030] Instead of discharging treated water in step (a), that is, at the same time, as raw waste water supply to the reactor, the treated water can be discharged together with the discharge of the biomass part of the reactor in step (d ), that is, before the feeding step (a) which follows step (d). In this case, treated water and biomass can be fed to the activated sludge process. This is particularly useful when booting the system.
    [0031] [031] An important aspect of the present process is that the average particle size and / or sedimentation rate of the biomass (suspended solids) that is removed from the aerobic granular process and can be fed to the activated sludge process is less than the size of mean particle and / or sedimentation speed of the aerobic granular biomass remaining in the aerobic granular reactor. However, the transferred biomass will have a larger particle size and / or settling speed greater than the average particle size and / or settling speed of the sludge in the activated sludge process, as explained above, and improves the sludge process performance. activated.
    [0032] [032] The granular biomass process is operated in an upward flow mode, in which the residual water, in step (a), is supplied from the bottom and displaces the treated water in the upper part of the reactor upwards. The oxygen-containing gas is supplied in step (b) at the bottom of the reactor, not earlier than after the supply of fresh waste water. In step (c), the suspended matter, partially comprising precursors of granular biomass, smaller granular biomass and bio-agglomerates with lower sedimentation speed, is discharged between 30 and 90% of the reactor height, measured from the bottom to the top, as biomass larger excess granular can be removed periodically from the process of the bottom part of the reactor. Additional details can be seen in Figure 4 described below. Thus, two types of biomass can be discharged from the aerobic granular process: first, the suspended solids, that is, the relatively light, small size and slow settling part of the granular biomass, which is often wasted by at least 30% the height of the reactor, the bottom and, secondly, the heavy granular biomass, which can be wasted at a lower frequency from the bottom of the reactor.
    [0033] [033] In a preferred process configuration, shown in Figure 1, an AGB reactor (4) is constructed and linked to the existing CAS reactor (3), so that it is parallel to the CAS reactor, the AGB reactor it is fed with part (2) of raw inlet or pre-treated waste water (1), while the suspended waste material from aerobic granular biomass reactors (10) is fed frequently to the CAS system (3 + 5) and results gradually in capacity and improved purification skills of the CAS process. In Figure 1, (5) depicts the final clarifier, continuously fed (6) by the excess flow from the CAS reactor, while (7) depicts the mud return flow, divided into RAS (8) and WAS (9). The AGB effluent (12) is obtained directly from the effluent (13) of the final clarifier, for direct discharge or tertiary treatment. Larger and fully grown surplus granules are periodically wasted from the AGB reactor (11). The new AGB reactor (s) can be constructed by adding new tanks or by retrofitting part of the existing CAS reactor (s) or compartments thereof or by retrofit existing tanks or clarifiers.
    [0034] [034] The proportion of the part of the waste water fed to the granular biomass process and the part of the waste water fed to the activated sludge process can be controlled, depending on the quality of the waste water. More typically, the ratio of AGB flow and CAS flow is selected between 5:95 and 75:25, particularly between 10:90 and 50:50. In this way, the process configuration of the invention can be used to reduce one of the disadvantages of batch feed AGB, the challenge being the handling of large oscillations in the hydraulic load, with greater proportions between storm flows and dry weather, as they occur in areas with combined health systems. For example, during storm water flow conditions, when the residual water is abundant and relatively diluted, most of the hydraulic load can be fed to the CAS system of continuous feed and treated with the help of the final clarifier, while the hydraulic load to the AGB system is increased only discretely. On the other hand, a relatively high proportion of the residual water can be fed to the granular biomass process in the case of smaller volumes of relatively concentrated residual water, as can occur under dry weather conditions. In particular circumstances, the residual water can be fed exclusively to the activated sludge process or to the granular process. This process configuration can significantly reduce the AGB tank volume or rainwater compensation tank volume and save the overall construction cost.
    [0035] [035] In principle, any residual water that is not excessively toxic to the biomass used can be treated by the process of the invention. For example, wastewater may contain organic waste at a level between 10 mg and 8 g expressed as COD by 1, in particular between 50 mg and 2 g COD by 1. Alternatively or additionally, waste water may contain total nitrogen (such as ammonia and / or other nitrogen compounds) at a level between 0.2 and 1000, particularly between 1 and 75 mg per 1 (as nitrogen), which will result in at least partial nitrogen removal, as explained below. Also, wastewater may contain total phosphorus (such as phosphate and / or other phosphorus compounds) between 0.05 and 500, particularly between 1 and 15 mg per 1 (as phosphorus).
    [0036] [036] The process configuration mentioned above can be applied in a favorable way to increase the overall capacity of WWTPs to operate with CAS systems. In this process configuration, one or more new AGB reactors are built in a parallel treatment mechanism, close to the existing CAS systems. The existing CAS systems are fed with a large part of the raw or pre-treated waste water, but a remaining part is treated by the AGB systems. In doing so, the size and capacity of the AGB treatment mechanism for the projected extension may become smaller, as the capacity and performance of existing CAS systems is increased synergistically. However, the small occupation area of the AGB system generally allows it to be built as an extension of the plant's capacity close to the existing CAS system (s) on the same premises, which is important when the area of occupation for plant expansion is limited or costly.
    [0037] [037] Thus, the activated sludge process, that is, the CAS system, can comprise two, three, four or more treatment mechanisms executed in parallel. The CAS effluent from the combined CAS reactors can be fed to a single clarifier or, alternatively, each CAS reactor can be provided with its own clarifier. Preferably, each of the multiple CAS reactors that run in parallel is fed with biomass from the aerobic granular process, although the biomass feed does not need to be identical or continuous with each activated sludge reactor. When multiple CAS reactors are used, the granular biomass process can comprise a treatment mechanism or, alternatively, multiple granular treatment units. It is also conceivable that the process comprises a single CAS system and two, three or more aerobic granular mechanisms.
    [0038] [038] The hybrid configuration of AGB and CAS in parallel has an additional advantage in that the additional compensation tank is generally needed to balance the discontinuous residual flow from the AGB reactor to allow continuous thickening and dewatering of sludge with reduced equipment capacities. By applying the innovative process configuration of this invention, all of the wasted biomass and other suspended material from the AGB reactor can be fed batchwise into the parallel CAS system and further processed continuously with the activated sludge in the sludge treatment facilities. of CAS.
    [0039] [039] The unexpected advantages of the invention have been tested and demonstrated. An AGB reactor was built to replace an existing CAS system and to accommodate the necessary increased capacity and purification performance of the existing WWTP. The AGB system was operated in parallel to the CAS system, as shown in Figure 2. The clean effluent from the AGB system (12) was temporarily sent to the final clarifier of the CAS system. The residue from the AGB system (10), containing suspended matter comprising precursors of partially granular biomass, smaller granular biomass and bio-agglomerates, was also temporarily wasted on the existing CAS system, which was operating in parallel to AGB. The residual material from the AGB system (4) was transferred gradually through (11-6-5-7-8) to the CAS system (3 + 5). This was done as a temporary measure to compensate for the reduced nutrient removal efficiency of the AGB system during startup. Then, it was surprisingly found that the performance and process stability of the CAS system improved gradually, but significantly as a result of this interaction with the AGB system. This improvement also developed over time when the discharge of residual material no longer proceeds through (11), but directly to the CAS system (3) and the effluent was discharged directly to (12), after the final clarifier (5 ), as shown in Figure 1.
    [0040] [040] As described above, the residual sludge material (suspended solids) from the granular biomass process is directed to the activated sludge process. Also, liquid effluent from the granular biomass process can be discontinuously directed to the activated sludge process.
    [0041] [041] Prior to the start-up of the new AGB reactor, the sludge volume indices (DSVI30) in the CAS system were 125-175 mL / g and dropped significantly to 75-100 mL / g without any changes made to the CAS system. As a result, the biomass concentration in the CAS system could be increased from 3-4 g MLSS / L to 4-5 g MLSS / L, without affecting the level of suspended solids in its effluent. Clearly, the residual biomass from the AGB system was captured largely in the CAS system, to its advantage. In addition, the total residual biomass concentration in the CAS system increased from 8 g MLSS / L to 12 g MLSS / L, in a reduced hydraulic flow towards the sludge treatment facilities.
    [0042] [042] Surprisingly, it was found that the population of microorganisms in the CAS system has become more diverse and has also significantly qualified more specialized and slower-growing microorganisms than before. The biomass of the CAS system still maintains its flake-like structure, but it becomes more dense with the small residual granular biomass inclusions, resulting in improved purification and settlement capacity. Also, it was measured that the concentration of biopolymers and extracellular polymer substances in the CAS system biomass increased significantly. In addition to these findings, the existing high-load, fully aerated CAS system showed a greatly improved capacity for denitrification. A remarkable finding, due to this high rate of denitrification, would be impossible based on the prevailing aerobic conditions and age of mud in the CAS system. The tests showed NO3-N effluent concentration decreasing from 8-10 g of NO3-N / L to 3-4 g of NO3-N / L.
    [0043] [043] The particulate matter in the residual effluent from the AGB system will displace part of the activated sludge in the CAS system. This residual AGB material (suspended solids) contains fractions of fine aerobic granules, granule strikers, bio-agglomerates and granule fractions, resulting from the breakdown of larger (and older) granules. As mentioned, AGB and parts thereof contain a population of highly diverse microorganisms, including specialized and favorable slow-growing microorganisms. Surprisingly, it was found that the physical characteristics of this residual particulate AGB material do not deteriorate in the CAS system and the material does not lose its denitrification capacity either, as is typical for larger granules.
    [0044] [044] In another process configuration, the synergistic effect of operating an AGB system in the hybrid configuration with a CAS system can be used advantageously to efficiently remove nitrogen components from wastewater. The enhanced capabilities of AGB systems are used to remove high levels of nitrogenous compounds from wastewater. In this process configuration, as shown in Figure 3, the AGB system (4) is (partially) fed by a lateral flow (16) of the CAS system (3 + 5) containing high levels of nitrogenous compounds, for example, which originate from a waste sludge processing unit (14). Most of these lateral flows are small in volume, but high in concentrations of nutrients (nitrogen, phosphorus compounds) compared to the influential (1), which can be treated by AGB. Examples of these lateral flows are: rejection of water from dewatering devices, decantation of water from digesters, water from anoxic selection tanks and mixtures of these flows with the influential. The effluent from the AGB system (12), together with its material and / or suspended residual biomass (10), is directed to the CAS system. This hybrid process configuration of AGB / CAS systems provides another example of the positive effect of adding an AGB system to a CAS system on the overall performance of WWTP.
    [0045] [045] Surprisingly, it was found that the invention also provides a cost-efficient solution for improving the biological phosphorus (P) removal capacity of an existing CAS system, equipped with chemical component P. removal. conventional biological P removal in CAS systems, anaerobic preconditioning of the activated sludge is necessary to obtain P released, first, before increased P intake can occur in the CAS system, under subsequent anoxic / aerobic conditions. As is known from WO 2004/024638, AGB systems increased the increased biological P removal capabilities, related to the proliferation of Phosphate Accumulation Organisms (PAOs) in the aerobic / anoxic coated granule. Also, it is known that due to pH profiles in the granule, precipitation of biocatalysed phosphate can occur, improving the P removal capacity of the AGB system.
    [0046] [046] The invention can be used to add biological phosphate removal capability to an existing WWTP system and combines it with CAS biomass sedimentation characteristics, as explained above. However, it was found that the overall biological P removal capacity of the hybrid AGB / CAS systems was much greater than could be calculated based on the sum of the two combined processes. A significant reduction in the need for chemical dosage for P precipitation in CAS was observed, resulting in a much lower, favorable chemical sludge production. Again, it was presented that the AGB residue directed to the CAS system resulted in the replacement or union of CAS biomass flakes with small granular biomass from the AGB system. This particulate matter also characterized the ability to remove good biological P under aerobic conditions in the CAS system. The invention allows the ability to remove additional biological P to be introduced into the CAS system, without the elaborate construction of separate anoxic and anaerobic compartments in the CAS system and with chemical P removal in the CAS system becoming less important or even superfluous.
    [0047] [047] The invention can also be used to optimize the performance of a CAS system that treats mixtures of waste water, including low molecular weight organic components. These compounds usually result in bulk sludge by filamentous microorganisms, which are difficult to settle. A selector tank, as the first step in the biological treatment process, is commonly used to minimize this problem. In these selector tanks, these components are partially biodegraded selectively. It was found that when this waste water or part of the waste water was treated in the AGB system that operates in parallel to the CAS system, part of the low weight organic components was biodegraded by AGB in anaerobic zones of the granules. This results in lower energy consumption for aeration and the production of biogas, which could be captured and used. In particular, it was highly notable that the anaerobic degradation of minor alcohol compounds, such as methanol and ethanol, was measured, since these compounds in traditional anaerobic reactors are converted hard at all times. In addition, it was observed that this remarkable anaerobic treatment capacity was transferred from the AGB system to the CAS system in the hybrid CAS / AGB configuration. In conclusion: another configuration of the invention is the operation of an AGB system in parallel to a CAS system, in order to improve the sedimentation characteristics of the sludge, while at the same time reducing the time of the required aeration capacity in the general WWTP .
    [0048] [048] The operation of the aerobic granular process is illustrated schematically in Figure 4, showing an aerobic granular reactor 4. The reactor is operated in an upflow mode comprising a lower bed 40 containing the larger granular biomass, and a portion upper 41 containing suspended matter partially comprising precursors of granular biomass, smaller granular biomass and smaller bio-agglomerates. Residual water 2 and, optionally, the side flow 16, is introduced at the bottom, through inlet means 42. Air is introduced through inlet 43 at the bottom with distribution means (not shown), and the spent air leaves the reactor at top. Clean effluent 12 leaves the reactor through the overflow and outlet 45. The excess material 10, having an average particle size, which is less than the average particle size of the granular biomass in the reactor, can be discharged through outlet 46, which is located somewhere between 30 and 90 the height (net) of the reactor. Larger excess granular biomass 11 can be removed via outlet 44. Inlet 42 and 43 and outlets 44, 45 and 46 are preferably provided with a valve to control the inflow and outflow of the various flows. In particular, air supply and distribution means 43 are provided with a flow regulator controlled by the oxygen level in the reactor content, in order to maintain an oxygen concentration in the reactor content within the necessary limits, that is, 0, 2-5 mg / l, for producing ideal granular biomass characteristics.
    [0049] [049] In an additional advantageous process, the hybrid configuration of CAS and AGB systems is applied to the target granulation in the AGB instead of the waste water treatment. The surplus produced from cultured granules can be collected as valuable residual biomass and sold as seed material for new AGB systems.
    [0050] [050] The invention also comprises equipment for implementing the hybrid process configuration with AGB and CAS systems, as described. This equipment advantageously comprises an activated sludge reactor (3) with a liquid inlet, a liquid outlet, a gas inlet, a granular biomass reactor (4) with a liquid inlet (42) at the bottom of the reactor and a liquid outlet (45) at the top of the reactor and an outlet (46) at least a third of the height of the reactor (4), a gas inlet (43) at the bottom of the reactor, a liquid channel that connects a output from the granular biomass reactor (4) to an activated sludge reactor inlet (3) and, preferably, a separator (5) connected to an activated sludge reactor liquid outlet (3), the separator having an sludge and a clarified liquid outlet, and further comprising a control valve to regulate the relative liquid flows for the liquid inlet of the activated sludge reactor (3) and the liquid inlet of the granular biomass reactor (4). The equipment can comprise multiple activated sludge reactors (3) and / or multiple granular biomass reactors (4) arranged in parallel.
    权利要求:
    Claims (14)
    [0001]
    WASTE WATER TREATMENT PROCESS, comprising dividing a main stream of residual water into (i) a first stream of residual water subjected to an activated sludge process using aerobic flake biomass, and (ii) a second stream of residual water which is fed to a granular biomass process operated in parallel to the activated sludge process and using aerobic granular biomass, in which part of the biomass emitting from the granular biomass process is fed to the activated sludge process, in which the part of the biomass fed the activated sludge process has a lower sedimentation speed than the part of the biomass of the granular biomass process that is not fed to the activated sludge process, in which the aerobic granular biomass is characterized by one or more of the following characteristics: an index of mud volume, defined as the volume in millimeters occupied by 1 g of a suspension after 30 min of sedimentation less than 70 ml / g; a sedimentation speed of at least 3 m / h; and an average particle size of at least 0.2 mm, and where the part of the biomass emitting from the granular biomass process that is fed to the activated sludge has one or more of the following characteristics: a sludge volume index, defined as the volume in millimeters occupied by 1 g of a suspension after 30 min of sedimentation between 40 and 90 ml / g; a sedimentation speed between 1.5 and 10 m / h; and an average particle size between 0.1 and 0.4 mm.
    [0002]
    PROCESS, according to claim 1, in which the aerobic biomass of the flake type is characterized by having one or more of the following characteristics: a sludge volume index, defined as the volume in millimeters occupied by 1 g of a suspension after 30 min of sedimentation, of more than 70 ml / g; a sedimentation speed of less than 3 m / h; and an average particle size of less than 0.2 mm.
    [0003]
    PROCESS, according to either of claims 1 or 2, in which aerobic granular biomass is characterized by having a sludge volume index, defined as the volume in millimeters, occupied by 1 g of a suspension after 5 min of sedimentation, less than 150 ml / g.
    [0004]
    PROCESS according to any one of claims 1 to 3, in which the aerobic biomass of the flake type is characterized by a sludge volume index, defined as the volume in millimeters occupied by 1 g of a suspension after 5 min of sedimentation, greater than 250 ml / g.
    [0005]
    PROCESS according to any one of claims 1 to 4, characterized in that the granular biomass process comprises the consecutive steps of (a) adding residual water to the aerobic granular biomass in a reactor, while discharging treated water from the reactor, (b) supply of oxygen-containing gas to the reactor, while maintaining the oxygen level in the waste water in the reactor between 0.2 and 5 mg / l, (c) allowing the granular biomass to settle and (d) collecting part of the biomass from the reactor and, at least partially, feeding this to the activated sludge process, in which the average particle size of the biomass that is collected is smaller than the average particle size of the biomass remaining in the reactor.
    [0006]
    PROCESS according to any one of claims 1 to 5, characterized in that the granular biomass process is operated by the consecutive steps of (a) adding residual water to the aerobic granular biomass in a reactor, (b) supply of oxygen-containing gas to the reactor , while maintaining the oxygen level in the waste water in the reactor between 0.2 and 5 mg / l, (c) allowing the granular biomass to settle and (d) discharging the treated water from the reactor comprising collecting part of the reactor's biomass and , at least partially, feeding it to the activated sludge process, in which the average particle size of the biomass that is collected is smaller than the average particle size of the biomass remaining in the reactor.
    [0007]
    PROCESS, according to claim 6, characterized in that the granular biomass process is operated in an upward flow mode, in which the residual water, in step (a), is supplied from the bottom and displaces the treated water, which is discharged in the same step at the top of the reactor, the gas containing oxygen, in step (b), is supplied at the bottom of the reactor and the biomass having the smallest particle size in step (d) is collected between 30 and 90% of the height of the reactor from the bottom to the top.
    [0008]
    PROCESS according to any one of claims 1 to 7, characterized by the proportion of the part of the residual water fed to the granular biomass process and the part of the residual water fed to the activated sludge process that can be controlled, depending on the quality of the water supply residual and be selected between 5:95 and 75:25, particularly between 10:90 and 50:50.
    [0009]
    PROCESS according to any one of claims 1 to 8, characterized in that the residual water comprises between 10 mg and 8 g of organic waste, expressed as COD, per l, between 0.2 and 1000 mg per l total nitrogen (such as ammonia and / or other nitrogen compound), and / or between 0.05 and 500 mg per l total phosphorus (such as phosphate and / or other phosphorus compounds).
    [0010]
    PROCESS according to any one of claims 1 to 9, characterized in that the activated sludge process comprises two or more treatment mechanisms.
    [0011]
    PROCESS according to any one of claims 1 to 10, characterized in that the granular biomass process comprises a treatment mechanism.
    [0012]
    PROCESS according to any one of claims 1 to 11, characterized in that the granular biomass process comprises two or more treatment mechanisms.
    [0013]
    PROCESS according to any one of claims 1 to 12, characterized in that at least part of a lateral flow process, derived from the activated sludge process and containing levels of nutrients greater than the initial residual water, is returned to the granular biomass process .
    [0014]
    INSTALLATION FOR CARRYING OUT THE PROCESS, as defined in any one of claims 1 to 13, characterized by comprising an activated sludge reactor with a liquid inlet, a liquid outlet, a gas inlet, a granular biomass reactor with an inlet of liquid at the bottom of the reactor, one or more liquid outlets at least a third of the height of the reactor and a liquid outlet at the bottom of the reactor, a gas inlet at the bottom of the reactor, a liquid channel that connects an outlet to the or more liquid outlets at least a third of the height of the granular biomass reactor with an activated sludge reactor inlet, and a separator connected to an activated sludge reactor liquid outlet, having a sludge outlet and a clarified liquid, and further comprising a device for regulating liquid flows relative to the liquid inlet of the activated sludge reactor and the liquid inlet of the granular biomass reactor.
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    同族专利:
    公开号 | 公开日
    BR112014024671A8|2018-12-18|
    JP2015512335A|2015-04-27|
    HK1205497A1|2015-12-18|
    AU2013244078A1|2014-10-23|
    SA113340438B1|2015-10-28|
    CA2869656C|2019-08-27|
    ZA201407205B|2016-01-27|
    US20150336826A1|2015-11-26|
    PH12014502247A1|2014-12-15|
    PH12014502247B1|2014-12-15|
    MX2014011972A|2015-03-13|
    PT2834198T|2017-03-22|
    NZ700605A|2016-08-26|
    JP6563333B2|2019-08-21|
    EP2834198B1|2017-01-11|
    PL2834198T3|2017-07-31|
    CO7170186A2|2015-01-28|
    MX351163B|2017-10-04|
    SG11201406330SA|2014-11-27|
    AU2013244078B2|2017-02-09|
    ES2618933T3|2017-06-22|
    CA2869656A1|2013-10-10|
    DK2834198T3|2017-03-20|
    WO2013151434A1|2013-10-10|
    MY168655A|2018-11-28|
    NL2008598C2|2013-10-07|
    KR102367743B1|2022-02-25|
    KR20150010940A|2015-01-29|
    EP2834198A1|2015-02-11|
    US9758405B2|2017-09-12|
    IN2014DN08410A|2015-05-08|
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    法律状态:
    2018-03-27| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-09-10| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-08-11| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2020-11-24| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 03/04/2013, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
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    NL2008598A|NL2008598C2|2012-04-03|2012-04-03|Hybrid wastewater treatment.|
    NL2008598|2012-04-03|
    PCT/NL2013/050247|WO2013151434A1|2012-04-03|2013-04-03|Hybrid wastewater treatment|
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