• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
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  • 优先权
    • 专利摘要:
    Method and system for the elimination of phosphorus, organic carbon and nitrogen by aerobic granular biomass and pulsating aeration. The present invention relates to a method and system for promoting the development of biopolymer accumulating organisms, with the objective of eliminating phosphorus, organic carbon and nitrogen from industrial or urban wastewater by aerobic granular biomass and pulsating aeration. The system and method employ a sequential batch reactor (SBR) with anaerobic feed-reaction or with feed without reaction. Pulsing aeration has a frequency of seconds. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2702430A1
    申请号:ES201830932
    申请日:2018-09-27
    公开日:2019-02-28
    发明作者:Fernandez Paula Carrera；Del Rio María Angeles Val；Corral Anuska Mosquera；Rodicio Juan Manuel Lema；Gomez José Luís Campos
    申请人:Adolfo Ibanez, University of；Universidade de Santiago de Compostela；
    IPC主号:
    专利说明:

    [0001]
    [0002] Method and system for the elimination of phosphorus, organic carbon and nitrogen by aerobic granular biomass and pulsating aeration
    [0003]
    [0004] TECHNICAL SECTOR OF THE INVENTION
    [0005]
    [0006] The present invention relates to a method and system for the biological treatment of wastewater with pulsating aeration. More specifically, the invention relates to a method and system, based on aerobic granular sludge enriched in biopolymer accumulating organisms for the elimination of phosphorus, organic matter and nitrogen.
    [0007]
    [0008] STATE OF THE ART
    [0009]
    [0010] Aerobic granular biomass was developed for the first time in the late 90s. Technological developments based on this type of biomass are scarce, although they are an interesting alternative to conventional aerobic sludge treatments. These systems offer a series of advantages, such as the reduction of the implantation surface (it is not necessary to use secondary decanters), reduction of sludge production and the concentration of solids in the effluent of the system. However, in the case of heterotrophic aerobic granules (with elimination of organic matter), long start-up times are required and they involve high aeration costs, because it is necessary to supply high quantities of oxygen to maintain the agitation of the reactor. and the biological reactions (A. Mosquera Corral, Advanced Technologies for the Treatment of Wastewater (2nd Edition 2013).
    [0011]
    [0012] An alternative to reduce the start-up time of the system and improve the properties of heterotrophic aerobic granules may be the application of pulsating aeration, since it has been demonstrated in other types of processes that a pulsating regime can help the granulation process of the biomass. In [Franco, A., Roca, E., Lema, JM (2006). Granulation in high-load denitrifying upflow sludge bed (USB) pulsed reactors. Water Research 40, 871-880] pointed out that the use of a pulsating feed (wastewater) flow in UASB reactors (in English: Upflow Anaerobic Sludge Blanket) improved the granulation of the anaerobic biomass and the specific density of anaerobic granules formed, reducing the washing of these and improving the stability and efficiency of the process. The flow of pulsating liquid helped to maintain higher solids concentrations (47.6 g SSV / L) than in a non-pulsation reactor with continuous liquid feed (16 g SSV / L), because the sedimentation rate of the biomass was high (88 m / h in the pulsation reactor, they do not provide data on the sedimentation rate in the reactor without pulsation). The same occurred in [Belmonte, M., Vázquez Padín, JR, Figueroa, M., Mosquera-Corral, A., Campos, JL, Méndez, R. (2009). Characteristics of nitrifying granules developed in an air pulsing SBR. Process Biochemistry 44, 602-606.], Where a system of autologous granular biomass enriched in nitrifying bacteria (only for the elimination of nitrogen) in an SBR (in English: Sequencing Batch Reactor) is proposed, despite the fact that the system pulsing that was used in the aeration, this was not enough to resuspend the biomass and it was necessary to use other strategies.
    [0013]
    [0014] On the other hand, the control of the contribution of air also allows favoring the elimination of nitrogen through the combined biological processes of nitrification-denitrification. In particular, denitrification is favored, which is a process that occurs under conditions of absence of oxygen and allows the transformation of nitrate, produced by oxidation of ammonium during nitrification, to nitrogen gas. Different operating strategies have been used with the aim of reducing the amount of oxygen supplied to the system during the aeration period in order to favor denitrification processes and reduce aeration costs. The strategies are based either on the alternation of aerobic and anoxic stages (absence of dissolved oxygen) or on the reduction of the oxygen concentration in the medium by continuous aeration.
    [0015]
    [0016] In [Lochmatter S., Gonzalez-Gil, G., Holliger, C. (2013). Optimized aeration strategies for nitrogen and phosphorus removal with aerobic granular sludge. Water Research 47 (16), 6187-6197] operated a reactor with intermittent aeration, with alternating periods of 6 - 10 min of air supply and 7 - 12 min without air intake and without the use of mechanical agitation, to eliminate organic matter, nitrogen and phosphorus through the cultivation of PAOs (Phosphate Accumulating Organisms). With this strategy, they obtained elimination efficiencies of 78% nitrogen and 95% phosphorus (they do not provide information on the elimination of organic matter) and granules with good settling (IVL8, Volumetric Index of Sludges at 8 minutes, of 19 mL / g SST). However, they already started with granular biomass previously formed under conditions of continuous aeration.
    [0017]
    [0018] In [Li J., Elliott D., Nielsen M., Healy MG, Zhan X. ( 2011). Long-term partial nitrification in an intermittently aerated sequencing batch reactor (SBR) treating ammonium-rich wastewater under controlled oxygen-limited conditions. Biochemical Engineering Journal 55, 215-222] opted for alternating 30 min of aeration and agitation and 10 min of mechanical agitation without aeration. It is therefore continuous aeration at certain times operations followed by anoxic phases. In addition, it was necessary to incorporate an additional unit for the reactor mixture (mechanical agitator). The process developed by these authors is a system that only removes nitrogen and organic matter, without using granular biomass. As a result of the operation of the reactor, biomass with poor sedimentability was developed with respect to the granules, with IVL values of 110 mL / g SST versus typical values of granules smaller than 60 mL / g SST.
    [0019]
    [0020] In [Jiang, X., Yuan, Y., Ma, F., Tian, J., Wang, Y. (2014). Enhanced biological phosphorus removal by granular sludge in anaerobic / aerobic / anoxic SBR during start-up period. Desalination and Water Treatment 57 (13), 5760-5771] opted for the introduction of an anoxic phase (80 - 148 min) after the aeration period (180 - 140 min), to develop the PAOs, with different duration depending on the operation stage. Despite achieving good elimination percentages of 88.5% total nitrogen elimination, 90% phosphorus elimination and 80% COD elimination (Chemical Oxygen Demand), the granulation process was slow, requiring 80 days to obtain a completely granular system.
    [0021]
    [0022] In [Lu, Y., Wang, H., Kotsopoulos, T., Zeng, R. (2016). Advanced phosphorus recovery using a novel SBR system with granular sludge in simultaneous nitrification, denitrification and phosphorus removal process. Appl. Microbiol Biotechnol 100, 4367-4374] also operated an SBR reactor to develop PAOs. In this case, they decided to reduce the concentration of dissolved oxygen during the aeration period to values of 0.79 -1.56 mg / L of dissolved oxygen. However, in this case, the physical properties of the obtained biomass were poor, being constituted mainly by flocculent active sludge or granular biomass with particle diameters in the minimum size limit that is considered for a granular biomass of 0.2 mm. This was due to the low level of stress to which the biomass was subjected due to the low flow of aeration.
    [0023]
    [0024] On the other hand, there are patents based on the use of intermittent aeration that aim to reduce the energy consumption of the system, both for biological processes and for cleaning tasks.
    [0025]
    [0026] In CN 104944701 (A) there is a process consisting of three reactors connected in series (anaerobic-aerobic-anoxic reactor) for the elimination of COD, nitrogen and phosphorus with intermittent aeration in the aerobic chamber. However, intermittent aeration consists of subdividing the aerobic reactor into independent zones to which air is supplied at different times. It is not a pulsating aeration, but continuous in certain operational moments in each of the areas of the aerobic reactor. In addition, it is not about granular biomass.
    [0027]
    [0028] In CN203728642 (U) a process for the elimination of COD and nitrogen is presented that includes a reactor divided into compartments (anoxic compartment-aerobic-membrane compartment) that operate sequentially, with pulsating aeration in the membrane area for the purpose of cleaning it. Despite the use of pulsating aeration, it is not responsible for the biological processes of COD and nitrogen removal, it is used only to clean the membrane.
    [0029]
    [0030] JPH09192688 (A) presents a system for the elimination of COD and nitrogen consisting of an active sludge chamber with intermittent aeration and a membrane chamber, which operate sequentially. Aeration / non-aeration times are 30-60 s and 5 -20 min. In this case phosphorus is not eliminated and it is not granular biomass.
    [0031]
    [0032] US 2013/0175217 A1 presents a system of submerged membranes for filtration processes, using intermittent aeration to eliminate the adhesion of biomass and solids on the surface of the membranes. In spite of applying short aeration periods (aeration of 0.5 - 20 s and non-aeration of 5 - 40 s), it is not a question of granular biomass or a biological process. Aeration has simply cleaning function, it is not used for biological processes of elimination.
    [0033]
    [0034] DESCRIPTION OF THE INVENTION
    [0035]
    [0036] None of the systems of the state of the art has been applied in systems of aerobic granular biomass constituted by biopolymers accumulating organisms, and pulsating aeration does not have as objective the improvement of the physical properties of the granular biomass nor the decrease of the time of laying in progress of the system.
    [0037]
    [0038] To obtain granular biomass it is necessary to promote the development of slow-growing microorganisms, since they tend to grow forming aggregates. For this, SBR reactors are usually used, since they allow the alternation of periods of satiety / hunger, which create gradients of substrate concentration and help the development of these microorganisms. This type of reactors operate sequentially in different phases: feeding (can be without reaction or with anaerobic reaction), aeration, sedimentation and discharge. The sedimentation stage also acts as a process of selection of microorganisms, allowing only those that are capable of forming aggregates and have a minimum sedimentation rate to remain in the system.
    [0039] Within the organisms of slow growth and accumulators of biopolymers are the phosphorus accumulators or PAOs, which are capable of eliminating both phosphorus and organic matter. In order for them to develop, alternating anaerobic and aerobic / anoxic periods is necessary, therefore, the reactor feeding stage is carried out under anaerobic conditions. The metabolism of these organisms works in such a way that, during the anaerobic feeding stage, they are able to store organic matter inside their cells, releasing phosphorus (stored as poly-phosphate inside the cells) into the liquid medium. Once the feeding stage is over, during the period of famine (aerobic), the stored organic matter is used for growth and the phosphorus released previously is stored again. A simple way of corroborating the presence of PAOs in the reactor is through the relationship between volatile suspended solids (SSV) and total solids (TSS), since the biomass enriched in these organisms usually has SSV / SST values around to 60% due to the phosphorus that precipitates inside the cells in the form of inorganic compound, poly-phosphate. Another indicator of the development of these microorganisms is the fact that, after finishing the anaerobic feeding stage, the concentration of phosphorus in the liquid medium is greater than at the beginning of the cycle, since it is released into the medium to be absorbed again in the aerobic phase, and decreases at the end of the aerobic phase when the effluent is removed.
    [0040]
    [0041] In the case of the feed stage without reaction the slow-growing organisms accumulate the biopolymers in the aerobic reaction stage. Once the biological reaction (accumulation of organic matter in the form of biopolymers inside the cells), during the period of famine (aerobic), stored organic matter is used for growth.
    [0042]
    [0043] To achieve good simultaneous efficiencies of elimination of different pollutants [from Kreuk, MK, Heijnen, JJ, van Loosdrecht, MCM (2005). Simultaneous COD, nitrogen and phosphate removal by aerobic granular sludge. Biotechnology and Bioengineering 90 (6), 762-769] were able to obtain eliminations of 100% of organic matter, 94% of nitrogen and 94% of phosphorus), it is necessary the formation of granules with good physical properties to avoid washing biomass system and ensure the stability of the process. These properties include optimal particle diameters (usually between 1 - 3 mm), as well as good mud density values (between 40 and 60 g SSV / L-granule) and sedimentation velocity greater than 10 m / h. In addition, it is important that the surface of the granules be smooth and without the presence of filamentous bacteria.
    [0044] To obtain granules with good properties it is necessary to guarantee a minimum level of stress in the reactor. It is usually expressed in terms of the ascending speed of the air used during the aeration stage of the reactor, so that the minimum value to obtain stable granules is 1.2 cm / s. The most common way of supplying air to the system is through continuous aeration, which implies high costs.
    [0045]
    [0046] The present invention differs from the works described above since it is a system that, after feeding without reaction or with anaerobic reaction, makes the contribution of air in a pulsating manner during the aerobic phase, with a frequency of seconds. With this option of pulsating aeration, it is possible to favor the development of biopolymer accumulating organisms and also to shorten the start-up time of the aerobic granular biomass reactors, decreasing the time necessary for the granulation process. In addition, pulsating aeration improves the physical properties of granules, such as density, and gives them stability. The latter is very important, since up to now the application of these systems on a real scale has been limited by events of low stability of the aggregates formed. Therefore, solving the stability problem of aerobic granules results in a more efficient operation on an industrial scale. Once the granulation process is completed, pulsating aeration also allows the reduction of costs associated with air consumption.
    [0047]
    [0048] The pulsating regime implies that, by providing a volume of air equivalent to that provided by continuous aeration, the flow rate in each pulse is greater. This allows to increase the ascensional speed during each pulse and therefore increase the level of stress and, consequently, improve the properties of the granules formed. Once the aerobic granular biomass is obtained, an air flow is chosen in each pulse equal to that provided by the continuous aeration, so that the ascent velocity of the gas is the same, but the total volume of air supplied to the system is lower.
    [0049]
    [0050] In one aspect, the present invention relates to a system for treating urban or industrial wastewater by means of granular biomass, characterized in that it comprises:
    [0051]
    [0052] a) a reactor that allows the development of biomass granules containing biopolymer accumulating organisms and where the residual water to be treated is introduced; Y
    [0053]
    [0054] b) a pulsating aeration unit
    [0055] where the reactor operates in cycles that allow the formation of granular biomass and comprise a first stage of feeding, a second stage of aerobic reaction, a third stage of sedimentation and a fourth stage of emptying the effluent, where the pulsating aeration unit controls the supply of air to the reactor during the second stage of aerobic reaction.
    [0056]
    [0057] The feeding stage is selected from an anaerobic feed-reaction stage or a non-reaction feed stage.
    [0058]
    [0059] If the feeding stage is an anaerobic feed-reaction stage, it has a preferred duration of 1/3 of the reactor operation cycle.
    [0060]
    [0061] If the feeding stage is a feeding stage without reaction, it has a preferred duration of between 5 minutes and 30 minutes.
    [0062]
    [0063] The system object of the present invention removes organic carbon and / or nitrogen from the effluent withdrawn in the emptying stage, where the elimination of organic carbon (expressed as COD) and nitrogen from the effluent is comprised in the range 77% to 92% and 23%. % to 43%, respectively. In another aspect, the system of the present invention, in the event that the feeding stage is an anaerobic feeding-reaction stage, also eliminates phosphorus from the effluent with an efficiency comprised in the range 89% to 100%.
    [0064] In another aspect of the invention, the reactor is a sequential batch reactor (SBR).
    [0065]
    [0066] The pulsating aeration unit emits pulses of air with an ascending speed comprised in the range 1.2 - 3.6 cm / s. In a particular embodiment the preferred air rise rate is 3.6 cm / s. The pulsating aeration unit emits pulses of air with a periodicity comprised in the range 2.5 s - 11.5 s, said pulses having a duration comprised in the range 0.5 s to 1.5 s, in a preferred embodiment the duration of the pulses is 1 s. The aeration unit blocks the emission of pulses of air for a period of time comprised in the range 2 s to 10 s, in a preferred embodiment the aeration unit blocks the pulse emission preferably for 2 s.
    [0067] In another aspect of the system object of the present invention the volumetric sludge index measured at 5 minutes (IVL5) in the emptying stage is comprised in the range 40 to 60 mL / g SST.
    [0068]
    [0069] In another aspect of the system object of the present invention the particle diameter of the granular biomass is comprised in the range 1 mm to 3 mm.
    [0070] In another aspect the present invention relates to a method of treatment of urban or industrial wastewater by granular biomass in wastewater characterized in that the operation cycle comprises the following phases:
    [0071]
    [0072] a) a feeding phase in which the waste water to be treated is introduced into a reactor that allows the development of biopolymer storage organisms;
    [0073]
    [0074] b) an aerobic phase with pulsating aeration;
    [0075]
    [0076] c) a sedimentation phase of the granular biomass; Y
    [0077]
    [0078] d) a phase of emptying the effluent from the reactor.
    [0079]
    [0080] The feed phase is selected from an anaerobic feed-reaction phase or a feed phase without reaction.
    [0081]
    [0082] If the feed phase is an anaerobic feed-reaction phase, it has a preferred duration of 1/3 of the reactor operation cycle.
    [0083]
    [0084] If the feeding phase is a feeding phase without reaction, it has a preferred duration of between 5 minutes and 30 minutes.
    [0085]
    [0086] The method object of the present invention is characterized in that it removes organic carbon and / or nitrogen from the effluent. The removal of organic carbon (expressed as COD) and nitrogen from the effluent by the method is in the range of 77% to 92% and 23% to 43%, respectively. In another aspect of the method object of the present invention, if the feed phase is an anaerobic feed-reaction stage, phosphorus is also removed from the effluent, with the removal of phosphorus from the effluent removed in the emptying stage in the range 89 % to 100%
    [0087]
    [0088] In another aspect of the method object of the present invention in the phase of pulsating aeration pulses of air are issued with an ascending velocity comprised in the range 1.2 - 3.6 cm / s, in a preferred embodiment the ascensional velocity is 3.6 cm / s. During the pulsating aeration phase, pulses of air are emitted with a periodicity comprised in the range 2.5 s - 11.5 s. In another aspect of the method the duration of the air pulses has a duration comprised in the range 0.5 s to 1.5 s, in a preferred embodiment the duration of the air pulses is 1 s. In another aspect of the method in the aeration phase the emission of pulses of air is blocked for a period of time comprised in the range 2 s to 10. In a preferred embodiment, the blocking of air pulses has a preferred duration of 2 s.
    [0089]
    [0090] In another aspect of the method the volumetric sludge index measured at 5 minutes (IVL5) in the emptying stage is comprised in the range 40 to 60 mL / g SST.
    [0091]
    [0092] In another aspect the present invention relates to the use of the system and the method for the simultaneous removal of phosphorus, organic carbon and / or nitrogen in waste or industrial water.
    [0093]
    [0094] Therefore, the invention consists in the application of an air pulsation system as a strategy to favor the development of biopolymer accumulation organisms, reduce the start-up time and improve the stability of a system with aerobic granular biomass for the elimination of phosphorus, organic matter and nitrogen from wastewater. In addition, once obtained mature granules, it also aims to improve biological activity, especially nitrogen removal, and reducing the volume of air that is necessary to contribute to the system.
    [0095]
    [0096] BRIEF DESCRIPTION OF THE FIGURES
    [0097]
    [0098] The detailed modalities in the figures are illustrated by way of example and not by way of limitation:
    [0099]
    [0100] Figure 1 shows the evolution of the concentration of phosphorus in the influent (•), at the end of the anaerobic phase (o) and at the end of the aerobic phase (□), for the "Control" reactor (a) and "Pulsante""(B) during the two stages of operation. From the comparison of both graphs it can be seen that the release of phosphorus in the anaerobic phase starts earlier in the "Pulsante" reactor than in the "Control" reactor, indicator of the development of the PAOs. The dashed line represents the change from the first stage to the second in the "Pulsante" reactor.
    [0101] Figure 2 shows the evolution of the concentration of total solids (SST, o) and volatile solids (SSV, •) for the "Control" (a) and "Pulsating" (b) reactor, in the two established operation stages. It can be observed how the difference between SST and SSV increases before in the "Pulsante" reactor than in the "Control", indicator of the development of the PAOs. The broken line represents the change from the first to the second stage in the "Pulsating" reactor.
    [0102] Figure 3 shows the concentration profile of P-PO4 (•) and TOC (Total Organic Carbon, o) for the "Control" (a) and "Pulsating" (b) reactors during a 3-hour operational cycle.
    [0103] Figure 4 shows the evolution of the percentages of elimination of COD (o), nitrogen (A) and phosphorus (•) from the "Control" reactor (a) and the "Pulsante" (b) during the different operational stages. The broken line represents the change from the first to the second stage in the "Pulsating" reactor.
    [0104]
    [0105] EXAMPLES OR DETAILED DESCRIPTION
    [0106]
    [0107] In an example illustrating the invention, the operation of a reactor has been carried out for 16 months. During this operation, conventional sludge from sludge (flocculent) was started with the objective of developing aerobic granular biomass enriched in PAOs.
    [0108] Two geometrically identical reactors of 1.7 L of useful volume each were put into operation, inoculated with active sludge from the Wastewater Treatment Plant (WWTP) of Calo-Milladoiro (A Coruña). The reactors were fed with a synthetic medium simulating a wastewater containing organic matter (190 mg COD / L), nitrogen (23.6 mg N-NH4 + / L) and phosphorus (13 mg P-PO4VL).
    [0109]
    [0110] Both reactors were operated as SBR in 3-hour operating cycles distributed in the following phases: 60 min anaerobic feed-reaction, 112 min aerobic reaction, 1 -7 min sedimentation, 7 - 1 min emptying. In one of them, called the "Control" reactor, a continuous aeration system was established during the aerobic phase. In the other, called "Pulsante" reactor, we opted for an air supply by pulses of 1 second, followed by 2 seconds without aeration (pulse 1 ON / 2 OFF in seconds). The 465-day operation was divided into two stages depending on the air flow rate applied in the "Pulsating" reactor, and no control of the dissolved oxygen concentration was carried out, so that in both reactors it took the saturation value during the aerobic phase. (about 8 mg O2 / L).
    [0111]
    [0112] In Stage I (days 0 - 397) the flow rate of the 1 second air pulse was set so that, at the end of the aeration period, the volume of air supplied to the system was the same as in the "Control" reactor. In this way during the 112 minutes of the aeration phase the same volume of air (448 liters) was introduced in both reactors, but in the "Pulsating" reactor during each pulse of air introduced the applied ascension speed was 3 times higher (3 , 6 cm / s) than the one applied in the "Control" reactor (1.2 cm / s). In this first phase of operation the sedimentation time was gradually reduced from 7 to 2 minutes (day 99) and finally 1 minute (day 128) in both reactors.
    [0113] In Stage II (days 398 - 465) the flow rate during the 1-second air pulse applied to the "Pulsating" reactor was reduced 3 times, so that both reactors were exposed to the same 1.2 cm / ascent velocity. s. However, the total contribution of air in the aeration period was different. In the "Pulsante" reactor it was 149 liters, while in the "Control" reactor it remained at 448 liters.
    [0114]
    [0115] Table 1: Characteristics of the aeration stage in both reactors
    [0116]
    [0117]
    [0118]
    [0119]
    [0120] The differences in the aeration strategies were reflected in the granulation process of the biomass, as well as in the elimination of phosphorus. In the "Pulsante" reactor, the granulation process was completed approximately 10 days before the "Control" reactor, and the PAOs were developed about 20 days before, which is reflected both in the elimination percentages and phosphorus concentrations end of the anaerobic phase (FIGURE 1), as in the relationship between volatile and total suspended solids, which decreased to an approximate value of 60%, typical of granules dominated by PAOs (FIGURE 2). Another way to confirm this fact is by observing the result of the analysis of the two operation cycles measured for both reactors on day 91 of operation (FIGURE 3). It can be clearly seen that the "Control" reactor has the peak of phosphorus concentration displaced from the 60 minutes of feed, which is when the anaerobic phase ends, and not all the organic matter is consumed in the anaerobic phase. In contrast, the phosphorus profile in the "Pulsante" reactor does not have the peak of the displaced phosphorus concentration and there is no increase in organic matter at the end of the anaerobic phase, which indicates that the PAOs were able to use it to the release of phosphorus. In addition, the release of phosphorus is higher in this case, 45 mg P-PO4VL compared to 37 mg P-PO4VL in the control reactor.
    [0121]
    [0122] Besides shortening the time for the granulation process, pulsating aeration also caused the appearance of granules with better physical properties, since the Volumetric Index of Sludge measured at 5 minutes (IVL5) and the particle diameter are lower in the reactor "Pulsating" (30 mL / g SST and 3.14 mm, respectively) than in the reactor "Control" (40 mL / g SST and 3.45 mm respectively). In addition, denser granules were obtained in the "Pulsante" reactor (Table 2).
    [0123]
    [0124] The elimination efficiencies of the "Control" reactor were 28.3 ± 10.3% nitrogen, 96.3 ± 7.2% phosphorus and 82.8 ± 7.0% COD (FIGURE 4a). In the "Pulsante" reactor the percentages were 32.9 ± 9.6% nitrogen, 95.6 ± 6.2% phosphorus and 84.3 ± 7.2% COD (FIGURE 4b).
    [0125]
    [0126] Once both reactors were operated with the same total aeration flow and different surface velocity for 397 days, the amount of air supplied in the "Pulsating" reactor was reduced to have an ascending speed of 1.2 cm / s. After operating the reactor with this condition for 67 days, the elimination efficiencies remained similar, with values of 36.6 ± 8.7% nitrogen, 94.6 ± 3.3% phosphorus and 86.3 ± 2.7 % of COD. The characteristics of the biomass were an IVL5 of 45 mL / g SST and an average granule size of 1.90 mm. This indicates that the results obtained are very similar to those of the "Control" reactor, with the difference that in this case the volume of air is three times smaller.
    [0127]
    [0128] Table 2: Summary of the results obtained from the "Control" and "Pulsating" reactors
    [0129]
    [0130]
    [0131]
    [0132]
    [0133] Therefore, it can be concluded that the contribution of air in a pulsating manner favored the development of the PAOs, thus reducing the granulation period and the time necessary to achieve high elimination efficiencies. This was due to the fact that, providing the same volume of air, the level of stress to which the biomass was subjected was greater, as higher air flows were provided. After reducing the air flow so that the The total volume contributed to the system was the same as in the continuous regime, the results remained the same, maintaining both the properties of the biomass and the efficiencies of elimination reached previously. The difference is that the contribution of air made is lower, which reduces the costs associated with aeration.
    权利要求:
    Claims (1)
    [0001]
    1- A system of urban or industrial wastewater treatment by means of granular biomass, characterized in that it comprises:
    a) a reactor that allows the development of biomass granules containing biopolymer accumulating organisms and where the residual water to be treated is introduced; Y
    b) a pulsating aeration unit
    characterized in that the reactor operates in cycles comprising a first stage of feeding, a second stage of aerobic reaction, a third stage of sedimentation and a fourth stage of emptying the effluent, said cycles producing particles of granular biomass, where the aeration unit controls the aeration of the reactor during the second stage of aerobic reaction.
    2- The system, according to claim 1, characterized in that the feeding stage is an anaerobic feed-reaction stage.
    3- The system according to claim 2, characterized in that the duration of the anaerobic feed-reaction stage is 1/3 of the reactor operation cycle.
    4- The system according to claim 1, characterized in that the feeding stage is a feed stage without reaction.
    5- The system according to claim 4, characterized in that the step of feeding without reaction has a preferred duration of between 5 minutes and 30 minutes.
    6- The system according to claims 1 to 5, characterized in that it removes organic carbon and nitrogen from the effluent removed in the emptying stage.
    The system according to claim 6, characterized in that the removal of organic carbon, expressed as COD, from the effluent is comprised in the range 77% to 92%.
    8- The system according to claim 6, characterized in that the elimination of nitrogen from the effluent is comprised in the range 23% to 43%.
    9- The system according to claims 1 to 3, characterized in that phosphorus is also eliminated.
    10- The system according to claim 9, characterized in that the elimination of phosphorus from the effluent is comprised in the range 89% to 100%.
    11. The system according to claim 1, characterized in that the reactor is a sequential batch reactor (SBR).
    12- The system according to claim 1, characterized in that the pulsating aeration unit emits pulses of air with an ascending speed comprised in the range 1.2 - 3.6 cm / s.
    13- The system according to claim 12, characterized in that the preferred air rise rate is 3.6 cm / s.
    14- The system according to claim 1, characterized in that the pulsating aeration unit emits pulses of air with a periodicity comprised in the range 2.5 s -11.5 s.
    The system according to claims 1 and 12, characterized in that the pulses of air emitted by the aeration unit have a duration comprised in the range 0.5 s to 1.5 s.
    16- The system according to claim 15, characterized in that the preferred duration of the pulses of air emitted by the aeration unit is 1 s.
    17- The system, according to claims 1 and 14, characterized in that the aeration unit blocks the emission of air pulses for a period of time comprised in the range 2 s to 10 s
    18- The system according to claim 17, characterized in that the aeration unit blocks the pulse emission preferably for 2 s.
    19- The system according to claim 1, characterized in that the volumetric index of sludge measured at 5 minutes (IVL5) is comprised in the range 40 to 60 mL / g SST.
    20- The system according to claim 1, characterized in that the particle diameter of the granular biomass is comprised in the range 1 mm to 3 mm.
    21- A method of urban or industrial wastewater treatment using granular biomass, characterized in that the operation cycle includes the following phases: a) a feeding phase in which the waste water to be treated is introduced into a reactor that allows the development of biopolymer storage organisms;
    b) an aerobic phase with pulsating aeration;
    c) a sedimentation phase of the granular biomass; Y
    d) a phase of emptying the effluent from the reactor.
    22. The method according to claim 21, characterized in that the feeding phase is an anaerobic feed-reaction phase.
    23- The method according to claim 22, characterized in that the duration of the anaerobic feed-reaction phase is 1/3 of the operation cycle.
    24- The method according to claim 21, characterized in that the feeding stage is a feed stage without reaction.
    The method according to claim 24, characterized in that the duration of the feed phase without reaction has a preferred duration of between 5 minutes and 30 minutes.
    26- The method according to claims 21 to 25, characterized in that it removes organic carbon and / or nitrogen from the effluent.
    27. The method according to claim 26, characterized in that the removal of organic carbon (expressed as COD) from the effluent is in the range of 77% to 92%.
    28- The method according to claim 26, characterized in that the removal of nitrogen from the effluent is comprised in the range 23% to 43%.
    29- The method according to claims 21 to 23, characterized in that it also eliminates phosphorus.
    The method according to claim 29, characterized in that the removal of phosphorus from the removed effluent is in the range 89% to 100%.
    The method according to claim 21, characterized in that in the aerobic phase with pulsating aeration pulses of air are issued with an ascending speed comprised in the range 1.2 - 3.6 cm / s.
    32. The method according to claim 31, characterized in that the preferred air rise speed is 3.6 cm / s.
    33- The method according to claim 21, characterized in that in the aerobic phase with pulsating aeration pulses of air are emitted with a periodicity comprised in the range 2.5 s - 11.5 s.
    34- The method according to claim 21 and 33, characterized in that in the pulses of air emitted in the aerobic phase with pulsating aeration they have a duration comprised in the range 0.5 s to 1.5 s.
    35. The method according to claim 34, characterized in that in the aerobic phase with pulsating aeration the emission of pulses of air is blocked for a period of time comprised in the range 2 s to 10 s.
    36. The method according to claims 21 and 33, characterized in that the preferred duration of the pulses of air emitted in the aerobic phase with pulsating aeration is 1 s.
    37. The method according to claim 36, characterized in that in the aerobic phase with pulsating aeration the blocking of air pulses has a preferred duration of 2 s.
    38. The method according to claim 21, characterized in that the volumetric index of sludge measured at 5 minutes (IVL5) is comprised in the range 40 to 60 m / g SST.
    39. The method according to claim 21, characterized in that the particle diameter of the granular biomass in the reactor is in the range 1 to 3 mm.
    40- Use of the system according to claims 1 to 20, and of the method according to claims 21 to 39, for the elimination of phosphorus, organic carbon and / or nitrogen in urban or industrial wastewater.
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    同族专利:
    公开号 | 公开日
    ES2702430B2|2019-09-27|
    WO2020065114A1|2020-04-02|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    WO1998037027A1|1997-02-21|1998-08-27|Technische Universiteit Delft|Method for acquiring grain-shaped growth of a microorganism in a reactor|
    WO2012023114A1|2010-08-18|2012-02-23|Veolia Water Solutions & Technologies Support|Method of treating municipal wastewater and producing biomass with biopolymer production potential|
    WO2012098171A2|2011-01-20|2012-07-26|Valbio|Method for the biological treatment of wastewater using an aerobic granular biomass|
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    PCT/ES2019/070633| WO2020065114A1|2018-09-27|2019-09-23|Method and system for removing phosphorus, organic carbon and nitrogen using aerobic granular biomass and pulsed aeration|
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