UA63890C2 - A method for treating waste material from the effluent water and an apparatus for realizing the same - Google Patents

Abstract

A method and apparatus for treating waste material to remove selected components form the waste is described using a reactor or a series of reactors in fluid communication with each other for receiving the waste to be treated as influent. The influent forms a biomass including the waste and microorganisms and is treated by controlling the metabolic activity of the microorganisms by monitoring the oxygen utilisation rate or the potential oxygen utilisation rate of the biomass so as to determine the required amount of oxygen to be supplied to the biomass and to determine the period of aeration of the biomass in order to maintain a predetermined oxygen utilisation rate or value so as to remove the selected components of the waste. The preferred selected components to be removed are nitrogenous, carbonaceous and/or biological phosphorus containing materials or derivatives.

Description

Description of the invention

The invention relates to improvements in wastewater treatment and, in particular, to a method of wastewater treatment using microorganisms and means of controlling the metabolic activity of these microorganisms in an activated sludge reactor with variable volume, which is alternately subjected to aeration and dehydration. In particular, the present invention relates to methods and devices for controlling the metabolic activity of microorganisms with dispersed growth by regulating the supply of oxygen relative to the rate of oxygen absorption by the biomass measured in the pool.

A beneficial result of this is the removal of carbon or carbonaceous materials from the wastewater, as evidenced by 70 measurements of chemical oxygen demand, biochemical oxygen demand, and total organic carbon; removal of nitrogen, which is evidenced by the data of measurements of the total nitrogen content, determined according to Kjeldahl, МН 3-М,

MO2-M, MO3-M; and removal of phosphorus, as evidenced by the data of PO measurements). This invention will find application, in particular, for the treatment of domestic wastewater, industrial wastewater or their mixtures. The invention, in particular, relates to the maximization of the rate of removal of biodegradable materials found in wastewater by microorganisms by optimizing the metabolic activity of those microorganisms that are used in the method of reaction with sludge of the same type. It turned out that under these conditions, among all the biological communities that must be maintained, there are at least four main species or families of microorganisms. Microorganisms that are mostly responsible for the total removal of hydrocarbon compounds, microorganisms that usually oxidize nitrogen compounds to nitrate nitrogen, microorganisms that usually decompose nitrates to nitrogen gas, and microorganisms that usually participate in the enhanced biological removal of phosphorus and in the general hydrolysis of prone to decomposition of volatile solid particles to the state of a soluble substrate prone to decomposition. All groups that make up biomass can contain up to 20,000 individual types of microorganisms.

Although the present invention will be described in relation to the treatment of industrial and domestic waste water and in relation to the method of such treatment, it will be understood by a person skilled in the art that the invention is not limited to these applications and can (3) be used to treat any biodegradable waste water or other waste water and any waste that contains water or waste with specific impurities or pollutants, as discussed below.

Usually, the treatment of activated sludge requires detailed recording of information, on the basis of which decisions are made about the control of the process to achieve the treatment goal. These analyses, which are well known to specialists, Ge"! usually include analyzes of biochemical oxygen demand (total), chemical oxygen demand (total), biochemical oxygen demand (dissolved substances), chemical oxygen demand (dissolved substances), with determination of the total nitrogen content according to Kjeldahl. analyzes of the content of organic nitrogen, MO3-M, the content of "9 orthophosphates, the total content of phosphates, pH, alkalinity of wastewater streams, both those that come for 3o treatment and those that have been treated. The measurements carried out in the basin include the measurement of the concentration of ee, dissolved oxygen, the concentration of suspended particles in the sludge mixture, the concentration of suspended volatile particles in the sludge mixture, the volume of the settled sludge, the fraction of biomass prone to decomposition (by aerobic decomposition of biomass for 28 days) . For the automatic control and operation of a reactor with a variable volume and activated sludge of the same type, in order to achieve an extremely high degree of removal of carbon, nitrogen and phosphorus without swelling of the sludge, simple parameters are used, which include the potential rate of oxygen consumption and the actual speed of its use. c" This invention relates to the treatment of activated sludge wastewater, and the main reactor is configured to operate in full mixing mode. While operation in the mode of variable volume with dosed loading and periodic aeration and draining of the liquid may be considered as the preferred option, the method is also applicable for operation in the mode of complete mixing at a constant volume with continuous aeration. Key words: metered loading, periodically aerated, complete co-stirring, reactor basin. The present invention may use a sequence of activated sludge reactors interconnected by a pipeline or other means with or without the use of means for interrupting the flow between said reactors. The last reactor of each sequence (Te) of 20 reactors is called the main reactor, from which biologically treated wastewater comes out. It is obvious to those skilled in the art that the reactor can be made in the form of a sedimentation tank with inclined walls, earthen, concrete-reinforced, lined with an anti-filtration coating or held by concrete, or as a conventional tank with reinforced concrete walls, or as a structural steel tank. Since certain shapes and proportions of the basins may be preferred, it is important to note that according to description 29 of the present invention, a tank of any geometric shape (square,

GF) rectangular, round).

It is well known to those skilled in the art that in order to achieve biological nitrification-denitrification and enhanced biological removal of phosphorus, a number of reaction conditions must be met. In particular, the nitrification reaction requires an adequate supply of inorganic carbon. Phosphorus removal by biological 60 means requires the maintenance of selective reaction conditions in order to force the necessary microorganisms to multiply rapidly. One of these requirements is a substrate that preferably contains volatile fatty acids and is better known as a readily degradable soluble substrate. An additional requirement is reaction conditions that carry out a cycle between the so-called concepts of oxygen and anaerobic. When using these terms, it is necessary to be more precise in the definitions, since there are degrees of anaerobicity that trigger certain biological reactions. because according to modern terminology, the absence of oxygen and nitrite-nitrate is not a sufficient factor to describe the concept of "anaerobic" to the extent that biological removal of phosphorus occurs. Anaerobic reaction conditions require a more precise definition also when it comes to multiphase treatment of activated sludge, in which conditions of oxygenic, anoxic and anaerobic reactions can be stimulated on a single-species sludge culture by relatively simple manipulation of filling and aeration periods. With sequentially changing conditions of anaerobic, anoxic and oxygen reactions, exposure of the culture to high pressures of acetate-substrate loading has an advantage over the pressures of the selective reaction. The absence of nitrate and dissolved oxygen is not sufficient to define anaerobic conditions that will force the appropriate species of microorganisms to release their poly-P content.

Usually, the conditions of the corresponding reaction are described through the oxidation-reduction potential of the liquid phase (the value of 70 electromotive force obtained during measurements with a standard electrode made of hydrogen or silver chloride). Therefore, this value must be sufficiently negative (-150mMV, for the hydrogen electrode) to guarantee a detectable degree of anaerobicity to support the phosphate release mechanism. It was determined that when the oxidation-reduction potential switches, the rate of reduction of the potential from positive (oxidation conditions) to negative (reduction conditions) depends on the metabolic activity of the biomass. The same metabolic /5 activity is a function of the amount of residual accumulated intracellular compounds found in the culture.

According to these considerations, if the oxidizing reagent (oxygen) is removed, the biomass that has a high value of the oxygen absorption rate in the oxidizing environment will quickly approach more negative values of the oxidation-reduction potential. Therefore, biomass with a lower value of oxygen absorption rate will reduce its oxidation-reduction potential at a lower rate. Biological 2o Release of phosphorus occurs at potential values approximately 250mV more positive than those at which reduction of sulfate to sulfide takes place. In another existing treatment process at a constant volume, it was necessary to determine the time criteria for liquid retention as a means of guaranteeing the appropriate reaction conditions.

By trial and error, a number of parameters were found that are related to the process and are simply described in terms of the actual rate of oxygen absorption by the biomass of one type of sludge, which can be used to set such reaction conditions that guarantee obtaining a reliable and always desired process result.

The application of these parameters to control the operation of the preferred option makes the entire i) process less expensive than known methods and less difficult to perform. The main parameter refers to the overall activity level of the biomass, which is derived from measurements of its oxygen utilization rate and its potential oxygen utilization rate. Controlling the process using these parameters gives the ability to use selected point values that correspond to reliable removal of pollutants and nutrients and at the same time produce biomass with excellent solids-liquid separation properties. co

It is an object of the invention to provide a method and device for the treatment of wastewater that at least partially overcomes one or more of the difficulties of existing methods and devices through more detailed control of process conditions and parameters related to biomass activity, for example, such as utilization rates of oxygen, including co with potential rates of oxygen use.

A method of treating waste by controlling the metabolic activity of microorganisms of a biomass comprising the waste to remove selected constituents therefrom prior to destroying the treated waste is provided, characterized in that the method comprises controlling at least one rate of oxygen utilization by the biomass with "

The purpose of determining the required amount of oxygen to be supplied to the biomass and controlling the duration from s of the biomass aeration period with oxygen to maintain a given rate of oxygen use or the value required to remove these components. ;" One embodiment of the present invention relates to the sizing of the activated sludge reactor(s), its mode(s) of operation, and automatic optimization of the amount of oxygen supplied to the reactor(s) as expressed by the rate and duration of its supply as determined by measuring metabolic activity biomass in

Ge" main reactor. This metabolic activity is measured as the actual rate of oxygen utilization by the biomass in the main reactor shortly before or at the end of the aeration period. After the air supply to the main reactor is cut off, its contents remain in motion for up to ten minutes while natural motion

Go! mixing decreases rapidly with time. Dissolved oxygen concentration values are measured and recorded at intervals of ten or twenty seconds. A minimum of ten points are measured and mathematically processed to obtain the slope of the best fit that most accurately describes the initial rate of decrease in the amount of dissolved oxygen, and therefore the nominal value of the actual rate of oxygen use. These experimental data are plotted in the form of a graph depending on the volume of the cycle, the volumetric loading used in the activity measurements, and the maximum concentration of dissolved oxygen measured during the cycle. dv The measured dissolved oxygen concentration and fan speed profile are also recorded. This invention relates to maintaining in biomass (a mixture of microorganism cultures), by optimal oxygen supply, (F) optimal selective biological activity, by means of measurements of the rate of oxygen utilization by the biomass, the suspended volatile solid fraction and the degradable suspended volatile solid fraction, which is determined later . The dissolved oxygen sensor measures the rate of oxygen use by the biomass at the location of the sensor, and this data is used to control and regulate the oxygen supply from the pump or compressor that supplies air to the inlet device. In preferred embodiments of the invention, the reaction conditions in this main reactor alternate sequentially from the air supply mode to the air shut-off mode. The aeration period is usually continuous and continues while the wastewater to be treated is fed to the basin(s), then the aeration is stopped, during which time the biomass 65 being processed in the main reactor settles, after which the supernatant is removed from the main reactor. In a similar way, the invention is implemented in the case when the air supply is not continuous.

At the end of the treated wastewater removal period, air and untreated wastewater are again supplied to the main working reactor until the time when the air supply period ends again. A typical full cycle of operation can be considered four hours, with a typical aeration period extending for two hours; other time ratios can be used. Those skilled in the art will readily appreciate that other time intervals can be used. Perform two measurements. The rate of decrease of dissolved oxygen during the first minutes after the cessation of aeration. Other intermediate speeds associated with multiple alternations of the aeration period can also be measured. The second rate is measured when the air supply is turned on again, and during this period the reactor or part of it is supplied with a flow of air at the maximum rate for a given time (this /o time is a variable value that must be specified for each installation and is subject, relatively infrequently, to adjustment by carrying out the calibration procedure). The rate of change of the increase and decrease in the amount of dissolved oxygen (aO»)/4di and the rate of change in the nature of biomass deposition 4(MI 55)/4di are related to each other, where 02" is the concentration of dissolved oxygen, and (MI 55) is the simple concentration of active mud Both of these values change over time when the air supply to the pool is stopped. Similarly, both parameters 7/5 Change with time at the beginning of the aeration period. In a preferred embodiment of the invention, the main reactor of the system is equipped with diffuser grids and supply lines to create more than one reaction zone with effective mixing after the air supply. At the beginning of the aeration period, at least one section of the main reactor will normally be aerated. Biomass from this initially aerated mixing zone is used to determine the rate of change of oxygen increase at the beginning of the 2o aeration period. In a preferred embodiment of the invention, it is possible to select the aeration time of different zones equipped with grids. In those embodiments of the invention where there is only one grid node, the same results can be achieved by aerating the entire volume of the main reactor.

It is also proposed to measure the rate of oxygen use inside the pool in order to determine its amount, expressed through the supply rate and the duration of the aeration period necessary to maintain the rate of oxygen use at a given level. In turn, this determines the reaction conditions for wastewater treatment when using the technology of one reactor with one type of sludge and dosed loading. Measurement i) and control is only one part of this invention. In a preferred embodiment of the invention, the treatment process in the reactor pool is closely related to the measurements. In this invention, both of them are related. It is clear to experts that aeration of the main reactor for too long, through successive periods of treatment, will quickly lead to the loss of metabolic activity of the biomass inside the reactor and, as a result, to the inability of this biomass to properly carry out denitrification and participate in the removal of phosphorus. Excessive aeration of biomass will also lead to weakened aggregation of flocs, and therefore to an undesirable increase in the concentration of suspended particles in treated wastewater. Long-term work with activated sludge, the age of which exceeds the desired limit, will lead to similar consequences. Measurement of the rate of oxygen utilization by biomass is used to establish the limit of the age of working activated sludge. co

This invention is illustrated as an example by the attached drawings, in which:

Fig. 1 is a schematic view of one form of reactor according to the present invention, which consists of a single reactor divided into two compartments;

Fig. 2 is a schematic view of another form of reactor according to the present invention, which is a single pool, which includes the main reactor and separate auxiliary reactors; in c Fig. 33 is a schematic view of one form of the anoxic denitrification model inside the flocs, which

And is used in this invention; and?" Fig. 4 - a graph of biospeed at a given operating point with insufficient nutrition;

Fig. 5 is a schematic diagram of determining the conditions of oxygen, anoxic and anaerobic reactions through the measured oxidation-reduction potential of the liquid phase;

Ge" Figures b(a)-6(9) - schematic views of reactor forms with different configurations of inlets and outlets for purified wastewater, including multi-slot inlets and outlets. Although it is clear to those skilled in the art that the reaction according to the invention can be carried out in various ways, further from

Go! for the purpose of illustration, a simple version will be described.

Figure 1 schematically shows one of the forms of a single-pool reactor according to the present invention. The boundary of the reactor basin, shown in Fig. 1, is shown in a vertical section marked (1) and is a solid structure designed to hold water. A minimum of two reactor zones are depicted, designated as (3) and (4), which are created by means of an additional compartment, partial wall, partition wall, or similar device (shown as (2)). Zones of the reactor are connected to each other by means of a pipe or other channel for liquid, or through a part of the open area formed by a partial partition wall. Means for dispersing the air, mainly through meshes of membrane diffusers, in order to supply the reaction component - oxygen, shown as

F) (5), receive a stream of compressed air from the mechanical pump shown as (6). Shown are the means for transferring the contents of the main reactor (4), using a pump that regulates the transfer and provides contact with the incoming stream of untreated wastewater (marked (11)), to mix this content and carry out the reaction in the reactor (3). Two important levels are shown in the reactor basin: (8) - calculated lower water level and (7) - calculated upper water level. In this embodiment of the invention, during the time when the flows marked (10) and (11) are moving, that is, during the filling from the lower water level (8) to the upper level (9), the aeration period continues. When this period ends, the aeration means are turned off to stop the mixing and oxygen transfer process, allowing the mixed solids to settle and separate to form an upper layer of clear supersludge liquid and a layer of settled solids. At the appropriate time, the decanter (9) starts working, which removes part of the liquid volume between the levels (8) and (9), after which it is turned off until the end of the next cycle. In this embodiment of the invention, the input stream (11) can be continuous or pulsating; the output of the liquid, due to the operation of the decanter (9), is necessarily interrupted relative to the total duration of the cycle, which allows for inflow, aeration, sedimentation and draining of the liquid. Sensor

Dissolved oxygen (12) is placed either inside the main reactor (4) or inside the pumping line, along which the biomass from the main reactor is supplied as an admixture to the wastewater (11), which enters for treatment in the first reaction zone (3); in this case, the location of the sensor is marked as (14). In a preferred embodiment of the invention, the device shown as (13) can be used to record the concentration of biomass in the pool (the concentration of suspended particles in the sludge mixture). The detector (15) of the surface/o suspended layer of the sediment is also useful for automatic sludge depletion operation, according to the variant implementation of the invention, which is preferred. Shown are two grid assemblies of diffusers mounted on the floor; positions (16) and (17) schematically show mesh assemblies that are selectively actuated by more than two devices consisting of a vertical pipe and a valve. It is clear to experts that the main reactor pool can have significantly more than two devices with vertical pipes and valves, in /5 Dependence on the total area of the reactor pool and the effective area of influence of means for diffusion mixing and oxygen transfer. Variants of the reactor according to the invention provide selective and periodic aeration of the surface or general aeration of the surface.

The variant(s) of the reactor(s) according to the present invention, shown in Fig. 2, have (have) similar components to the reactor of Fig. 1 and, accordingly, the same numbers of marks to identify the identical features of the reactors) .

The present invention relates to a method of wastewater treatment and means of managing the general metabolic activity of microorganisms with dispersed growth within the sludge mass of one species. The beneficial result of this is the reliable and simultaneous removal of carbon compounds, as evidenced by the data of measurements of chemical oxygen demand, biochemical oxygen demand and total organic carbon content, nitrogen removal, as evidenced by data of measurements of the total nitrogen content determined according to Kjeldahl, МНз-М, МО »-M, MOz3-M, and the removal of phosphorus, as evidenced by the data of PO measurements, from wastewater within the duration of the treatment process, which consists of repeated cycles. The invention relates to means of measuring the rate of oxygen use inside the pool i) and controlling the incoming aeration flow in order to maintain the reaction conditions within the given regime, which allows to perform the treatment of single-species sludge in one pool with carbon removal and/or nitrogen removal and/or enhanced biological phosphorus removal . These reaction conditions depend on the given rate of oxygen utilization, as it determines the viability of the microbial population at a given age of the working sludge, and it itself depends on a number of properties of single-species sludge deposition. Wastewater can be purely domestic or industrial, or a mixture of both. co

Industrial wastewater is characterized by a discrete composition, which distinguishes it from general domestic wastewater, which necessarily contains human waste (feces, urine), wastewater from bathing, washing and) laundry and cooking. Industrial wastewater is, in fact, water generated during the production of products, and, in particular, this wastewater is biodegradable. Modern technologies that use microbiological reactions involving cultures with dispersed growth are well described in the literature, for example:

Ochi T., EsKepieideg MU. MU., apa Sogopegu M. S, "Asiimaye Zitsade; Zia(e-oi-(pe-Agi). Styisa! Kemiemuv ip

Epmigoptepia! Sopigoi, SKS Rgezz Moi. 15, Izetsze 2, 1985. "

Eskepgeideg MU., UUezieu, "Ipdivigia |! MUaviematseg Tteaiitep!", MsOgam NII, 1991. with s. Rybiizpipd Sotrapu, Ips., 1980. Without limiting the scope of the invention, we will provide reference data on individual components of wastewater; in household and other?" in industrial wastewater, their relative shares may differ. What is important is that these fractions exist, and their relative magnitude can affect the method of using the invention and the operating setup in which the invention is carried out.

Wastewater usually contains soluble and insoluble components, which include soluble organic substances prone to easy decomposition, soluble organic substances that do not decompose so quickly, soluble organic substances that do not decompose, substrates formed by particles that easily hydrolyzed and decomposable, substrates formed by particles that are slowly decomposing or not decomposing. These substrates, their relative concentrations and their concentrations in relation to other components, such as total and Kjeldahl nitrogen content, MNUI-H, MOZ3-M, total phosphorus and ortho-P, can have a large effect on o growth rate and for the reproduction of ordinary types of microorganisms with dispersed growth.

Sbogopeg2gu M.S. apa EsKepieIdeg MU.MU., "Te gaye oi (She dedgadayop oi rgitagu zoiiavz ip asiimaiei vishdde riapiv", Rgoseedipdz U/a(eg Roishiop Sopigo! Redegaiop Sopiegepse, Togopio, Sapada. Osioreg 1991.

The method of wastewater treatment by micro-organisms with dispersed growth usually covers the spheres of oxygen, anoxic and anaerobic reactions and the mechanisms by which energy is transformed, including (Ф, electron acceptors for the general reduction of the concentration of organic compounds, according to the data of measurements of chemical oxygen demand, biochemical oxygen requirements, the total content of organic carbon, and the amount of nitrogen and phosphorus (fig. 5). 60 These treatment regimes in general can be described partly through the concentration of dissolved oxygen, nitrite and nitrate nitrogen, sulfate, phosphate, and partly using a scale of oxidation-reduction potentials relative to a standard hydrogen electrode. Positive values of the oxidation-reduction potential typically correspond to oxidizing conditions, while negative values of the oxidation-reduction potential typically correspond to reducing conditions. On the positive side of the scale, there is no definite relationship between the 65 oxidation-reduction potential and the concentration of dissolved of oxygen, although the supply of oxygen, as a chemical source of this element, forces the oxidation-reduction potential to be less negative or more positive.

Temperature can affect the relative value of the oxidation-reduction potential, as can the presence and relative density of microorganisms. The removal of carbon compounds and compounds that determine the total nitrogen content necessarily requires aerobic conditions, the removal of MO 3-M and MO»-M requires conditions from anoxic to anaerobic, and the removal of phosphorus requires oxygen-anoxic and anaerobic conditions during cyclic exposure of biomass , or special biomass particles in the aeration basin, in order to reach the range of oxidation-reduction potentials necessary for the reaction, which vary from approximately 50 MV to -150 mV (for the hydrogen electrode), and to allow all reactions that take place during processing to take place. An understanding of the actual discrete mechanisms, while important to the processing results, is not of great 7/0 Significance for the description of the preferred embodiment of the invention provided herein.

There are reaction modes that provide a complete treatment process, which is absolutely necessary for the removal of the above-mentioned compounds with the help of single-bit sludge. Typical domestic wastewater is described using weighted stream samples lasting 24 hours, where the measured parameters of total amounts of chemical oxygen demand, total nitrogen content, determined according to Kjeldahl, phosphorus reach 100Omg/l, 85mg/l and 15mg/l. nn nn

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The relative values of the amount of carbon, nitrogen and phosphorus, indicated in Table 1 according to the literature, significantly "differ from those necessary for normal biological growth, as can be seen from the ratio of carbon and nitrogen obtained by empirical analysis of cell material - C5H)MO" - together with the fact that - c cells contain approximately 1 to 295 phosphorus by mass. That is, in untreated wastewater, as shown in Table 2, carbon is present in insufficient quantities compared to nitrogen and phosphorus. This deficit is more pronounced in settled wastewater, and further added to this is the fact that during biological treatment, about 5,095% of organic carbon is oxidized to CO.

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Ge in water (mg/l) 60 In wastewater treated at a biological treatment plant, nitrogen and phosphorus usually remain in excess relative to the needs of biological growth. The form in which these nutrients are present in treated wastewater can be markedly different from the form in which they exist in effluents submitted for treatment.

In untreated sewage, nitrogen is present in the form of organic nitrogen and ammonia, most of which is the result of hydrolysis of urea, the main component of urine. During biological treatment, some of this nitrogen is involved in the growth of new cells and is removed as bioactive sludge, while most of the remaining nitrogen

can be in the form of ammonia or, depending on the treatment conditions, in the form of oxidized forms, nitrate and, in smaller quantities, nitrite. A part of organic nitrogen, mainly bound to solid particles suspended in these waters, also remains in treated wastewater.

Phosphorus in untreated wastewater is present in two main forms - organic and inorganic.

In fact, many forms of phosphorus compounds are present in untreated wastewater, either in solution or as suspensions. The inorganic insoluble forms consist mainly of orthophosphates and condensed phosphates, while the dissolved organic forms are organic orthophosphates.

One specific mechanism relates to reaction conditions that maximize the initial rate of removal and 7/0 accumulation of the readily degradable soluble fraction of the wastewater stream entering the treatment plant. In the present invention, a treatment plant is described as a means for receiving said wastewater, a means for bringing the untreated wastewater stream into contact with the cultured active microorganisms, a means for keeping said wastewater in contact with the decomposing microorganisms in order to carry out a complete treatment process and means for separating said treated wastewater from microorganisms which /5 participate in decomposition and remain in the reactor. The complete treatment process involves the production or presence of a sufficient concentration of active microorganisms (Xo), in which the close contact of these microorganisms with the soluble and easily degradable substrate (Zo) of the incoming wastewater stream leads to a rapid enzymatic reaction, due to which Zo is transferred into a bacterial culture with the subsequent production of poly-B-hydroxybutyrate, glycogen and/or other intermediate compounds-"accumulators" in the structure of the cells of active microorganisms with subsequent production of the glycocalyx (coagulable polysaccharide compound). Transferring the substrate from the liquid phase to the solid phase requires energy. In the conditions of the oxidative reaction, which are amenable to measurement, there is an accelerated increase in the rate of consumption of dissolved oxygen (the rate of oxygen use). The energy-oxygen equivalence is easily measured by introducing the mass of dissolved oxygen to the biomass, then the utilization rate is simply measured as the amount of dissolved s about OXYGEN Dependent on the time of measurement. As the ratio of Bo to Ho increases, the peak rate of oxygen utilization increases until a maximum value or plateau is reached. This is the first stage i) of the reaction, which also determines the mass and speed of removal of soluble substrates easily prone to decomposition.

The rate of oxygen use also corresponds to the rate of removal of the soluble substrate of the liquid phase, and this allows us to formulate their mutual energy dependence (Fig. 3). Measurement of wastewater decomposition using oxygen balance assumes that all reactions in which oxygen is consumed take place in the soluble substrate during biological growth reactions. Me

In a culture with dispersed growth, new microorganisms are formed, and other viable cells die due to endogenous metabolism, lysis, and predation. The total active share of the bioculture is related to the limiting share of non-degradable compounds, the age of muluiMSKT) and the loss of cell viability. Decreasing food availability (initial loading condition) or excessive (extended) aeration of a food-limited culture will cause intense loss of microbial viability.

The transfer of dissolved oxygen to the liquid phase in order to meet the oxygen requirements of mixed wastewater and bioculture is very difficult. The most important factors that must be taken into account are the chemical composition of the water, the features of the geometry and construction of the transfer device, the geometry of the pool (width, length, "depth of water near the edge), the power contribution per unit volume of filling the pool, the depth ratio in filling the pool to its filled area, total amount of soluble solids, residual

And the concentration of dissolved oxygen, temperature, surface tension, the average diameter of air bubbles, the time and delay of air bubbles in the liquid medium, the need for oxygen for the contents of the pool, the speed of the air flow through the oxygen transfer device, the ratio of the area of the air flow supply device to the total area of the bottom of the pool, distribution of oxygen transfer devices over the pool area, height above sea level, concentration

Ge" of bioculture, the age of the sludge in the system, the share of active microorganisms in the bioculture, the average size of the particles of the bioculture, the total rate of removal of dissolved oxygen by the biomass (read more: BIOVELOCITY). o For all reactions involving adsorption, absorption of nutrients, their metabolism in the direction of o formation of biological solid particles and the subsequent breakdown of biomass, oxygen and the speed of its use are the most important factors. Therefore, for the resulting rate of removal of nutrients with the help of se) oxidizing and reducing agents, for the resulting rate of accumulation of biological solid particles and for the total removal of phosphates by biological means, the supply of oxygen at an appropriate rate is a key element in the use of a cyclic treatment method that consists of stages of aerobic , facultative and anaerobic microbiological processing. The rate of oxygen supply, its total residual concentration and BIORATE, which are related to the distribution of zo/Xo, generally determine the factors of the total growth of various groups of microorganisms, which is usually described as the predominant formation of flocs or as filamentous (F, forms. Excessive development of filamentous forms leads to a result that is opposite to the purpose of processing, because this factor causes the destruction of the time scale of separation of solid particles from the liquid. Therefore, biological development must necessarily be associated with microorganisms that form mainly flocs. The option is also aimed at achieving this goal preferred process implementation and biomass processing control means based on set oxygen utilization rate values.

The removal of nutrients by any of the mechanisms: adsorption, biosorption, oxidation and assimilation with the final aerobic destruction of biological solid particles requires different proportions of oxygen. Total oxygen use is directly related to the relative amount of nutrients removed by each 65 OF THESE mechanisms.

BIORATE is a function of the conditions in the biomass and the nature of the soluble substrate in contact with the biomass. It is possible to produce a single-species sludge system to detect the maximum and minimum dependence of the biorate on the aeration time and the initial value of the Zo/Xo ratio. The active fraction of biomass affects the range of biovelocities that this biomass can detect.

To demonstrate typical absolute values and their changes, below are data obtained in a system of 5 consecutive constant volume reactors with complete agitation. mon and mon oi a 11 o! 10016 of 17777116 lived

These velocities were obtained for the presence of wastewater in the first reactor for 70 minutes with a total residence time of wastewater in the treatment reactor for 420 minutes. sch o nn nem p V PO PO PNYA OLIA POLON PO PN o z o z | Bioshdkst | 352 | 33 | 43 | BTe 53 | 744 | 704 800 | 47 (22)

Instantaneous values of the rate of oxygen utilization can be measured by the common method of table scales, in which the time decrease in the concentration of dissolved oxygen in oxygen-saturated samples of activated sludge removed from the operating reactor is measured. These are simple weighing studies, in which the sample must be taken from the me) pool of an activated sludge reactor, subjected to aeration and placed in a stirred reactor, inside of which there is a sensor for measuring the amount of dissolved oxygen; at the same time, the access of air is prevented. When the dissolved oxygen measurement device detects a decrease in the amount of oxygen, measurements of the amount of dissolved oxygen are made as a function of time.

Conventional respirometric monitoring of activated sludge processing is complex and indirect. Respiration rates are measured by a device that typically consists of a closed respirometric chamber with complete mixing, through which activated sludge is continuously pumped from a tank where the reaction takes place under the action of aeration.

The concentration of dissolved oxygen is periodically measured by an oxygen sensor near the inlet, as well as near the outlet of the respirometric chamber, which is achieved by changing the flow direction using a system of valves (one of the variants of the method).

The problem of measuring the oxygen content in activated sludge near the inlet and outlet openings of the respirometric chamber is that the oxygen content inside the chamber is significantly different from the oxygen content near the inlet and outlet openings, which leads to false measurement results. o The purpose of the invention is to create a device for wastewater treatment and a method of wastewater treatment, in which o the metabolic activity of biomass is maintained at a level that ensures the maximum rate of biological

Removal of nutrients by means of oxidation and reduction, by measuring ise) BIORATE inside the main basin of the reactor, and the measurements are carried out by recording the changes in the signal characterizing the oxygen concentration at the end of the aeration period.

A wastewater treatment plant is proposed, which includes a main reactor capable of keeping wastewater in contact with biologically active microorganisms that cause decay, a receiving device for receiving wastewater into the reactor, an oxygen transfer device through which air enters the main reactor, and controls the operation of the mentioned sequence and the necessary equipment, oxygen recording means for (F) recording relative changes in the amount of dissolved oxygen present in the main reactor, and control means for regulating the amount of oxygen supplied to the main reactor so that the activity of microorganisms is not limited by the amount of oxygen, present in the main reactor, for which oxygen is registered inside the main reactor.

A device or process is proposed in which biological cultures with dispersed growth are used for wastewater treatment and which include the following elements in combination with each other:

Means for maintaining the maximum potential BIORATE in the first non-aerated reaction zone for a culture created by mixing specified quantities of wastewater entering treatment and biomass in5 From the main and last reaction zone, means for introducing dissolved oxygen into the given zone(s) i) the main reactor for operation on pre-selected areas and with pre-programmed aeration periods,

means for interrupting the flow of untreated sewage to the first reaction zone, means for removing a portion of the supersludge clear purified water after a given period of no aeration, means for recording and measuring the position of the inner surface of the activated sludge layer, means for the interaction of the interface of biological solid particles in accordance with the depletion program of activated sludge and with registration of the position of the inner surface of the activated sludge, means for setting automatic time sequences for automatic operations, means for operating the main and last reaction volume as a fully mixed and variable volume device, means for measuring the biorate in the main and to the last response volume using a dissolved oxygen sensor appropriately placed in 7/0 of this pool volume, a means to measure the rate of change of dissolved oxygen concentration and compare it to the actual breathing rate in order to control the rate of injection of oxygen to the processing system, means of manipulation to maximize the ratio of the potential rate of oxygen use (determined by mixing a known amount of biomass from the main reactor with the wastewater entering the treatment) to the rate of oxygen use in the main reactor, means for automatically setting the duration /5 of the aeration period based on the results of measurements and calculations that take into account the actual respiration rate, means to optimize the use of aeration productivity to achieve nitrification and denitrification conditions, means to control the system by controlling the BIORATE to achieve maximum biological removal of phosphorus, means to conduct the process so that the main and the last aeration volume was operated at an approximately constant value of the effective rate of biological respiration (corrected for the active fraction of the biomass), a means of using the rate of decrease in the amount of dissolved oxygen obtained as a result of the interruption of the air flow to pool, and the algorithm for setting the biomass concentration to determine the parameter

BIOSPEEDS, means for removing near-surface supermud liquid from a depth, approximately 20 cm below the surface, with a constant speed to depths corresponding to a two-meter layer of liquid, in a pool with a depth of mainly 5-6 meters, and the shapes of the reactors allow placing the inlet devices near the edge of the pool or in the center of the basin, and for devices for draining treated wastewater allow transverse or longitudinal placement, due to which the device and process are used for the treatment of wastewater. and)

A wastewater treatment plant may consist of one or more reactors and at least one main reactor. In a preferred embodiment of the invention, the wastewater treatment plant consists of at least two reactors with fluid coupling means. In another embodiment of the invention, the installation consists of several reactors connected through a liquid, thanks to which various components, such as nitrogen, phosphorus, carbon and the like, accumulate and are removed from different reactors. In yet another embodiment of the invention, the oxygen content in each reactor is significantly different. co

In yet another preferred embodiment of the invention, the wastewater treatment plant consists of at least two reactors, and the first reactor has several zones that are typically not subject to aeration, due to which phosphorus absorption and biological release mechanisms are realized in it, and "the second reactor operates in the conditions of the cycle of oxygen - anoxic - anaerobic reactions for the microbiological decomposition of carbon compounds and compounds that determine the total nitrogen content in wastewater and for the microbiological removal of MO 3-M, MO"-M and the microbiological removal of phosphorus from wastewater water; both reactors are connected to each other through a liquid. "

In yet another embodiment of the invention, the wastewater treatment plant consists of one in s main reactor, and the conditions inside the reactor are cyclically regulated so that these conditions change from aerobic to anoxic to anaerobic and repeated using the definitions described above. ;" The means for recording oxygen can be any suitable means for recording dissolved oxygen. In a preferred embodiment of the invention, the oxygen recording means records dissolved oxygen

Oxygen. In another embodiment of the invention, the oxygen recording means is an electronic oxygen sensor capable of measuring the rate of change of the dissolved oxygen concentration in the form of a primary control signal of 4-20 milliamps with the help of a computer and another programmable logic controller that generates output signals that allow interactive control of the air input speed

Go! inside the reactor according to the given concentration profile. In another embodiment of the invention 5p, the oxygen concentration is perceived as a result of aeration of a mixture of wastewater and microbiological cultures in the main reactor. o Normally, the oxygen concentration is regulated during water treatment. In a preferred embodiment of the invention, the oxygen concentration in the mixture of wastewater and microbiological cultures is regulated during the aeration period. In particular, the concentration of available oxygen is regulated by adjusting the duration of the aeration period and/or adjusting the air flow during the aeration period. The air flow can be controlled with the help of the speed control mechanism of the air flow generator or in the air flow itself with the help of (Ф, the position control mechanism of the corresponding control valve or other means characteristic of the oxygen supply device. Controlling the air flow with the help of any means leads to controlling the mass rate of dissolved oxygen transfer to the main reactor. In a preferred embodiment of the invention, the oxygen sensor is placed inside the main reactor itself. The oxygen sensor is placed inside the mixture of wastewater and microbiological cultures. In another embodiment of the invention, the oxygen sensor is placed approximately 3 cm from any surface of the bottom of the main reactor. In yet another embodiment of the invention, the sensor can be placed in a pipe through which the biomass is pumped out of the main reactor. 65 In yet another embodiment of the present invention, the oxygen sensor calculates the actual absorption of oxygen in b assays based on the sum of endogenous or basic oxygen absorption and the rate of oxygen absorption during oxidation of easily biodegradable substrates, such as substrates in carbon and nitrogen form, depending on the microorganisms present and the age of the working sludge in the system, and in height above sea level and temperature are taken into account.

Experimental work showed that there is a relationship between the potential rate of oxygen use and the ability of sludge to settle, provided that the concentration of dissolved oxygen is not limited. In addition, there is a relationship between the value of the actual rate of oxygen use and the rate of reduction of the oxidation-reduction potential. The value of the effective rate of oxygen use, not counting the rate of endogenous oxygen use, is also related to the quantitative determination of the mass of the accumulated soluble and easily degradable 7/0 substrate that remains in the biomass, and the ability of this biomass to participate in the quantitative mechanisms of enhanced biological removal phosphorus One of the variants of implementation of the invention offers means for maintaining mass transfer of oxygen (due to aeration), which is approximately equal to the oxygen demand for biomass, and the use of these means for starting aerobic decomposition mechanisms with optimal use of oxygen transfer energy. Automatic means are also offered for setting the length of the aeration period, the mass of 7/5 Microorganisms to be introduced into the main reactor, setting the desired dissolved oxygen concentration profile according to the resulting set rate of oxygen use measured at the end of the aeration period; and the values of the ratio of the potential rate of oxygen use to the rate of oxygen use.

In yet another version of the implementation of this invention, a joint process of nitrification-denitrification is proposed until their practical completion, and mechanisms of enhanced phosphorus removal, which are well known to specialists, are proposed.

In one variant of the implementation of this invention, one or more reactors are proposed, the first of which, through the system connecting them, is supplied with liquids, one of which is a mixture of sewage and microorganisms that are in the sludge mixture of the last reactor.

In a preferred embodiment of the invention, a metered-load reactor volume is used which, despite the variable volume, operates during the aeration period essentially as a fully stirred reactor, during which time the flow is supplied of domestic sewage entering for i) treatment, and the flow of solid particles of the sludge mixture from the reactor volume with metered loading.

In a preferred embodiment of the invention, the mixture of wastewater and microbial cultures is passed through a complete aeration cycle. After that, the same mixture undergoes a cycle of no aeration, during which the layer of solid particles and the surface layer of liquid are separated. The sequence of events is completed by removing part of the surface liquid layer from the main reactor with the help of draining means. After that, the full b" cycle is repeated. co

In the variable volume activated sludge treatment method, which is preferred due to operation with full mixing and air supply and cut-off, it became possible to regulate and measure the me) respirometric capacity of the biomass directly in the main reactor. There is also an opportunity to check the progress of the treatment during the course of the reaction under the action of aeration, due to the interruption of the air flow and the subsequent measurement of the rate of decrease in the amount of dissolved oxygen.

The measurement of the oxygen utilization rate at the end of the period together with the comparison of the obtained process volume (relative to the minimum set volumes) provides the basis for automatic adjustment of the aeration cycle during the period, which effectively increases the organic loading and therefore the oxygen utilization rate. , as a guarantee for the biological consumption of phosphorus, after its release during other unfavorable conditions of the absorption reaction. ;" Usually, in real-time respirometry, the dissolved oxygen concentration is measured at the outlet of a respirometric chamber separated from the main activated sludge reactor, which is equivalent to

The concentration of dissolved oxygen in the respirometric chamber should not be speed-limited. If necessary, activated sludge must be aerated before entering the respirometric chamber. Typically, respiration rate is measured every minute after mass equilibrium of dissolved oxygen is established near a separate respirometric chamber. The actual rate of breathing is defined as the rate

Go! oxygen absorption in the main aeration tank. To measure this rate, activated sludge from the main reactor, where aeration takes place, is continuously pumped into a separate respirometric chamber and on a real-time scale, which is equivalent to measuring the average effective respiration rate in the pool of the main reactor with activated sludge, provided that the loading of sludge into the respirometric chamber is equal to its loading in the aeration tank. In order to maintain loading equivalence to the sludge flowing into the respirometric chamber, in a given proportion, wastewater is continuously added to it, which is received for treatment.

Owat - Oip Mgez/Mai, where

Owat - a portion of untreated sewage flowing into the respirometric chamber; (F, dFip - raw sewage flow; ka Mgez - volume of the respirometric chamber;

Uai - the volume of the aeration tank. 60 In all cases, real-time respirometric measurements are conducted under conditions of lower organic loading than that existing in the main reactor of the aeration unit. Therefore, several values of simple breathing rates have been established. The rate of endogenous respiration, which is typically defined as the rate of oxygen uptake by activated sludge that has been aerated for 1.5 hours without feeding.

The maximum rate of respiration is defined as the rate of oxygen absorption by activated sludge in conditions of an excess of soluble substrate (substance that is easily biodegradable). This rate is measured when a stream of raw sewage is continuously added to the sludge flowing into the respirometer chamber. The instantaneous respiration rate is defined as the rate of oxygen uptake by the activated sludge flowing through the respirometric chamber directly from the aeration tank with complete agitation. This speed is usually lower than the speed of oxygen absorption in the aeration tank, that is, the actual speed of breathing. The absolute value of the instantaneous breathing rate depends on the duration of the water stay in the respirometric chamber. The maximum rate of biomass respiration is also equivalent to its potential rate of oxygen use.

In one variant of the implementation of the invention, regulation of the actual breathing rate is used based on measurements made inside the aeration reactor (main reactor), and not with the help of a separate 7/o registration device operating on a real time scale, as is usually accepted.

In a preferred embodiment of the invention, the actual respiration rate is the sum of the endogenous or basal respiration rate and the rate of oxygen uptake in the oxidation of readily biodegradable substrate, in both carbon and nitrogen forms, the latter occurring when the nitrifying biomass is selectively grown . At the maximum rate of respiration, the activated sludge will be in conditions of /5 overload, which will result in incomplete removal of the substrate, easily prone to biodegradation. And this means that there is a critical respiration rate between the maximum and basic respiration rates, and at this rate, the quality of treated wastewater meets the requirements, and the removal of easily biodegradable substrate is satisfactory, among other parameters. At no time should oxygenation capacity limit speed. It is necessary that the kinetic processes in which dissolved oxygen is used, 2o end during the duration of the reactions, which will ensure the end of these reactions. In the case of nitrification mechanisms, the amount of transferred oxygen required by the oxygen demand must be satisfied by its supply per unit time, which is recorded and provided by measurements of the rate of respiration.

In advance, it is necessary to manually determine loading rates, actual breathing rates, and dissolved oxygen concentration. There is an advantageous situation when the actual breathing rate is always equal to or close to the critical actual breathing rate. In this case, the activated sludge is never overloaded and works at the maximum acceptable speed. Therefore, the total amount of activated sludge maintained in the system is i) optimal, and the metabolic activity of the biomass can be maintained at levels acceptable to assist other nutrient removal reactions. By manipulating the concentration of biomass, the duration of aeration and the rate of supply of oxygen demand, it is always possible to achieve a perfectly constant effective rate of respiration.

Specialists know many ways of managing wastewater treatment systems with microorganisms with dispersed growth. These methods involve the operation of one or more interconnected reactors with a constant volume, at least one of which is subjected to continuous aeration and a mixture of wastewater and microorganisms flows through it. The final basin in this system is a non-aerated "quiet" tank in which the solids are separated from the liquid, with the near-surface clear liquid being treated sewage and the bottom solids being sent to the waste and reagent tanks. . When repeating cycles, various internal flows also occur. As long as the variant of the invention is carried out in this configuration, it is not limited in its application. In a preferred embodiment, the invention relates to the use of a metered-rate reactor which, during the aeration period, operates "essentially as a fully stirred reactor, despite the variable volume, and during this time in 00 7-) from it is fed a combined flow of wastewater entering for treatment and a flow of solid particles of the sludge mixture from this reactor. ;" The preferred embodiment of the invention is formulated for the reaction conditions that are created, and not necessarily for the number of reactors and their zones through which the mentioned reagents pass. This is not a limitation of the embodiment of the invention. A portion of the volume, referred to as a fed-batch reactor, undergoes complete agitation during a particular aeration cycle, and kinetics characteristic of a variable volume with complete agitation can be applied to this volume. Next is the period of no aeration, and during which the layer of solid particles and the surface layer of the supersludge liquid are separated from each other,

Go! and their relative thicknesses depend on the history of the contact interaction of the wastewater stream entering for treatment with the concentrated solids flow of the sludge mixture, which is directed from the main tank se) with a variable volume, where complete mixing takes place, and is mixed with the stream of untreated sewage water o This variant of the operating mode requires means to remove a certain proportion of the upper layer of the supersludge liquid at the end of the period of no aeration. After the end of this operation, the aeration period is repeated with subsequent mixing of the reagents, as described earlier. 5B Without limiting the embodiment of the invention, the mode of operation of the batch reactor treatment method is most easily implemented in more than one pool module. The duration of the cycles of operation with aeration (F) is easy to set equal to 2 hours or another number of hours that is a multiple of two pools. Another duration of the cycles of work is set for three pools and their larger number, whether even or odd. Since the variant of the invention is not limited number of modules, it is easily explained using the example of two bore basins.If necessary, practitioners will be able to extrapolate from the two basin mode of operation used in this discussion.

While the volumes in front of the reaction zone have a large effect on the efficiency of the treatment method, the main requirement is that a significant fraction, greater than 5095, of the volume of the batch reactor is operated under fully stirred reaction conditions and variable volume, for which a special device 65 is used for the combined process of aeration and mixing.

Although a preferred embodiment of the invention utilizes a diffuse aeration system,

this option does not limit the application of the invention. Two variants of installations for the implementation of this invention will be described. Both configurations require the use of a dissolved oxygen sensor that has an acceptable time constant for measuring the rate of change in dissolved oxygen concentration (aО5/a0.

The previous discussion explained the importance of dissolved oxygen demand and supply under load, compared to substrate load, time of load application, and proportion of viable biomass.

The first configuration requires the use of a suitable dissolved oxygen sensor, complete with the electronics necessary to provide measurements of the rate of change of dissolved oxygen concentration as a control signal, through the use of a special computer or other programmable 7/0 logic controller that generates output signals that allow to carry out interactive control of the rate of introduction of air into the reactor with full mixing (and/or into other parts of the reactor connected by liquid) during the aeration period. Interactive control is carried out due to the regulation of the duration of the aeration period, together with the regulation of the air flow by the mechanism for regulating the air supply speed of the source, or the air flow through the positional mechanism of regulation of the corresponding /5 control valve, as a means of limiting the flow. Controlling the air flow by any means results in regulation of the mass rate of dissolved oxygen transfer to the reactor with metered loading and complete agitation.

In the first preferred embodiment of the invention, a minimum of one reactor tank is proposed, which is a metered-load reactor and operates as an activated sludge reactor in a variable volume basin. During the filling and aeration process, when more than one tank compartment is used, these compartments are fluidly connected.

An important feature of this invention is the method and means by which the wastewater to be treated enters the reaction means. Also important are the initial relative mass flow rates of activated sludge solids that are fed into the untreated wastewater stream. Next, the time of interaction of these components of the flow and the means by which mutual mixing and mutual coupling of these two flows are supported are important. One of the known methods uses i) propellers placed under a fixed or floating surface, which are set in motion by electricity and due to energy consumption, create a directed flow in which solid particles and liquid are mixed together. These means can also be used in this invention. In the preferred embodiment of the invention, there is no special equipment of the kind mentioned. Mixing is proposed to be carried out by various methods due to the operation of aeration means, which are necessary to support the processes of aerobic and anoxic decomposition, and/or to create conditions for a combined Me flow, with the help of pipelines, channels and guide partitions. co

As it turned out, the process has inherent advantages, the source of which are the means of introducing activated sludge and wastewater in certain proportions, the contact time of these two flows when flowing in a mixed state, and the way in which, during the initial period of the reaction, kinetic natural mixing is used in the contact . Without neglecting the application of this invention, the total initial reaction time is calculated to ensure the removal of at least 6595 of the readily degradable portion of the soluble substrate contained in the wastewater. This share of wastewater can be different. For example, for the biochemical oxygen demand of approx

ZOOmg/l and the associated chemical oxygen demand in bOOmg/l in domestic wastewater, and for a typical mesh "

Designs, the basic assumption that the easily degradable fraction of the soluble substrate is 2590, with c will give acceptable process results. The duration of the reaction is from twenty to about sixty minutes, which

And is determined by the retention time of the liquid inside the biological selection device, usually leads to a desired result, provided that the mandatory division of the input device into compartments provides a suitable degree of dispersion and, at the same time, the appropriate mixing energy, which increases the intensity of the formation of biological flocs and their aggregates . A feature of the invention is the placement of the partitions of the upper and lower b flows relative to the calculated lower water level and the bottom of the reactor basin. The open surface of the downstream baffle is limited, which allows the downstream flow to be created with an energy greater than three times the average energy of the flow over the spillway. The free surface of the lower flow uses

Go! share of the corresponding length of the lower partition. Thus, near certain areas of the bottom of the reactor

Energetic conditions for deep mixing are created. Further, in the upper part of the basin, there are zones of lower energy disturbance and aggregation, formed by spillway partitions. The geometry of the water inlet is designed to promote the formation of pulsating energy zones in which the transport and growth of flocs are ensured, and at the same time, the flow of biological reactions with the removal of soluble substances after the biochemical absorption of oxygen and from the transformation into products with intracellular accumulation, partial denitrification and release phosphorus with the help of microorganisms grown in biomass, which remove biological phosphorus.

While all of the processes mentioned above refer to a single tank variant, in a preferred embodiment (F) of the invention, a plant consisting of four (4) basins or four (4) modules is used. Each module can have from one (1) to M (where M»1) pools. Stopping the selection at 4 modules depends on the implementation (design) of a four-hour (4) cycle, based on which the geometry of the pool is designed. It is obvious to specialists that with the same right other selection numbers can be used, for example, C and 5. This design meets specific requirements for load distribution (hydraulic), regulation of organic load, biological treatment (including nitrification-denitrification and biological removal of phosphorus in one stream), provision of oxygen requirements by automatically regulating the biospeed, maximizing the efficiency of oxygen transfer, optimizing the separation of solid particles from the liquid depending on the depth, to which is being removed, and the speed of removal of treated wastewater. In any case, the preferred four-module variant operates as a purely continuous process, with the rising point being the reception of the wastewater to be treated, followed by the continuous discharge of the treated wastewater to the plant, the flow rate remaining at all times constant relative to the actual volume to the drained water reservoir, which is removed from each module. A different order can be followed, whereby the drain rate will remain the same in each drain period. A preferred embodiment of the invention is designed to operate with a flow that is split and fed into four modules (pools) for processing. The module can be given the form when wastewater is supplied for treatment at one end of this module (pool), and the discharge of purified water is carried out at the opposite or remote end of the module (pool), but the input and output devices are located on the long walls of the pool (see /about figures b(a)-6(9)). For typical domestic wastewater containing 300mg/l of total dissolved solids, 55mg/l of total Kjeldahl nitrogen content and to be treated to a degree of 6 x AOMUE, the area of the inlet devices should extend to 890 of the total tank area. This zone is divided into at least 5, and typically 8-14 subzones, for each main reactor, and each of them has a part of the volume in which the oxygen absorption rate for the first mixing zone is set from the very beginning to be more than 20 mg О 5" per g volatile /5 Ssuspended particles per hour. The volume fraction of suspended solids of the sludge mixture coming from the main reactor volume is typically greater than 2095 but less than 3395 of the average wastewater flow entering for treatment. On both sides of the reactor basin below the spillway, the device terminates, so half of the combined flow decays to this location on each side of the main reactor basin.

The pumped suspended solids of the sludge mixture continue to exist for the duration of the complete cycle. The flow of wastewater entering for treatment is interrupted during the settling period. The excess sludge is taken from the zone after the biological selection device, which is designed as an inlet device, and is removed during the aeration period or during the sedimentation period that occurs without aeration. The dimensions of the reactor basin are typically chosen based on up to 15 kg of solid particles suspended in the mixed flow, s per m? reactor area; and for the effective removal of nutrients from domestic wastewater - based on the calculation of the biochemical oxygen demand load of 0.33-0.40 kg of biochemical oxygen demand per m? despite the fact that the share of water that merges is 0.46. The speed of draining the liquid in depth reaches Svmm/min without the addition of means that precipitate phosphorus. With the addition of phosphorus precipitants, for treatment in normal dry weather, this depth removal rate can increase to 44mm/min. The load on the flow of solid particles in the pool reaches (ав) ABkg of solid particles suspended in a mixed flow per m and up to 1Okg of total nitrogen content per kg Fo of suspended solid particles per m2 per day with an accuracy of 2095 for the former and up to 30905 for the latter.

In another embodiment of the invention, the growing medium is added to the system to increase the biomass load to the volume that can be placed in the system. In this embodiment of the invention, the variable volume reactor is divided into three zones.

Zo Persha is the zone of the biological selection device, the dimensions of which for domestic wastewater are usually determined as described above. For organic industrial wastewater, the specified ratio increases and reaches approximately 1295 of the surface area of the basin. For effective subsequent removal of the soluble substrate, this zone, as mentioned, is divided into compartments. The first zone is followed by a second zone connected to it by liquid. The flow of solid particles of the sludge mixture in the reverse direction from zone C to zone 1 for deposits of untreated sewage, in which the biological oxygen demand reaches 200 Ω/l, or from zone 2 to zone 1, increases the average o) c flow by 2-3 times incoming liquid. The growing medium, which is arbitrarily packed into a cage, is placed in a "" flow passing through this cage. Zones 1 to 3 are permanently connected to each other by fluid. The "arbitrary" packing in zone 2 is approximately O0.4m from bottom of the reactor basin and within 0.15 m below the calculated lower water level. Zone 2 is coordinated with the means of varying the intensity of aeration, in zone 1 there are aeration diffusers connected to valves, which allow rough regulation of the process

Me. aeration and mixing. 2) It is obvious to specialists that the same nature of operation and management is used for wastewater treatment for the removal of only carbon, carbon and nitrogen, carbon and phosphorus, and for the removal of carbon, nitrogen and co-phosphorus. co 20 This device has been described with explanation, but many other variations can be made within the spirit and scope of the invention, which includes every new feature and new combination of features disclosed herein.

Those skilled in the art will recognize that the described invention provides options that differ from those specifically described.

It is clear that the invention contains all such options that fit within the limits of its essence and scope. iF)

Claims (41)

The formula of the invention is) 1. A method of processing waste that is at least a part of biomass containing active single-species 60 sludge in a bioreactor with variable depth, in which a regulated intermittent sequence of periods of aeration and draining of liquid is used for the simultaneous cultivation and maintenance of a culture of autotrophic, heterotrophic and facultative microorganisms in a sequentially aerated active single-species sludge for the biological removal of organic carbon, nitrogen and phosphorus components from wastewater entering the bioreactor, said biomass being placed in a working reactor with variable depth having at least two interconnected sequential zones, one of which is the first reaction zone , and the other is a second zone, in the implementation of which at least part of the treated content of this second zone of the reactor is returned to the partially segregated non-aerated volume from the first zone of the reactor for admixture with wastewater entering for treatment, at least during the operating period of the aeration os lower or second zone of the variable depth reactor, which is characterized by the fact that one dissolved oxygen concentration sensor or probe means is used to automatically and continuously monitor the concentration of dissolved oxygen in the biomass of the second or last zone of the variable depth reactor, and this sensor or probe means is placed in to such a place of the said biomass that at least the part thereof that is in that place is in motion during the time of automatic and continuous measurement of the concentration of dissolved oxygen, and this sensor or probe means is used to control the oxygen supply device during the arrival of sewage in 7/0 VRUGU or the last zone of the reactor and their aeration in this zone, the sensor or the probe means are used together with computer means to develop algorithms for converting the measurement results into a protocol for setting the dissolved oxygen concentration values, which are successively increased from zero to approximately 2.5 mg/ l during the day specific, adjustable increments of time to optimize the retention of adsorbed organic substances inside the biomass, to maintain the accompanying and optimal processes of nitrification and denitrification /5 during the aeration period, the release of phosphorus during the period of absence of aeration and the absorption of phosphorus during successive periods of aeration, when a reaction takes place in the wastewater, record and automatically calculate the rate of oxygen use by this biomass in the second or last zone of the reactor with a variable volume, due to which the duration of exposure of the biomass during each aeration period is regulated, and the mentioned measurements and regulation are characterized by the fact that the biomass in the second and last zones of the reactor has the potential rate of oxygen absorption measured in an aerated mixture of biological solid particles of single-species sludge with an admixture of untreated sewage is approximately three times higher than the value of the rate of absorption by biological particles of single-species sludge, measured by a resolution sensor of oxygen, and are such that, in combination with the predetermined oxygen transfer rate and the potential oxygen absorption rate, limit the oxidation of nitrogen, mainly to the form of nitrite nitrogen, and flow, due to mixing and variation in the second variable volume zone , the accompanying reaction of the reduction of nitrite nitrogen to gaseous nitrogen so that at the end of the aeration period, the rate of use of oxygen by the biomass is automatically set at i) the set operating point, and with the additional introduction of air into one or more partially segregated volumes in the first zone of the reactor, the release is partially limited of phosphate in the mechanism of biological removal of phosphorus in such a way that the first zone of the biological reactor is continuously and automatically controlled with the limitation of sequential flow of oxygen, anoxic and anaerobic reactions in this first zone of the biological reactor with variable depth. b" 2. The method according to claim 1, which is characterized by the fact that the waste is domestic, industrial or technical wastewater, including human waste products, wastewater from bathing, laundry and cooking, and their combination. and) 3. The method according to claim 1 or 2, which differs in that the volume of the last zone of the reactor is set greater than 5090 He of the total volume of the reactor zone and that in the first zone mixed or unmixed contents recycled from the second or last zone of the reactor are received, for admixture with waste that is sent for cleaning. 4. The method according to any one of claims 1-3, which is characterized by the fact that during the step of draining at a rate that does not cause the removal of sediment of solid particles from the layer of sludge that has settled in the reactor, up to 40 percent of the calculated depth of the reactor with variable depth from the village 5. The method according to claim 4, which differs in that during the period of aeration, the control valves are controlled by motors. work together, either a part of the valves is closed, or all the valves are open and closed according to a predetermined order of operation. 6. The method according to any of claims 1-5, which is characterized by the fact that the total oxidation-reduction potential of the liquid flow passing through the initial reaction zone acquires values in the range of -150 mV...-200 mV b compared to the standard hydrogen electrode. 7. The method according to any one of claims 1-6, which is characterized by the fact that up to 40 percent of the total volume of the bioreactor o is introduced into the first zone during a time equivalent to the duration of the cycle, which is less than the time period of removal of Go! fluid and on/off air supply. 8. The method according to item b or 7, which is characterized by the fact that the proportion of the main content of the reactor, mixed with se) untreated sewage, is sufficient to achieve values of the oxidation-reduction potential from -150 o mV...-200 mV for less than 80 minutes. 9. The method according to any of claims 1-8, which is characterized by the fact that the oxidation-reduction potential of the segregated sludge in the second or last reaction zone is generally in the range of -150 mV...-200 mV during 90 minutes of absence of air supply . 10. The method according to any one of claims 1-9, which is characterized by the fact that the concentration of solid particles F) of biologically active sludge in the second or last zone of the reactor is approximately 5000 mg/l. ka 11. The method according to any one of claims 1-10, characterized in that the biomass remains mobile for up to 10 minutes after the cessation of air or oxygen supply. in 12. The method according to any one of claims 1-11, which is characterized by the fact that the value of the concentration of dissolved oxygen is continuously automatically determined and recorded during the complete periods of turning on and off the air supply in each cycle. 13. The method according to any one of claims 1-42, characterized in that the operating cycles are controlled by measuring the rate of oxygen consumption to set Its values at the required level, which provide 65 stoichiometric oxygen demand for the reactor, which allows to alternately serve two zones of the bioreactor one source of air. 14. The method according to any one of claims 1-13, which is characterized by the fact that the total nitrogen content according to Kjeldahl in the activated sludge reaches approximately 10 kg of TCM/KoMI 58/M 2/4 for the treatment of typical domestic wastewater. 15. The method according to any one of claims 1-14, which is characterized by the fact that the total content of phosphorus in solid particles of activated sludge reaches approximately 2 kg of phosphorus/comi 58/M 2/4 for the treatment of typical domestic wastewater. 16. The method according to any of claims 1-15, which is characterized by the fact that the concentration of dissolved oxygen in the main reactor is regulated to a level not lower than 0.7 mg/l (on average) during 75 percent of the duration of the air supply period and to values from 2 to 3 mg/l for the rest of the duration of the air supply period. 17. The method according to any of claims 1-16, which is characterized by the fact that the microbial treatment of wastewater 70 is additionally carried out in the presence of a population of microorganisms that have adapted to wastewater pollutants and their concentrations in wastewater, which include nitrifying microorganisms capable of convert nitrogen to at least o nitrite nitrogen, facultative microorganisms capable of denitrifying nitrites, and optionally nitrifying organisms capable of converting nitrite nitrogen to nitrate nitrogen, and facultative microorganisms capable of reducing nitrate nitrogen to nitrite and to gaseous nitrogen, and microorganisms that 75 remove phosphorus, capable of biological removal of available soluble phosphorus. 18. The method according to claims 1-17, which is characterized by the fact that the concentration of solid particles in the sludge mixture in the second reactor is measured and recorded at the moment of stopping the air supply to this reactor, and the oxygen absorption rate is measured, recorded and analyzed immediately after the end of the oxygen supply, and the liquid level - at the moment of closing the valve through which raw sewage passes to the reactor, plus approximately two minutes. 19. The method according to claims 1-18, which is characterized by the fact that the measured parameters of the process are processed and used to determine the duration of sludge pumping, the duration of the air supply period during the next cycle, the mass flow rate of air in the next cycle, the selection of the set values of the dissolved oxygen concentration in this way , so that this mode of operation is sufficient to maintain the set values of the oxygen absorption rate in the main reactor, determined according to the results of measurements carried out at the end of the previous CM aeration period. at 20. The method according to any one of claims 1-19, which is characterized by the fact that the pH correction is carried out in the waste water received for purification. 21. The method according to any one of claims 1-20, which is characterized by the fact that the path of the flow of mixed components from the first zone of the mixing bioreactor consistently passes near the bottom of this reactor and further to the surface liquid "25 in the reactor on its way to the first bioreactor, due to which the mixing energy, which is associated with the flow path near the bottom of the first reactor compartment and which is at least 3 times greater than the mixing energy Ф associated with the flow path near the liquid surface, leads to successive local (ee) energy pulsations, nucleation and floc formation in a mixed flow. 22. The method according to claims 1-21, which differs in that the given rate of oxygen absorption is determined experimentally, and, as a rule, it is within 2054 mg О 5/9у55/yg (mg ОО" per gram of volatile "(0 suspended particles per hour at 207). 23. The method according to claim 21 or 22, which is characterized by the fact that the rate of oxygen absorption or the measured potential rate of oxygen absorption in the primary mixing reactor is at least 20 mg O5/d955/Ppg. " 24. A device for the biological removal of carbon, nitrogen and phosphorus from wastewater, which contains a partially closed water-retaining multi-zone cyclically aerated reactor with variable depth, which includes - with at least the first hydraulic zone and the last hydraulic zone, made with the possibility of transferring liquid between the zones and at least during a portion of the aeration cycle, an aerator for selectively exposing the reactor contents to air during the aeration and deaeration cycles, characterized in that the first hydraulic zone has an inlet for supplying thereto wastewater to be treated, at least during the air supply cycle, with the hydraulic zone designed to separate waste water at least with (o) the possibility of separating clean surface liquid, the aerator includes an air purge system installed on the bottom of the reactor, designed to simultaneously mix and carry oxygen in at least the last hydraulic zone , and means of directing the flow in working air to the reactor to carry oxygen inside (ee) the reactor with at least two different flow rates during the air supply cycle, means for stopping the incoming wastewater flow at least during part of the air supply cycle, means for draining fluids from the last hydraulic zone to a location remote from the reactor, at least during the air shutdown cycle 62, means for transferring the contents of the last hydraulic zone to the first hydraulic zone at least during the air supply cycle, means for blocking the inlet flow of wastewater and the flow of operating air entering the reactor for at least part of of the air shutoff cycle, means for reducing the volume of cleaned surface fluid contained in the last hydraulic zone during the air shutoff cycle to a predetermined lower level by means of a motor-driven separation device comprising horizontally mounted liquid receiving means equipped with catch of positive solid i.e.) particles floating on the surface of the liquid, except for skimmers, connected through at least one drain element to a rotating drum shaft equipped with water-retaining gaskets and pipes 60 for removing air blockage, means of automatically maintaining an optimal mixture of working acclimatized heterotrophic, autotrophic and facultative microorganisms and wastewater by continuously measuring the rate of change of the dissolved oxygen concentration in the reactor together with the measurement of the potential rate of oxygen uptake by the biomass, the rate of change of the dissolved oxygen concentration being measured by means of a dissolved oxygen sensor or probe installed in the biomass such that at least part 65 biomass is in motion at the time of measurement in order to display the absorption rate as a function of time, means for analyzing the rate of successive changes in dissolved oxygen concentration determined at the end of each air supply cycle in the last hydraulic zone, means of continuous measurement of the rate of change of dissolved oxygen concentration at the beginning of each air supply cycle, means of setting set values of the rate of change of dissolved oxygen concentration in the last hydraulic zone of the reactor taking into account the speed of the working air flow, means of setting the duration of the air supply cycle and a mixture of heterotrophic , autotrophic and facultative microorganisms, means of setting and processing set values of dissolved oxygen concentration as a function of time profile in each air supply cycle in the last hydraulic zone in order to determine the cessation of obtaining suitable set values of the rate of change of dissolved oxygen concentration during the air supply cycle, means of automatic setting durations 7/0 of each completed cycle and the next cycle, means of determining and processing the values of the duration of consecutive cycles of stopping the air supply among the values of the duration of consecutive cycles in the last gi wood zone, means of determining and processing the speed of the flow of working air entering the reactor as a function of time, as well as means of determining and setting the duration of the operation during each cycle, aimed at removing a given volume of the mixture of biomass and wastewater from the reactor in successive cycles stopping the air supply. 25. The device according to claim 24, which is characterized by the fact that the second or last zone of the reactor is equipped with oxygen transfer means located on the bottom or near the bottom or base of the main reactor. 26. The device according to claim 25, characterized in that the bioreactor is equipped with at least two vertical pipes for air supply and motor-controlled control valves in such a way that the latter can be alternately opened according to the mentioned air supply control program during a cycle with 2 o subsequent closing. 27. The device according to any of claims 24-26, which is characterized by the fact that a bioreactor is used with vertical walls that are made of reinforced concrete or structural steel, or a reactor in the form of a sump with inclined walls made of clay, reinforced with concrete, lined with an anti-filtration coating or walls supported by concrete. with 28. The device according to any of claims 24-27, which is characterized by the fact that an electronic oxygen sensor is used as a dissolved oxygen concentration sensor or probe, capable of measuring the rate of change in the concentration of i) dissolved oxygen in the form of a primary control signal. 29. The device according to any of claims 24-28, which is characterized in that the dissolved oxygen concentration sensor or probe is placed inside the second reactor, at a distance of about 30 cm from the bottom surface of the second reactor, or in a pipeline with pressure flow, or in the pipe, through which part of the suspension of solid particles in the liquid flows from the second reactor to the reactor into which untreated wastewater is introduced. b" 30. The device according to any one of claims 24-29, which is characterized in that it uses up to four bioreactors or up to four modules forming a bioreactor, and a flow distribution system for feeding the wastewater received for treatment to each bioreactor or to each of the four bioreactor modules so that each of the 5 modules operates as a separate equivalent bioreactor. co 31. The device according to any one of claims 24-30, which is characterized in that each bioreactor has a place for the inflow of untreated wastewater and a device for the inflow of impurities, as well as a device for draining treated wastewater, which contains a channel for receiving a moving liquid, made with the possibility of removing surface material in an amount up to 4095 reactor depth. " 32. A device for the biological removal of carbon, nitrogen and phosphorus from wastewater, which includes a partially closed water-retaining multi-zone cyclically aerated reactor with variable depth, which includes at least a first hydraulic zone and a last cyclically aerated hydraulic zone, which have in common;" maximum upper water level, designed to allow liquid transfer between zones at least during part of the air supply cycle, an unaerated initial reaction zone, an aerator for selectively subjecting the reactor contents to time-controlled repetitive cycles of air supply on and off, Ge" characterized in that the aerator comprises a grid system for generating air bubbles installed at the bottom of at least the second or last zone and means for directing the flow of process air to the reactor o for intra-reactor oxygen transfer at at least two different mass flow rates during the o air supply cycle, an inlet for supplying wastewater of incoming material to the mentioned first 5r Non-aerated zone, in the mentioned second or last zone - means for enabling the separation of wastewater and, material into at least the overhead flow that has undergone treatment, means for blocking the flow of wastewater from the incoming material to the first zones at least during the combined liquid separation and treated wastewater removal cycle, a valve or pump for removing the liquid contents from the second or last zone at least during the air-off cycle, a channel for transferring the liquid contents from the last zone to the first zone at least during the air supply cycle, control means to block the flow of incoming waste material and the flow of process air to the reactor at least during the combined (F) cycle of liquid separation and removal of treated wastewater, a movable spillway for collecting wastewater of treated water to reduce the depth of the liquid in the last zone during the air shut-off cycle to a predetermined lower level using a separator (9), which contains a horizontally placed rectangular drain box filled with a foam barrier, connected at least one downspout element with a rotating shaft of a drum equipped with water retention we are gaskets and pipes for removing air blockage, in which the device additionally contains a sensor (15) or a probe for determining the position of the surface layer of the sedimented biomass sludge in the second or last zone, a sensor (13) or a probe for measuring the concentration of biomass in the second or last zone, a sensor or probe for determining 65 the oxidation-reduction potential of the biomass in the second or last zone, control means for operating between the variable positions of the liquid level set points indicated as the lower (8) water level and the upper (7) water level, sensor (12) or probing means for measuring the dissolved oxygen concentration and the rate of change of the dissolved oxygen concentration of the biomass in the second or last zone, whereby a single sensor for determining the dissolved oxygen concentration is placed in the moving biomass, a programmable controller for the determination and analysis in successive cycles of successive rates of change of oxygen concentration taken at the end of the cycle of turning on the air supply in the second or last zone (4), automatic adjustment of the operating time during each complete and successive cycle, operation and determination of the duration of the cycle of turning off the air supply during successive cycles in the second or the last zone and determining and using the execution time of each cycle to remove a predetermined volume of the mixture of biomass and waste material in successive /o cycles of turning off the air supply from the second or last zone. 33. The device according to claim 31 or 32, which is characterized in that the bioreactor (1) is equipped with at least two air supply pipes and motor-controlled air supply control valves in such a way that the motor-controlled latter can be opened sequentially and/or alternately according to a given program control the air supply during the cycle and then close. 34. The device of claim 33, wherein all of the air control means are operated in concert during the aeration cycle, or some of them are closed, or all of them are opened and closed according to the presented sequence of operations. 35. The device according to any one of claims 31-34, characterized in that the dissolved oxygen concentration sensor or probe is an electronic oxygen sensor capable of measuring the rate of change of dissolved oxygen concentration. 36. The device according to any one of claims 31-35, characterized in that the second or last zone (4) is more than 50 percent of the total volume of the bioreactor. 37. The device according to any of claims 31-36, which is characterized by the fact that the bioreactor is made with vertical walls of reinforced concrete (1) or structural steel, or the reactor is in the form of a sedimentation tank with inclined, clay, reinforced concrete, lined with an anti-filtration coating or held with concrete walls. 38. The device according to any one of claims 31-37, which is characterized in that the dissolved oxygen sensor is placed in i) the second or last zone (4) or in the pipeline with pressure flow or the pipe (10) through which part of the content flows from the second or last zone to the non-aerated zone (3) for mixing with the wastewater entering for treatment. about zo 39. Device according to any one of claims 31-38, characterized in that each bioreactor has a place (11) for the inflow of wastewater, for example in the form of a pipeline, a zone (3) for the incoming mixture, and Me) a separation device (9) with a motor drive, which contains a horizontally movable rectangular liquid receiving chute, designed to remove material floating on the surface, connected by means of a chute element to the rotating shaft of the drum, which has suitable o c5 water retaining gaskets and pipes for removing air blockage, appropriate sensors for measuring MI 55 concentration, oxidation-reduction potential and determining the separation surface of the sedimented sludge layer, level indicators and adjustable positional limiters for determining the variable working upper and lower water levels for each cycle. 40. The device according to any one of claims 31-39, which is characterized by the fact that the biomass contains an added medium « 70 Cultivation, stationary or mobile in one of the two zones of the reactor. in the village 41. The device according to any of claims 31-40, which is characterized by the fact that the size of the reactor basin is approximately 18 kg of MI 55 per square meter of its bottom area. ;" (22) (95) (ee) o 50 (42) F) ime) 60 b5