DE2552384A1 - SYSTEM FOR SUPPRESSING WALL PRESSURE IN A LINE - Google Patents

Description

System for suppressing hot water pressures in a pipe

Sin suppression of the surge to dampen pressures or hammering by introducing gas into a flow line in such an amount that the gas introduced exceeds that which is necessary to saturate the liquid is. Preferably these gases are those which are relatively inert and not overly reactive and have relatively low saturation values with respect to the liquid. The gas should have a link to the Flow line can be added near a high turbulence. The suppression of the wave can in general with a liquid system and especially with a liquid

809843/027 $

BORO MONKS: TELEX: TELEGRAM: PHONE: BANK ACCOUNT: CHECK ACCOUNT: 8 MONKS 22 1-85844 INVENTION BERLIN BERLINER BANK AQ. W. MEISSNER, BLN-W ST. ANNASTR. 11 INVEN d BERLIN 030/888 60 37 BERLIN 31 12282-109 TEL: 089/228844 030/888 23 82 3695718000

transmission system can be used.

Another embodiment relates to a sprinkler egg or scrubber for purifying gases and may include an or contain two steps to remove impurities, e.g. through the use of easily soluble liquids, knock down the dirt or catalysts (heating stages) to knock down the dirt, contain oxidizing or reducing agents. The barrage egg includes a packed pad and packing can be identified as such where the hydraulic inner radius is equal to the hydraulic radius of the outer flow channels is. The scrubber or sprinkler egg is especially for treating (cleaning) materials like ozone, which is suitable in a deodorizing or disinfection system is used.

Another embodiment relates to the purification of a gas by treating it with a fluid (i.e. gas or liquid) in a flow line with a plug outlet at its inlet which is an injector mixer contains, with a first, a high turbulence causing device and a second or behind such a facility works together. The treating fluid is preferably at the Vena contracta supplied to the first facility.

The invention relates to a two-stage oxidizer for disinfecting material, the nitrogen in the form of ammonia or ammonium for operating waste or sewage treatment plant effluent through Adding a primary oxidizing agent to the drain and a secondary oxidizing agent to the Creation of a synergistic disinfection system, in

609843/0 2 78

which shifts the distribution of ammonia or ammonium to almost all of the ammonium. A desirable one pH is 7 or below, with the desired primary active ingredients being aluminum chloride or ferric chloride and the secondary active ingredient contain chlorine, chlorine dioxide, ozone in oxygen or air, or sodium hyperchlorite.

The invention also relates to the nitration of ammonia in the form of a secondary treatment effluent from a waste treatment plant in which the ammonia in Nitrates is converted, so that the runoff has a low .lUDmonia content.

A rotary distributor arm with improved distribution nozzles and a flow control that is controlled by a stepped pin takes place to the arm itself, ensures an even distribution over the entire radius of the distribution medium, so that the uniformity and optimal economy and optimal efficiency in relation to the sprinkling filter itself is achieved because a uniform fluid is distributed over the entire upper surface.

The invention also operates an injection-Bischanlage in a contact container, the good mixing devices for Disinfect and use a unique flow arrangement in the inflow channel as well as in the contact container, whereby a maximum dispersion of the disinfectant is achieved through the influence with the greatest economic efficiency will.

The application is an addendum to US patent application serial no. 355.738 "System for Pollution Suppression" from April 30, 1973 »which in turn is an addition to the US patent application Ser. No. 100.333-dated December 21, 1970 is

609843/0278 _ * _

552384

it.

the meanwhile tin US patent 3 «730,881 led hai
This, in turn, is an addition to the patent 3 · 54-9 ·? 28 of December 22, 1970, which is an addition to the patent application
over. No. 362.118 of April 23, 1964, which did not result in a patent.

The invention relates to a surge suppression system for preventing surge pressures or hammering In liquid systems. In particular, the invention relates to the suppression of surge pressures during pumping of liquids.

So far, various techniques have been used for stripping wall pressing or pipe hammering ή η liquid systems used in which a pump is usually used. Most of these techniques are complicated, inefficient or impractical and reduce the '.val pressure not sufficient in the system. One such technique uses a flywheel to add inertia to the pump motor. Another technique is based on the use of a standpipe, which is either a standard pipe or a Differential pipe can be - ^ this type is common as a means of protection against negative pressures when regulating the flow in pressure pipes or hydraulic turbines appear. Another technique requires a storage tank or an air vessel. A variation of this technique is a so-called disposable storage container, i.e. a storage container, which is provided with a non-return valve, which allows a flow only with a line negative pressure or the like. Another change in storage technology is the use of a very small storage container, which can be a water container open to the earth's atmosphere.

609843 / 027S - 5th

The invention also relates to the use a sprinkler system for general cleaning of a gas barrier, in which the hydraulic radius of cylindrical members in the egg is equal to the hydraulic radius of the outer fault channel is. In particular, the invention relates to a sprinkling or washing system in the one or two stages of purifying a gas connection through the use of highly soluble liquids or oxidizing or reducing agents can be used.

Heretofore, sprinkling eggs with wrapped pads or the like have been used to facilitate the absorption of a liquid phase to bring about. Although undesired mixture removal is effected, efficiency generally does so of the process by restricting the hydraulic loading, by compromising between gas and liquid flow or reduced by excessive pressure drop in the gas phase system. In relation to cleaning Liquids were used that are not readily soluble. There were also solids like activated carbon and thus periodic replenishment was necessary.

The invention relates to treatment or purification a first fluid with a second, if possible a gas, the first being under turbulence is in a line. In particular, the invention relates to cleaning a first fluid by another (gas) in a line, in which eddy currents a mixing or a moment transfer cause.

So far, liquid phase treatment systems have been used for

S09843 / 0276

Holding liquids or fluids generally used as liquids or gases. When cleaning a Gas by other gases was generally cleaned in contact chambers, packed documents and the like The treated fluid circulates in these systems through the chambers and the treating fluid comes into contact with the treated on the packed Document. Where the active ingredient for the treatment is a gas, it will be dissolved in the treating liquid. Of the Contact takes place as before. There is also direct contact between a treating gas and a treated one Fluid possible. Although cleaning is done, the amount leaves something to be desired.

The invention relates to a synergistic two-stage oxidizer for disinfecting materials. In particular, it relates to such a facility that a primary oxidizing agent in one stage and a secondary oxidizing agent in a second stage Used to treat waste or sewage.

So far, in disinfection and mainly in relation to the treatment of waste and waste water have been oxidizing Active ingredients used for disinfecting. The use of the various oxidizing agents gave up, however also in combination mainly a reduction in bacteria proportional to the amount used or to the Set of multiple connections. Furthermore, the effluent treated usually had a lot of ammonia, the ammonia itself a lot of secondary ammonia oxidizing agent or which required further extensive treatment to remove it from the It is necessary to plant and prevent it from being released into streams or watercourses, where it has a highly toxic effect on fish and marine animals. In addition, there is strong removal of ammonia by venting

S09843 / 0278

2bb23B4

to .Earth atmosphere because of the smells and pollution undesirable.

The invention relates to a plant for generating of runoff from low ammonia treatment. In particular, the invention relates to such a plant in which the secondary effluent is to a nitrification tower given via a special distributor, ventilated according to a special process and through Iuedien is filtered with special hydraulic parameters, whereby the nitrification tower is isolated.

So far, various methods of converting ammonia to ammonium nitrogen have been used in treatment plants used by ii. waste and sewage. These procedures are generally complicated and expensive and cannot be done all year round.

Summary of the invention

It is therefore the object of the invention to provide a system with wall suppression, in which a gas in a Liquid at one point in the flow system in one Amount is introduced which exceeds the value of the gas saturation of the liquid.

Another object of the invention is to provide such a system in the facilities that have a strong Cause turbulence, are located in the line system of the liquid, which coincides with the gas introduction points.

Additional turbulence devices should be located behind the gas introduction turbulence devices. The plant for V / a Hunt suppression is intended for use in fluid transmission systems be suitable. ."G

2 b b 2 3 B

According to the invention, the Unterdrückungsanl & containing ge an Agitation or power transmission line with a liquid, comprising introducing means for a gas in the Wetz or the line, and aie amount of the introduced gases exceeds necessary to saturate the liquid, "narrow, ./alldrücke order to ' dampen.

It is therefore the subject of the invention an egg for .Reinigen a gas for the use of fluids indicate with preferred and good solubility, which causes a precipitate if possible, or catalysts contain or are heated to promote the precipitation, uni oxidizing or reducing agents knock down.

Furthermore, the irrigation eggs are said to be the usual ones for cleaning a gas or contain special packaging and the hydraulic liadius of the outer otröuiungskanal should be the same be that of the inner channel. -.ui;. he should also have an or two stages included. The respective gas is here with ozone.

In general, the invention relates to a method for purifying a gas with supplying the gas a contact area for injecting a mixture, the sprinkling egg containing a packed pad, with feeding a fluid to the irrigation eggs selected from those selected from the group consisting of detachable oxidizing and reducing agents, direct the gas through the packed substrate and expel the treated gas.

The subject matter of the invention is therefore an arrangement for treating a fluid with a device indicate that causes turbulence to increase contact. This device is located in the direction of the flow seen behind the plant.

609843/0276

^ 552384

A fundamental object of the invention is to provide a facility for treating an otrömungsinmittel, in which the injection mixture and the contact is carried out under precisely regulated conditions of the flow, UE. the contact opportunity as large as possible and the notwen ^{r 'n'} ge ^T oncentration the required treated fluid (gas as small as possible to make This is done as follows: injection and Idischen so daP d ^A e concentrate 'ons ^r;. Radients in the axial direction are suppressed in the angular direction where intense radial mixing of a turbulence device and with a high concentration gradient in the radial direction because of the coaxial injection of the treating fluid (gas) into the fluid being treated (Liquid or gas ^{N is} induced, whereby it is recognized that the radial concentration gradient in the direction of flow behind the injection point is weakened in an overhang length, the distance /. To build up a stable velocity profile in the turbulent flow is 25 to 50 diameters and preferably at least 50 diameters , then suppressing a residual radial concentration gradient at the E. nde the transition section is suppressed, and a second turbulence device is used. This causes a radial wobble, so that a residual radial concentration gradient is suppressed, if the second turbulence device is an opening in a flat plate, another problem comes into play. That is, the opening in the flat plate is one of the few, if not the only, turbulence devices that direct the laminar and turbulent boundary layer away from the conduit wall, mixing it into the main stream of treated fluid flow. With this facility, the greatest possible contact between the treating and the treated flow can

S09843 / Q276

- 10 -

- ίο -

medium lasting for a time that varies from reaction rates depends, because of the suppression of concentration gradients and the intense mixing the reaction rate is very fast, which affects the contact time and concentration for the fluid being treated (Gas) makes it very small.

In general, the invention relates to "a method of treating a fluid with delivery this to a flow line, so that the Reynolds term is at least 3000, the conduit having a turbulence device, and with supplying a treating fluid to the fluid channel and expelling a treated fluid.

It is therefore the object of the invention to specify a two-stage oxidizing plant for disinfecting material, containing a distribution of ammonia and ammonium, a primary and a secondary oxidizing agent being used. The ph value of the material should be this is reduced and synergistic disinfection results are obtained. The system is intended for the treatment of drinking or serving water, waste or sewage. The primary one oxidizing active ingredient is used here in the first stage and the second oxidizing active ingredient in the second stage. The distribution of compounds of ammonia and ammonium is shifted significantly to ammonium.

The invention relates to a two-stage oxidation process for disinfecting material that contains a distribution of ammonia-ammonium compounds, and consists of delivering a primary oxidizing agent to the material for disindication and degradation the pH value of the material and the supply of a second

609843/0276

- 11

The oxidizing agent in order to minimize the number of bacteria to obtain, where the jnmoniak-iiininoniuin distribution to the ^ aninonium is moved. Here the iiinmonisk in the secondary treatment outflow of an ibfall— Treatment area weakly oxidized to stabilize nitrates.

Another object of the invention is a .rOisfluss in a waste treatment plant, the by using a distributor, a ventilation device and a packing base with special hydraulic parameters has a low .onmonia content.

In general, the invention relates to a waste treatment plant for weak jimonia discharge with a mitrification tower, containing a packaged pad, to the delivery of secondary treatment effluent Nitrification tower that is ventilated and dissolved oxygen contains, the aem discharge through a small ear, in which is a Turbulenzeinriehtung, added v / ird.

The drawings serve for a better understanding of the invention. In these is:

Figure 1 is a block diagram of the proposed system as a whole with the flow arrangements and the stages:

Figure 2 is a plan view of an improved sedimentation tank with one of the stages of the system;

ifpar 3 is a cross-section of the settling container according to FIG. 2 on line 3-3 »

2552

Figure 4- a schematic (cross-section of an improved Sprinkler filter with one stage of the system according to the invention;

FIG. 5 shows a flow diagram of the disinfection device, those under a hydraulic gradient with sensors and a gas inlet control is operated;

Figure 6 is a cross-section in a larger Iviaßstab one of the Openings in a flat plate of the disinfection device according to - ^ igur J? j where the gas inlet and the stitch relationship to the opening has the greatest efficiency when introducing the disinfectant gas and get the greatest elimination of concentration gradients;

FIG. 7 is a flow diagram of another basic system with improvements and flow control;

FIG. 8 is a graphic representation of the hydraulic and organic loading of the influence;

FIG. 9 is a graphic representation of the optimal flow rates for case A with constant treatment flow, a fixed flow quality and solid hydraulic-organic loading;

FIG. 10 is a graphic representation of the improvement of the flow loading system in cases A, B and G, included in the description;

609843/0

- 13 -

Fig. 11 is a representation of the ball O, which is also in the Description is explained;

Figure 12 is an end cross-section of the drilling means used in the sprinkling filter can be used;

FIG. 13 a -..- cross-section on a larger scale of a short one Pipe with the injection device to achieve good iridescent or gas-as-a-liquid mixing characteristics;

FIG. 14 a cross-section of the container that covers the bottom of the Sprinkler filter crossed, and shows how a corresponding ^ storage active ingredient in the otrö-Bimittel can be entered;

15a © in * iuer section of an injection mixer elbow; 15b shows a cross section of a unit with an opening;

Fig 15c a ^ ^uerscnn I't "^':' an opening in a flat plate;

FIG. 16 is a schematic representation of a two-stage sprinkler;

Fig. 17 ^ a cross section of a treatment plant for a fluid with such a high efficiency and the use of facilities to generate high turbulence;

FIG. 17B is a schematic illustration of a gate in FIG part of the complex;

Figure 18 is a diagram of the relationship between B _e temperatures, pH, and the equilibrium between ammonium and ammonia;

FIG. 19 shows the cross section of a nozzle;

FIG. 20 the top view of a large distribution arm Diameter and its pivot pin;

Figure 21 is a front view of the distribution arm of Figure 20;

FIG. 22 shows a view of the arm alone with the dashed representation of the internal structure;

FIG. 23 shows a view of the arm according to FIG. 22;

FIG. 24 is a partial view, on a larger scale, of the nozzle arrangement in the circled area of FIG. 23;

Figure 25 © in cross-section on a larger scale on the line 25-25 of Figure 22;

Figure 26 is a modified dual flow channel similar to that shown in cross section of Figure 25;

Figure 27 is a larger-scale cross-section showing

like the flow path in the distribution head the double flow channel according to ^ igur 26 results;

FIG. 28 shows, on a larger scale, the distribution nozzle in the distribution arm according to FIGS. 20 to 23;

Q 9 8 4 3 / Ö 2 7 6

FIG. 29 is a side view of another sweeping arc which can take the place of the distribution nozzle according to FIG. 28;

FIG. 29A shows a view of the sweeping arc according to FIG a flattened outer end;

FIG. 30 is a diagram of the optimal concentrations of Polyelectrolyte feeds for maximum removal of suspended bodies;

Figure 31 is a view of a contact container with the preferred one Injection mixing system according to the invention;

FIG. 32 is a cross-section on the line 32-32 of FIG. 31 The container is shortened in length according to Fig. 31 is;

FIG. 33 shows a partial cross-section of the contact container on the Line 33-33 of Figure 31;

FIG. 34 - a partial view on a larger scale of the injection l'.ischbogen, which is used in the container of Figure 31; and

Figure 35 is a schematic representation of an activated Sludge air injection system.

The disinfection of alkalines, flavobacteria, microcokes and enterobacteria

All types of bacteria make an activated sludge,

*
however, ordinary plant anaerobes reduce the number

according to the air available. A protein waste

609643/0276

■ - 16)

favors alcalins, flevobacteria and bacilli. A Hydrocarbon waste profiles pseudonomies.

Anaerobic overlooks

The anaerobic work-up bacteria contain facultatives and condition anaerobes in active metabolism. It can be dormant aerobic forms, like spores from mushrooms give. Acid build-ups are predominantly facultative forms, although there are few obligate anaerobic metabolites and products who are pissed off.

Methane images are obligatory anaerobes, methanobacteria, Methanosarms and methanococci in the metabolic pathway to follow end products of which methane is a precursor is. Because of the particular vulnerability of methane images to oxygen, oxygen-ozone or air be crossed. The selective disinfection thus provides a means of preventing the formation of methane or to negate a metabolic pathway to subsequent end products where methane is the necessary precursor. In the negative, one path can change another path by changing it environmental conditions such as aerobic activity. In this way no methane would be produced. The source material carbon dioxide would not be reduced. This is an unnecessary step in the process Waste treatment, as carbon dioxide is a stable end product aerobic treatment is. The hydrogen contained would not be effected. He is likely a component of formic or acetic acid .. The alternative metabolic pathway opened is that for the aerobic microbiological precipitation of acetic acid. Instead of the anaerobic consequent acetic acid / acetic acid Acid to acetoacetic acid-isopropanol or to butyric Acid developed the invention the aerobic sequence. It is: acetic acid, possible pyrovic acid, oxaloacetate,

6098 43/0 27 6 _ _

2b5238A - 17 -

Citrate and the citric acids (cancer) circulate for end oxidation.

Similarly, the anaerobic reduction of Sulphates are inhibited by the obligatory anaerobic Desulfovibrio. It has been shown that this in the Practice can be easily achieved through ventilation. The consequences contain a marked reduction in impermissible Odor and long resistance to aerobic action. This case shows up unexpectedly through exposed Methylene blue stability always indicating a shift towards products of anaerobic metabolism.

microorganism in waste treatment

The sprinkling filter. Microorganisms reflect the optional nature of the filter. "Aerobic, facultative and anaerobic bacteria are predominant. Obligatory aerobic spore forming bacilli can easily be detected in the upper aerobic plates. The obligate anaerobic desulfovibrio can be found in the lower levels at the plate-stone interface, where DO is usually zero. The majority of bacteria are optional, they live aerobically until DO becomes zero, then anaerobically.

Figure 1 shows the waste treatment facility, the process and the overall system of operating devices in which the invention is used. An irimal sedimentation container 10 picks up comminuted raw waste with settling solids from a line 12 which branches off from a main line 14-. Several lines 12 and successive start-ups can be provided.

The following operations result in two or more streams

809843/0276 - 18 -

introduced that a feedback of a processing supernatant line 12a and a primary recirculation line 12b. The supernatant portion is garbage with a high organic content, relatively low flow and withstands aerobic treatment two reasons. First of all, it represents a biotic population that is suitable for anaerobic processing, and second, its organic composition, the products of anaerobic hetalobism.

The second part of the flow is the primary recirculation, which is usually in the range of half a to three of the raw waste rate takes place. This recirculation flow is characterized by a low organic content and a high degree of treatability in an aerobic Process · It has "dilution" effects on raw waste can not only be marked, but also in connection with the secondary recirculation with great advantage when leveling of hydraulic and organic components can be used, which will be explained later.

These three currents are due to the primary sedimentation pressed on. The legislature often determines the hydraulic Design features for sedimentation systems with regard to container overflow speeds, which apply to the compound flow. Such overflow speeds can be achieved by the technique of Figure 1 of the interception of a Affected are some of the flow which, as indicated by 16, is directed to bioprocessing. How else will be explained, there are additional advantages when using feeding techniques, e.g. when leveling organic ingredients.

The basic flow from the primary sedimentation 10

609843/0278 " ¹⁹

reaches a primary stage of bio-treatment 16. It becomes a roughening sprinkler filter shown. To the remote basic flow three component flows can be added there. One, 18, is, as mentioned, an intercepted one Forward flow. The second, 20, is the shunt portion of the primary recirculation. The third party, 22, is the secondary recirculation of Figure 1. The existence of the feedback flows, the forward flow and the baseline flow prior to biotreatment is important. This combination results in sufficient degrees of freedom for independent rules in this and in subsequent operations of hydraulic and organic loading with flexibility and without overloading the primary sedimentation. From the biotreatment 16, like the roughening filter shown, in most cases the flow of the respective systems leads to secondary sedimentation 24. In some cases a second stage for biotreatment 26 can be provided. Usually this would be an irrigation fine filter be. Less common, but preferable, would be a stage of bio-treatment with activated mud.

In this case, as FIG. 1 shows, is from the first biotreatment stage 16 split the flow, with the primary recirculation via line 12b being a fraction withdraws for feedback at early stage 10 treatment. The remaining fraction goes to the second bio-treatment stage 26. Before introduction to bio-treatment 26, z. B. for the treatment of activated sludge, this can be mixed with recirculating sludge from line 28 will.

A remainder of the recirculating activated sludge becomes for processing with the sludge from the primary settling tank in a primary and a secondary processor 30 and 32 given.

- 20 -

6098 4-3 / 0276

From the treatment 26 of the activated sludge 26, the flow passes to the secondary sedimentation 24-. The legal determination of the overflow speed is here again. The permissible excess speed for the secondary sedimentation 24, however, from which differ from the primary and also depend on the type of bio-treatment. Treatment of the activated Sludge is by rapid recirculation over the pipe 22 of the settled sludge, as shown in FIG.

From the secondary sedimentation treatment 24- the Flow for the feedback recirculation over the Line 22 are intercepted after a partial sedimentation. A second part of the completely separated flow can flow into the secondary ground re?;; ierkulation fed back through the line 34 will. The remainder of the completely separated flow reaches the disinfection via line 36. At the Operation of the disinfection device 38 can be a gas-liquid disinfection via the line 40 by injection before the usual contact chamber disinfection. It can be the technique of gas injection or the complementary disinfectants are used. For example, an ozonization in the line can be a Contact chamber chlorination device 38 may be connected upstream. The chlorination can also take place in both stages or only in the contact chamber without disinfection in the line. The disinfection results in the final effluent via line 42.

Figure 1 has shown that the sludge from the garbage in successive Stages of waste treatment is eliminated. The mud is usually anaerobic in two stages Conditioners 30 and 32 stabilized. The stable

6Ö9BU / 0276 - 21 -

Sized sludge can be left to dry from the conditioner 32 on bases, in a drying oven, a fluidized base reactor or in a vacuum dewatering drum to be given. One final use of pesticides can be land replenishment or incineration be. The deposition of treatment supernatant via line 12a has already been mentioned. It is this Complete framework of the work processes of the devices, in which the idea proposed by the invention must be used. The explanation is made with reference to every described workflow of the devices. A later section then shows the optimal summary of the plants.

However, ventilation or other injections can also be used take place in many other places in the outflow of the .anlage according to Figure 1. In particular, the air into the processing supernatant recirculation, into the Raw waste input the outflow from the disinfection container 38 and into the outflow from the secondary biotreatment container 26 must be entered. In some cases, a chlorinated water solution should be added to the discharge prior to disinfection can be entered to obtain a breakpoint chlorination. The chlorination can therefore also take place in the disinfection container 38 can be used.

The setting

The setting or the sedimentation is the work of a standard device in the waste treatment. The effectiveness of this This process is important because of the high concentration and the wide size range of the particles in the wastewater. The concentration of these particles falls into a size classification of a diameter of ο, οοοοοΐ up to 5.0 millimeters.

609843/0276

This is an important property as it affects the settling speeds influences on which the setting or the clarification depends. The main speeds are above a lower limit of 10 "^ millimeters per Second. These speeds are used for clarification or for. Set in wastewater treatment achieved and are of primary interest because of their wide range and very small size.

The significance of this from the practical standpoint lies in the degree of the setting or clearing process. Apparently it is a speed value that approaches the described setting speeds. The significant inclusion however, this lies in the fact that the kinetic Energy at the inflow to the settling chamber is reduced to the lowest practical level shall be. That which seeks to increase the kinetic energy of the inlet nozzle sets the formation of clarification and settling down. Recirculation has such effects, but it has offsetting compensation benefits when weakening the organic content to be treated. On the other hand, there is a high speed or Excessive momentum exchange makes it difficult without a withdrawal advantage.

To understand the basic construction of the sedimentation tank 10 and 24 reference is made to Figures 2 and 3 of the drawings. The specific effects of the amendments of the sedimentation chambers are as follows:

a) To regulate the flow path before free settling.

b) To reduce speed and turbulence at the influence in the area of free settling.

c) To increase the settling flow path length and the settling time.

- 23 609843/0276

d) To increase the functional effectiveness of weaning.

e) To reduce the hydraulic component in the settling tank by feeding techniques and especially to reduce the overrun speed.

f) To introduce a further degree of freedom in the hydraulic and organic loading in the feedback recirculation.

The device for refurbishing the improved sedimentation tank according to the invention can be fitted into a conventional round .ubsetzbehälter. Its distinctive Element is a radial or hyperboloidal twisted impact diffuser that includes spiral vanes 60a. The rotary deformation goes through 7 ° or less to minimize the likelihood of flow separation at the To ensure channel boundary. This is a critical factor in the because of the induced flow delay three-dimensional diffuser construction.

Smaller but similar three-dimensional, spiral-shaped ones Collectors 62 and 64 can be one or more centrally appropriate ring-shaped collector points are used, an upper effluent collection and / or an intermediate effluent collection to obtain. The flow is the acceleration there and the boundary layer separation is less Meaning.

In a normal sedimentation tank, a distinction can be made between the influence and the outflow. So far and now these are considered with regard to the optimum total circulation. *) In it there is usually an upward flow in a medium source of influence. At the upper limit of this source, the flow is predominantly radially outward, with both tubulence and speed being great.
) This is shown by the view of the sedimentation tank - 24 · ■

posed. 609843/0276

In such a container, the predominantly radially extending surface nozzle induces a circulation in the middle area. Hence one develops there maintained toroidal vertebral circulation. This means that the intended sedimentation flow is disturbed will. It is functionally reduced by twisting vision, which usually occurs mechanically and gravitationally by the rotation of the earth.

Often the outflow is predominantly a peripheral hadial flow. It induces a similar toroidal vortex at the overflow. This toroid shows comparably low turbulence and a much larger diameter. This circulation is of less energy corresponding to the reduced overflow speed. The direction of rotation in the second toroidal vortex is the same as in the influx circulation. This means that at a radial intermediate point in the container, the two toroidal eddies interact with opposing local vertical flow components. This interaction shows itself through the ^T uomentaustausch which reduces settling.

To settling under the impressed conditions ru try the above antagonistic for the functional goal seems to be ill-advised. It is desirable to recognize that overall circulation must be considered and that the direct and induced flow described must be complementary to the necessary circulation. This is the general object of the sedimentation container according to the invention.

In the event of a drop, this is in a round, flat view

- 25 -

609843/0 276

possible when a single toroidal vortex induces the overall circulation under controlled conditions can be. Ideally, this should apply to such done wisely like increasing the primary sedimentation stream and, if necessary, to obtain a secondary oi flow with a given sedimentation.

This can be done by pasting and using the described middle collector 62, which is located under the middle inlet nozzle 82. V / egen one hyperboloidal diffuser surface or a wing 60a can the mean .vus flow with very little reduction the iCinfluence nozzle are working. He is also working on a well-separated fraction of low turbulence of the.-i settling container contents. These conditions result even with the production of a consistent, predictable fraction of a partially sold flow, which determines the tank overflow speed belittles.

At the inlet of the intermediate value collector in the settling containers, the hyperboloidal profile of the upper diffuser wing can have 6üa, since it is less critical when accelerating the flow. When optimizing the plant, it seems essential that the. To be run by hand or to regulate automatically in order to obtain the desired flow. A; _n *, own device 70 is provided for automatic or manual ramming. Devices for sensors? 2 for flow are an essential requirement. One way to determine the organic part is to use laboratory techniques on certain days. The average otund results can be read off. A regulation of the

609843/0276 ~ ²⁶ "

direction 70 may be based on the expectation that this entry. But it is also possible to measure interfrequency solutions of the load, e.g. those that relate to light transmission or spectral absorption are based in narrow wavelength converters. Maybe No rapid, intensive oxidation can be accelerated in this way be, dr, ß it rm BOD results in real time data. Then you can nn di <=> 4-system control for manual or automatic operation on an expected program (previous findings) be built up by real Time measurements of the actual hydraulic and organic loading conditions, for example with sensors 72 is amended. This is a standardized control technique with a servo system. The main feature is to program it to build up an error, an error corrector and measure the result to make the corrected error certain. > <if not, a secondary correction can be introduced.

Flotation separation

This thought can have a secondary function Effect of the middle source of influence 90 introduced v / ground. The influence can be applied where the flotation, especially for oil and fat separation, is affected. These conditions arise with the primary Sedimentation. To achieve this result, a presaturation of the influence with air, e.g. by a Injector 92 at pressures in excess of that upon dispensing is desirable. The iais write excess Air allows when the system is pressurized is, increased flotation in the source of influence

- 27 -

§09843 / 0270

90 of the primary sedimentation tank. This unites equipment and methods of improving sedimentation with those of the gas-liquid mixture according to the invention.

The collectors 62 and 64- eliminate two flow cuts from the .Vbsetzbehälter and from the ^ bsetzausflußabgabe cus the overflow collector. Of the The top cutout goes 6 to 75 cm below the liquid line, which is usually close to the top edge of the container runs. The lower section goes from 90 to 120 cm from this fluid line. The greater part of the intercepted flow of about 2/3 takes place from the upper discharge collector 62. The lower collector 64 removes the remaining flow with it Except for the sludge and the extracted liquid. Usually it is for the one picked up by collector 64 Discharge necessary to pass to another treatment for further treatment. From weaning leads the basic flow sheet for biotreatment. The outflow flow in the settling tank is indicated by arrow 94 · and enters line 66 through valve 70 to the source of influence 90, is from the pump 68 driven and released from the upper part 91 <ler source 90, passes through screen 74 and into a spiral dispenser by wings 60a which are adjacent to the upper surface of the spout. The Üiffuserflügel 60a are slowly rotated by a motor 110 mounted on a bridge girder 112 is held, which runs over the top of the container. The motor 110 has speed control and is operated for the correct width of the container as the vortex for the outflow depends on the width.

- 28 -

609843/0270

The flow is regulated by valves 82a and 84-a (Figure 2) and at the inlet of valve 70 iJie effect: the valves when inducing turbulence cm diffuser outflow is by means of the hole size in the sieves 73 and 74- suppressed. It can of course also be similar Processes take place at greatly reduced speeds in the container, which has an upper discharge collector 64- make redundant.

At the end of the wings of the diffuser 60a, the outflow aligned tightly tangentially in the horizontal. The vertical component of speed is because of the Delay in the diffuser extremely low. With regard to the low speed it can be seen that the Sedimentation takes place in the diffuser. It's an ongoing one Sludge removal provided. This is done by operating the diffuser close to zero lift, a mechanical technique familiar to those skilled in the art.

The diffuser blade 60a rotates very slowly, perhaps once an hour. This serves as a collector of fine classified material. The sludge is through the pipe 93 in the middle section and the tank bottom as well as by a sludge container 95 and a sludge— line 94- (not shown) derived.

The great care taken in the construction of the paragraph container can be due to two factors. One is the wind-induced surface cooling and the superimposed horizontal flow. The second is the density analysis in water, which can occur ^{at 40 G.} This factor can have serious consequences for vertical circulation. There is also the usual effect there

- 29 609843/0210

the temperature fluctuation on the density of the water. For this reason, the invention uses an air pocket on the lid 102 above the container, which the
Attenuates the effects of wind and temperature.

At least one of the middle flow cones 83 or is vertically adjustable, and probably both, so that their setting according to the flow needs. nissen is guaranteed by the container for optimal training.

Ura to ensure a lightweight loading, the rotary diffuser 80 is carried at the edge at each sector by a wheel 80b, the one with a fixed load running around on the ground. The wheel load control can be attached with appropriate resilient washers will.

The secondary waste container 26 receives the effluent from the lower incision of the first container 10.
Its primary sedimentation in its diffuser directs particles of ash size 200 or finer into the correct container. The section described for
Particles larger than those that will pass through a 200 flap screen will settle and are removed from sedimentation that results in diffuser 80 under the false bottom as well as in flow path 75.

In the secondary settling tank 26 is the hydraulic one Outflow one third of the system outflow. The right one The container separates the coarsest of the discharge particles, which are smaller than 200 meshes, in two sections

- 30 S09843 / Ö27S

are. In the upper section of the separated flow, two thirds of the discharge is removed. The lower Part of the flow eliminates a third of the reservoir discharge or about a ninth of that originally hydraulic charge given to the system. Only this fraction of the flow reaches the sprinkler filter or another BOD treatment.

The sprinkling filter

The following explanation shows how it works the first bio-treatment stage, a üufrauhfilter 36, known as a sprinkling filter. The ventilation level 34- on the influence is not described, since this has been dealt with in the aforementioned applications. The organic treatments are for the main ones Reduction in the BOD responsible. The basic theory of an irrigation filter is that an extensive area is provided, which usually uses a steep fill and is approximately 2 meters deep and on which a microbial plate is flushed with a film flow of cooling liquid with dissolved oxygen (DO) developed. The plate consists of a surface anaerobic substrate that contacts the chine, immediately next to the anaerobic and facutative microbiological Forms prevail. Aerobic forms can be located above this layer. This layer contains a source of oxygen. Apparently this “us” arises an induced, vertical, naturally convective air circulation that is parallel or counter-current to the pulsed Liquid flow occurs.

A fundamental limitation of the usual sprinkling

- 31 -

SD9843 / 027S

filtering is the indifferent oxygen occurring there generation. Thus, aerobic processes that are essential for biotreatment, prevented. Another limitation complicates this problem. It increases because the hydraulic one is responsible for air circulation Charge is limited. This increases the capacity of the filter and the effectiveness of the filling treatment decreased. This happens because the hydraulic compromise limits the flow recirculation to the filter, an important effector in deriving an essential BOD reduction.

To show the kangaroo of the free convective air flow In the case of sprinkling filters, it is of interest to refer to the working conditions that this flow induce. A basic equation for air speed becomes "Waste" Vater & Waste & Water Enbineering, Fair, et al, John Welev & Sons ", YoI. 2, Taken from pages 35-13. It is:

Ya = 0.0 * 1 Δ Τ - 0.14

where Va is the air speed in meters per minute and T is the temperature difference between air and wastewater in degrees Fahrenheit.

The sewage-air temperature difference rarely exceeds 25 ° 0. For example, at temperature differences of 10 °, 3.4 ° and -3.3 ° F Va is + 0.305 and respectively - 0.305 mpm. The positive sign means downward flow. Recognizing the filter is one with stones pitched base about 2 meters deep. In no case is there a displayed realistic air speed

- 32 609843/0278

age. Circulation with forced air was with low prospect checked. The resistance of the packed substrate to the air flow can be high especially with superimposed hydraulic flows.

Limiting ventilation and compromising on hydraulic loading is not necessary. The ideal tool is to use an effective one. mlage for mixing air with liquid in the inlet line of the sprinkling filter. This results in DO in the area from 7 to 8 ppm all year round and with hydraulic Loading. The particularly undesirable restriction on recirculation can be alleviated. This simple aids enables hydraulic loading in the range from 406 to 1218 and more liters per Square meters and day. Common on-going practice is about one-fifth "of the lower range of these values. The hydraulic flows are restricted to this level, to prevent blockage of the air flow necessary for ventilation. Cancel I.it The tradeoffs determined by inadequate ventilation of previous technology can be a simple change allow a full recovery of the irrigation filtering process. This change is one of the means out a size range; coarse stones to a reduced one Smaller medium size range. The change in the coat is primarily responsible for the hydrodynamic flow, v / eil compromises with respect to a flow are not necessary. Even more so than the change in hydrodynamic properties, it is common to refer to the desired properties of the agent describe the hydrodynamic parameters.

- 33 609843/0278

The parameters of interest are the friction factor, the Reynolds number and the coarseness coefficient. The size factor of the means is expressed as the equivalent diameter. The characteristic length of the
ötrömungsbahn is the depth of the support, di ⁿ is usual. The relationship between these factors is of the form:

where F is the friction factor, a is a constant, H ^ the Renold number and B is the rawness factor of the document.

The defining equations of interest are: _{f β} 2g De ₂ P TT De

t _{T /} 2 and

T ^r

ills suffices the Littel in relation to its equivalent Determine diameter and coarseness factor? U. The stream The functional relationship between the friction factor and the Reynold's number certainly.

The usual parameters for new agents are in the range, ax for a hydrodynamic or hydrofoil element are listed. This gives the relationship to a high DO contaminant garbage with no ventilation in the right one Filter.

A substitute plastic material, e.g. PVC, has been calculated. The means is an extruded pipe system, those in an equilateral triangular sieve for kaxiting is composed of the area per volume.

609843/02 * 76 ~ ³ ^ '

The pipes are distributed in order to create a balanced Ensure flow in the vertically arranged 'pipes and outside the pipes. this requires that the hydraulic radius for the inner and outer passages be the same.

A common result appears as follows in Figure 12:

OD = - 2.13 cm

ID = 0.74 "1.88 cm

L »Grid spacing 2.94 cm

The hydraulic radius of the channel is

Area from section to perimeter.

The section described shows an area for bio-

2's logical disks of about 1J2. m / m · Sin common stone

owns less than 40% of this special area.

The lengths in a continuous section can have the entire depth from 1.89 m to 9.15 m. However, shorter lengths that are stacked to the total depth "have the following advantages: The basic advantage is that the laminar boundary layer of liquid or plate begins and builds up at zero thickness. A length compared to the length required to fully develop a stable laminar boundary layer Dissolved oxygen source readily available to plate. The diffusion gradient increases in two ways: First, the concentration is kept high, and second, the thickness of the boundary layer is reduced.

The length to fully develop the boundary layer in the laminar flow is meters to water in pipes of about 3/4 "diameter in the delimiting transition area

- 35 609843/0276

rich of the Reynold's number, i.e. about 3,000 flow towards it permit. To express the distance as a diameter, the transition length is about 1/10 to 1/20 of the Reynold's number.

The flow in the distributed pipe means at the limiting laminar Reynolds number can be estimated will. It is 67 i. Illion liters per day and one

ρ
93 m area · Hydraulic pavement speeds are typically less than 4 million gallons per day and 100 square meters. Thus, the planned high hydraulic load can be carried out with this means.

The speeds not included in a compromise allow a much higher organic load, instead of the current upper limits of less than 1.12 kg BOD per day for every thousand cubic meters of the agent the three to fourfold charging appears possible. The high organic or nitrogenous charge will only possible with pre-aeration, which allows a much higher hydraulic load. All three variables, DO, the hydraulic and the organic charge work together. Therefore there is only a mutually compatible solution feasible. In this case, bring equipment and procedures the integrated advantage of effective gas-liquid exchange and organic treatment processes in Aktjon.

The structural details of the improved sprinkling filter use a tool 13 ² S which has been described in connection with FIG

- $ 36 609843/027

aerated discharge charge from the ^ .setzbehältern absorbs. The rod 122 rotatably supports a distributor arm 126 which is hydraulically operated by a motor 128 is made by the v / elle 130 and a double flange coupling 132 is connected. The influence of fluids goes through the pipe 124 through the center bar 122 and sprinkled out from the distributor. Very low when it is rotated by the rotor 128. All these Parts are used in the usual manner in sprinkling filters used.

In the particular construction used, a wire mesh type is used to form a large circular length 134- with loosely packed thongs ^ or special Filled with material that looks larger in areas Areas granted per "unit of volume, oo l-.long as dde Problems of clogged fluid flow and inadmissible g-phase flow restrictions: en considered the large-area packing can be used effectively in this / training. In one case the liquid dispensed by the distributor arm 126 drips through the packed pad into the open base.

The invention also employs a plurality of air blowers 14-0 positioned around the hand of the container 120 and propel the air in the direction of arrow 142. Since one of the purposes of such an irrigation filter is to reduce BOD, it must be ensured that more oxygen will oxidize the fluid outflow causes the air to flow necessarily through the pad in a reverse direction to the flow Direction, the circulation can release the oxygen to maintain aerobic metabolism.

- 37 -

2552284

remote. It is also used to increase the oxygen atmosphere excess oxygen is sprayed through the pipe 144 into the turbulence mixing chamber 148, the is regulated accordingly by the valve 146. Also for operating the filter with a humidity of almost 100Ci in the atmosphere can create a D-chabdec-kung I50 supported by a catenary cable assembly 152, ooiait krnn the sprinkler f j lter 100; ^ relative Humidity, air circulation and one enriched with oxygen because of the oxygen spray into the outflow use atmosphere. The increase in .nl & prenkajja— city and the reduction of BGD can be easily achieved with this ^ ei ^ eseen advertise.

This aerobic process can therefore be seen that the described-n design features for the improved sedimentation facility the Lüllbehandlunpjsanlage : "r> srj; esaTnt increase. In other words, that Oxygen: spray into the oil processing facility 22 is intended to greatly increase the operating capacity of this facility to ensure safe sludge concentrations to create.

"The invention can also include the addition of excess Oxygen is directly contained in the humidified atmosphere through a Hohr 160, which is regulated by a valve 162 will. To control the amount of oxygen entering, can a corresponding sensor 164 associated with the discharge outlet pipe 138 and associated with a velocity of a flow instrument 166 and through an oxygen concentration device 168 is operated. Corresponding sensors 164a to 164d are for speed the flow instrument 166 and the oxygen concentrator device 168 to be completed.

609843/0276 ~ ⁵⁸ ""

Direction assigned and are used to regulate the flow of the amount of oxygen through the tube 160 in the most economical work of the plant.

Biotreatment of the sludge activated in the second stage

An activated sludge work can be the only biotreatment device or a secondary element in a be two-step bio-treatment. This is the realization of the sensitivity of edits enabled Sludge to fluctuating hydraulic or organic influence charges. Although this is not the usual current practice is, edits can be enabled Sludge suitable for treating fluctuating hydraulic and organic charges in the system be. This allows sufficient flexibility of the circulation for the inclusion of an independent compensation of hydraulic and organic charge in activated sludge processing.

Regardless of the - «xt of the application of the processing of the activated sludge, there is a predeterminable requirement for aeration. One watched Ventilation corresponds to an amount of JO up to 4-3 cubic meters Air per kg BOD removed. The oxygen requirement is from 7 »5 up to 10.5 kg of oxygen per kg of BOD removed. An equivalent Fenge is provided by derived from surface ventilation. The usual total need for oxygen is between 15 and 21 kg Oxygen per kg BOD removed. Since BOD is one to be put at one with the need for oxygen by definition is the oxygen through the ventilation,

- $ 39 09843/02? $

The usual techniques used are irrelevant for the efficiency. This interference remains valid even if available internal oxygen sources from the biological reduction of nitrates are permitted. This finding is za expected since the ventilation efficiencies often range from 2 to 10%. These values apply to aeration of liquid with an initial DO of zero. This results in the highest possible degree of efficiency. A more realistic degree of efficiency is that for a DO in the range of 2 ppm.

The practical solution to the load issue in the activated sludge processing is described in the patent applications mentioned. The technology and equipment offers oxygen mirrors efficiencies of more than 50/0. The use of this ventilation device in the present processing of activated sludge is made visible. This reduces the necessary air compressor capacity by more than an order of magnitude and also reduces the drive power requirement to less than half of the usual value.

The treatment method can be one of seven basic methods that are activated when machining Mud can be used. What is important is the integration of the effective gas-liquid mixing techniques at this stage of the bio-treatment. From the processing of activated sludge, treated kull is sent to a second sedimentation released. Where this processing does not take place by sedimentation, the following can be used Hedimentation process well the definite final sedimentation be.

- 40 GQ9843 / 0276

The secondary sedimentation

In the case of the arrangement according to FIG. 1, the treated material is released from the processing of the activated sludge in a medium influence as a source for the primary sedimentation. Excessive ventilation to degas and increase flotation from fat and / or sludge is unnecessary. This expectation includes equipment and process flow for priinär ⁿ sedimentation beschrieber · can be, V can be expected ie /, expectations advocate of de ~ secondary sediment "tj or, in the preferred state of the effluent.

For example, settled secondary sludge is in usually eliminated and returned to the influence of the activated sludge operation. Something of this flow is diverted so that excess waste is directed to the primary conditioner. Of the Clarified .Discharge is sent to the disinfection with distraction the necessary quantities for secondary circulation submitted. The desired balance between the hydraulic and the organic load the partially settled intercepted secondary circulatory flow may be included in the secondary circulation. This is shown in FIG. 1.

In the effluent from the secondary sedimentation leading to Disinfection is intended, this is introduced on the line that excites the secondary. This technique uses highly effective gas-liquid freshening techniques, which have been described in the aforementioned applications. First of all, the suggested disinfectant is using

- 41 609843/0276

2S52384

the organic charges become effective in short periods of time. Secondly, this 3) esinfekt <"nt potentiated Ch. It acts synergistically with egg counter value of a secondary oxidised conditioning * The secondary Oxidieranla _s e k'inn Ohloreinsen be, which is added in the secondary clarification sedimentation, or it can be standardized . be chlorine additives in, each case reduces the ozone enriched oxygen air, the final OhlorbedJrfnis and ensures -uisflnß, dor relatively low Ghlorrückstände with highly ii; having eloi3tom oxygen disinfection characteristics of ozone öauerstoff and ^l: otenzierungseff'ekten of Ohioreisen. The standard techniques rubbed Ohloreiaen into the secondary sedimentation system so that it works together with an Op-CU addition during disinfection.

The Desin fektionsbehan d development

! '.' alas the idea of the invention is applied to the disinfectant material a hech-effective system according to a two-stage system with a distribution of a connection of aniiionia and ammonium provided that especially suitable for the treatment of sheath or sewage discharge is. To disinfect the material as well as to lower the pH value, a primary and also a secondary one is used Oxidizing agent used. Although the oxidizing agents are common compounds for treatment of LiUIl and ilbwasserausfluß can be included they use aluminum chloride or chlorine iron as the primary oxidizing agent, and chlorine, chlorine dioxide, ozone, neither by itself or preferably in oxygen or air and sodium hyperchlorite as secondary oxidizing

- 42 B09843 / 027S

fabrics. It has been shown to have synergistic results of oxidative disinfection in a two-stage treatment system m, ch of the invention can be achieved, with the primary oxidizing agent in the first stage and the secondary oxidizing agent is used in the second stage. Preferably it will be a good value a first stage oxidizing agent and a small amount of the secondary oxidizing agent to generate added to a very small number of bacteria.

A two-stage oxidative disinfection system is preferably suitable for the treatment of oil and wastewater. The primary oxidizing agent can be the final clarifier or effluent and the secondary agent of the disinfection contact container influence of a conventional waste treatment plant or facility as described here. When treating garbage and sewage, a fecal coliform bacterial count less than 10 parts per 100 millleter treated Vaginal discharge can be easily preserved. The use of the preferred primary described Oxidizing agent can lower pH. Preferably, such an amount of a primary oxidizing agent is used used that the pH of the effluent coming from the final treatment plant was 7 or below with 6.7 to 6.8 being desirable. According to FIG. 18, a pH value at room temperature shifts the ammonia Ammonium compound shifted, i.e. in an excess of about 97% and sometimes 100%. If a higher one pH is used, smaller amounts of ammonium result. In general, a pH value is desired, in which the amount of ammonia is reduced. Sin

- 43 - 6090 ^ 3/0276

pH 8 and less at room temperature may be suitable. The importance of reducing ammonia eats that iunmonium chloride or other χππαο-nium compounds or complexes often exert virtually no oxidative demands if they are b ^ kteristic L'etobolism in the presence of oxygen under are exposed to a pH of 7 »0. In the treatment from garbage and sewage, Gomit becomes the oxidative nitrogen f need virtually reduced to Küll. Against it shows ammonia a substantial oxidative need that is about 4 1/2 times the ammonia nitrogen concentration is. With conventional filling systems, at which the concentration of ammonia is in the concentration released by the secondary clarifier of ammonia is released in the discharge, which in the The range of 30 parts per million requires approximately 135 or 145 parts per million of oxygen demand nisBes. This need does not only apply to a Yiass stream or toxic effects, it also has an immediate effect the dissolved oxygen concentration in the stream.

Because of the toxicity of a stream it is known that ammonia in water fishes at a concentration 4 to 5 parts per million can be dangerous. On the other hand, ammonium compounds are not toxic and, as mentioned, often do not have any oxidative needs. In addition, ammonium compounds act as inhibitors the formation of nitrogenous metabolism due to the presence of bacterial forms. In addition to the energetic reduction of bacteria during disinfection, this creates the shift the equilibrium of ammonia - ammonium to ammonium compounds high practical results, in particular

_ 44 _ 609 ^ 43/0276

with regard to the regulating agents, C. ie the Reduction of nitrogenous biochemical oxygen demand and a minimum of practical Require chlorine concentrations that are compatible with the disinfection and based on new knowledge the role of chlorine in the development of cancer.

At a common or typical urban wastewater treatment plant , the primary, waste residue treated, an amount of primary oxidizing agent is about 85 parts per 1-.IiIIi on as an = - e- · measure to generate a pH range of about 6.6 to 6.7 and to promote sedimentation in the final sewage treatment plant established. A minimum amount of at least 50 parts per million is found to be desirable. In addition, the amount of solid suspension in this stage is generally very small. This plague suspension will ■? η of the secondary sewage treatment plant deposited and so from the treated. ^ outflow stream removed. It has been shown that in the two-stage oxidative disinfection system described in the relatively large kengen of primary oxidizing agents are used, so that very low kengen secondary oxidizing agents are necessary. For example, the concentration in use ozone contains 0.7 parts per million, while for ghlor the concentration is 4 to 5 parts per Ή Hi on can be to carry out the disinfection mentioned. That is a facalcoliform number of two or less per 100ml. In practice, because of the ineffective mixing of the oxidized salt such as aluminum chloride or Ghloreisen in secondary clarifiers, the ozone

- 45 609843/0 2 78

conzeitrotion generally higher than the smallest 'enp; e. T * ". A maximum of 10 parts is generally sufficient pro I illion to disinfect. The mixture with the maximum "clout" -rann from the use a device for creating high turbulence such as using openings in a flat plate, as already mentioned, and the use of special arrangements r? «ch. Figures 6, 13 and 15 as well as no: ch the IJSA patent documents 3.730.881 and 3.805.4-81 derived from "" .en.

In the case of the invention, a first stage of an oxidative treatment or disinfection of aluminum chloride or aluminum chloride is carried out by adding 85 parts per ion. The Päkal- koliformzahl the first step is quantitatively '] O ^J / 100 Iv.illiliter. The fakalkoliform number of the second stage of the oxidative disinfection system with a chlorine feed rate of 4 parts per million at 0. Furthermore, the degree of sinister sterilization effected by agar cultures at 37 ° C, which does not indicate any closure, was confirmed.

Furthermore, when using the described two-stage Disinfection system found that adding a good dose of chloride to the first stage for the sedimentation, which is a dose of 6.6 parts Per Hillion of ozone in oxygen in a second stage can, in less than 8 seconds, the concentration dissolved oxygen can rise to 37 parts per million. Such a sample was immediately after the oxidative disinfection sealed and five days

- 46 609843/0276

measured later. A dissolved oxygen concentration of 31 parts per million is recorded been. The difference of 6 relates to the fact that the metabolic activity of the surrounding Bacterial forms has been virtually completely inhibited. This is done through immediate disinfection and by almost oxidative killing, which affects the viability of the organisms and their ability to spread caused. Maintaining the dissolved oxygen concentration from 37 to 31 after five days leads to final disinfection.

The optimal system

The optimization of the plant in the waste treatment will usually discussed in terms of a fictitious constant load. The optimization cannot affect the Outflow quality standards can be obtained with a minimum of capital and maintenance costs.

The characteristic load

The characteristic garbage load of a plant is the combination of hydraulic and organic components. It is not constant during the day. It is likely to repeat itself from day to day with the exception of holidays and weekends. Rain and 02 ¹ I ¹¹¹⁰ S time effects result in long-term changes in the load.

The loads on a weekday can be a geometric A series of a few values can be calculated approximately. It is not uncommon to note

- 47 609843/0276

2S5238A

that the loading area. ? 5 / o of the average load can be. In contrast to this fluctuating load, the criteria require the discharge with usual quality that a prescribed maximum is never exceeded. In practice means this that the regulation of the plant with better quality with 95 or 99? <> Probability is achieved by how much better the quality target will be should is a critical economic question.

Obviously, there are no fixed rules for regulating the elasticity and economic efficiency of the procedure in the case of a fixed ice drift and a variable entrance. An obvious approximation is to accumulate mixed ⁷ I ^1- JlIs for longer periods and then treat a continuous short at an average daily rate. This requires large storage containers and problems of storage, rotting and cost.

Despite these problems, there is a great advantage from the constant hydraulic and organic loading, that can be achieved through the optimal use of the system. The main advantage in simplicity the controlled regulation of the work of the system. This is essentially a servo system. To one Obviously it would be easier to obtain a fixed exit in the prescribed kenge, a fixed procedural rule that corresponds to this quantity, whereby the input is also fixed. At this entrance the best practice and the best regulation is then a difficult problem, although this problem is fundamental it has not yet received the attention it deserves.

- 4β -

603643/027 $

2 b 5 2 3 8

In the equipment and procedural machinery of this thought, a double attack on the design and proposed rule problem. The basis of the attack is reasonable flexibility in the Machining control to better approximate a uniform hourly hydraulic and organic Loading over a normal working day obtain. This made the size and the impact the fluctuations in the load are kept very small. The second basic element of approach is a pro - measuring regulation for working with the suppressed load fluctuations to maintain the desired value of the discharge quality at all times. This gives the optimal Plant in terms of the lowest total cost to continuously derive the acceptable quality of the Kus river. Calculated execution, process conditions and basic factors of the total costs are given and will be described in detail later.

With regard to the optimization of the system, the ideal solution requires excessive capacities of the settling tanks on both the primary and secondary tanks. The practical answer is the compromise at the current.

Example A shows that with an arbitrarily changing influence rate and concentration of the organic components, it is possible to obtain a process influence which has a constant flow rate and a constant concentration of the organic charge component. The condition shown relates in each example to the influence of the.-I-settling container. Thereafter

- 49 -

600843/0276

The hydraulic charge changes over time in the process, but the concentration of the organic charge is kept constant. The compromise condition enables a change and the hydraulic and the ok: nisoien charge in the settling tank. The lower Ges · -: Bite. Influence influences the result of the primary sedimentation. The design constraints then lie in the process, which means that the interval from over which the integrals are considered is short, or that point values are used. In addition, a simplified on-off control is shown to approximate the exact solution. This gives a. rectangular area for integration instead of the area under a trigonometric curve or a point of hydraulic and organic loading. The Fy11 D? Eip: t that at - ^ = 3.0 for the 24 hour rate, a total drenching of 3 »3 results in an optimal flow. The '-.tr'-irnungsbedingung results in a narrow Annäh.erung an ax constant concentration of the organic charge for sprinkling filter, such as the diagram of FIG ze IGT. 11 When treating activated sludge, the concentration could be kept constant by controlling the return sludge rods. The hy '-' aul ⁴ "dien charges were in, each representation of the from; v; ezop: enen representation D1 or the dashed 1) 2 in case D vary.

Case Λ - The schematic flow diagram according to. FIG. 10 shows states for the unified hydraulic and organic loading with an arbitrarily variable charge. The figures between the Sections ή η Figure 8 are the BOD of the treated liquid in ppm. Case A, as indicated by the diagrams of the figures S ηηά 9 is shown, uses a pro

measuring control of the flow in Q ₁ , Q ,, Q ^, and Q ₁ -. Q ₂ can be kept at O.

Maximum charge - C ". = 1.4 LiGD. B = 350 ppm. Secondary Recirculation for 10:00 AI./Pi, "charge.

I. (BOD) 83 (Q + Q ₃ ) = 1.4 350 + Q ₃ . 20th

0. 1.4 (35-83) _m 1.4. 267 _ _{ς Q} , 3 83 - 20 63 "^ ¹ '

He circulation ratio H = - ¹ - = 3.24

Flow to primary: 5 ^ 93 ^T "GD-Hate. Secondary circulation for 8:00 and 12:00 AM / PK-charge

83 x 5.93 - 1.1 x 275/20 Q ₃ = 58 483 - Q ₃ % - 107.5 / 38 = 2.83; Q ₁ - 4.83 - Q ₅ = 2.0 uecondary circulation of other currents 7:00 and 1:00 ΜΙ / ΡΪ '

This is an average loading condition.

83. 5.93 = 8 χ 200 + 20 Q ₃ + 58 (5.13 - Q ₅ ) and at Q ₃ equal to zero:

5.93 x 83 - 8 χ 200 + 58 (5.13 - Q ₃ ) 492 + 34 = 20 Q ₃ - 58 Q ₃
Q - - 34/38 = about 1.0

2nd case for 8:00 and 12:00 ΔΜ / ΡΚ

83 x 7.33 = 1.1 χ 275 + 20 Q ₃ = 58 (6.23 - Q ₃ ) 610 = 20 Q ₃ - 58 Q ₃ = - 38 Q ₃ Q ₁ - 6.23 - 1.42 » 4.81

- 51 -

809843/0276

III. lall for 7:00 and 1:00 / di / Pv average charge 83 x 7.33 = 0.8 χ "00 + 20 Q ₅ , + 58 (6.53 - Q ₅ )

610 - 160 - 379 - 71 = - 38 Q ₃ , but for Q, = 0

71 - 58 Q ₁ , Q ₁ - 71/58 = 1.23 flow test 6.53 B + 0.8 χ 200 = 83 χ 7.33

6.53 B = 450; B = 450 / 6.53 = 69.

The flow must _{shift to Q 1} / + Q ₄ continuous solid percentage lines primary 3 $ and solid secondary percentage lines 6%.
Primary sludge 3> at 7.33 HGD = 0.22 MGD; BOD = 83-58.

average delivered = about 2500

IV. 83. 733 = 0.8 χ 200 + 600 Q ₄ + 58 (6.53 -Q ₄ )

+ 71 = 600 Ci ₄ 0 58 Gi ₄

q ^ = 71/542 = 131 V.GD then Ο «» is 6.40 VGD

Y. Conditions at 6:00 and 2:00 M '/ Ff- 83. 7.33 - 5 + 125 + 60 ^ '^ ₄ + 58 (6.83 - Q ₄ )

151 = 600 Q ₄ -

VI. Conditions at 5:00 and 3:00 ΑΜ / ΡΠ

83. 7.33 = 28. 70 + 600 Q ₄ + 58 (May 7th Q ₄ )

181 - 600 Q ₄ - 58 U ^ ₄

Q ₄ = 33 FGD

Q ₁ = 6.72 I'GD VJI conditions at 4:30 and 3:30 Al

609643/0 2 76

83. 7.33 = 0.22 χ 55 + 2500. Q ₅ + 58 (7.11 - ^)

Q ₅ - 0.089 HGD, or

shows the alternative to the secondary sludge process of the treatment supernatant

83. 733 - 0.22 χ 55 + 600 Q ₄ +

(7.11 - Q ₄ )

186 - Q ₄ (600 - 58) Q ₄ - 343 MGD Q ₁ - 6.77 Ϊ-GD conditions at 9:00 and 11:00 AM / PM 83. 7.33 = 1.32 χ 327 + 20 Q ₃ + 58 (6.0 - Q ₅ )

VIII. Conditions at 8:30 and 11:30 AL; / PH

• 83. 7.33 - 1.22 χ 305. + 20 Q ₅ + 58 (6.11 - Q ₃ )

Q ₁ = 3.11; Q ₃ =

IX. Conditions at 9:00 and 11:00 AM / PM

83 * 7.33 = 1.32 χ 330 + 20 Q ₃ + 58 (6.0 - Q ₃ )

₃ »4.58: Q ₁ - 1.42

X. Condition at 9:30 and 10:30 AM / PM

83. 7.33 = 1.38 34-5 + 20 Q ₃ + 58 (5.95 - Q ₃ ) - 211 - - 38 Q ₃ ; Q ₃ - 5.55 Q ₁ = 0.4

Case A pump capacities - flow around the primary sedimentation equal to gravity.

609843/0276

Flow around the sprinkler filter is zero. flow by dj.e secondary sedimentation equal (L · - Q ^, = 6.4. Secondary mud flow equal to 0.4. Then 0.400.000 / 24 + 60 = 278 GPK. Take 300. GPK 2: 150 GPM, -Secondary 6.4 / 1440-4.450 and 4: 1200 GPMl

Equipment size in case A: Primary: 4 18.2 m diameter Secondary 4 18.2 m diameter sprinkler filter 2 22.5 m diameter

System characteristics - Large sedimentation requirement. Moderate pump requirement. Conservative treatments required. Fixed effluent BOD for chlorination of 20 ppm with an influence of BOD of 50 to 350. BOD reduction from 94.3% to 43%.

A second case can be examined. It reduces the primary and secondary needs when it snows, that a practical change from the imaging gas A, which has already been mentioned, suggests a compromise based on the peak flow condition at 10:00 AM / PM. The compromise is the assumption of a plant condition of 9:00 or 11:00 AM / PM for hydraulic loading. An organic charge in ppm can be kept constant. Instead of the ideal situation of keeping the hydraulic load constant 24 hours a day, the hydraulic Charge held at 9-11. Then in the interval 9 to 11 AM / PM, i.e. twice a day, for two Hours a hydraulic "overload" is allowed. This only affects the primary and secondary settling tanks he and im not serious in comparison with the potential cost savings. With the exception of the interval 9 to 11, the hydraulic and organic loading can be kept constant.

609843/0276

However, other compromise options can also be selected. For example, the interval can be 8 to Be 12. For the three cases A, 9 to 12, the relative flows are 1.4, 1.32 and 1.1. Most legal Regulations require that sedimentation tanks be sized to provide certain overflow rates, expressed record as MGD per unit of surface. This reduces the facilities from 1.4 to 1,1 so that the required area reduction is 3/1 ^, which is proportional to the cost reduction.

Any or no flow is typical for practical manual control. It can set and for valves be opened for a certain time. This type of control is also possible for the automatic control of the system. It enables simple time controls "

The understanding discussion includes more difficult controls typical of ordinary servo control systems. The mentioned conditions will be invoiced. The performed calculations and diagrams of the figures 8 to 11 are based on controls of certain integrals. These have the following form:

Q = - gc dt, where Q is an organic charge, from time limits for the charge increase q is a flow rate and dt is the differential time.

The control is based on the manipulation of several integrals for approximate concentrations of organic charge at indicated locations throughout the process. A special The case is represented by the influence of the sedimentation tank Br, where the organic and hydraulic charge

- 55 -609843 / 027-6

must be kept at constant values. The effect on the increased overflow rates at the sedimentation tank are like ■ noted above.

In order to reduce the overflow rates in the primary sedimentation, the condition for the constant hydraulic and organic charges are placed in the biotreatment. For a sprinkler filter or a device for the treatment of activated sludge should the hydraulic as well as the organic charge be kept constant. This is because of the working of the device for the activated sludge. To illustrate this condition, a limited number of the above calculations are used to illustrate a typical solution is used.

The disinfection system:

The disinfection system according to Figure 5 is a gas-liquid mixing system, which is under a hydraulic Pressure gradient worked It consists of a source 200 for liquid oxygen, a source or a Ozone generator 202, an oscillator 204 and a process flow line 206. The line 206 operates in the turbulent flow with a Reynold's number 3,000 or above. At least certain T-shaped flanges 208 there are high torque exchange elements, which are usually openings 208a in a flat plate that induce intense mixing, which are sufficient to greatly reduce the radial concentration gradients in the treated fluid outflow, which enters flow line 206 at 209. the

- 56 -

609843/0276

Misehelpers 208a can have jib booms 210 upstream operated by an adjustable source 211 at or near its natural frequency These can be worked in relation to the gas injectors to further increase the moment exchange in primary consideration of reducing the Concentration gradients can be arranged in the angular direction in addition to the radial gradient suppression occur due to the main basic mixing element, the opening is induced in the flat plate »In addition, the primary task is that the stitches 210 are mechanical, exert disruptive forces on flakes, plates or agglomerates that are located in the treated liquid drainage can be located. The task of the directional forces is to reduce the size and the available Enlarge the area for disinfection on these flakes, plates or agglomerates.

The openings 208a in the T-shaped flanges 208 are located at the flange connections for simplicity. The orifice diameter to tube diameter ratio is usually equal to or greater than 0.7 · ^{There are two other elements in the T 1} S 208 that contain the openings 208. One of these is a 0, -O ₂ injection device 212, which is inserted in an axially fitting position lying in the ideal center, which runs through the opening preferably up to or somewhat behind the constracta vein, which is formed by the flow through the opening will. An optimal injection takes place with a minimal concentration gradient in the direction of flow. This is very easy to achieve in that the flow

- 57 -

speed over short or longer times or by an equal proportional control of the flow is made evenly »The stitch 210 is the second element, which is in the same way in the axial position + is introduced and serves as an injection device 212.

The O ^ -Op injection occurs at a concentration of 5% or less due to the weight of ozone in the oxygen. For generalized disinfection, it is introduced in amounts greater than 0.5 milligrams of ozone per liter of liquid. The concentration sprayed in is diluted in the flow line. Two factors cause this dilution. One of these is the rate of disintegration for O ₇ ,, which leads to Op in water. The second dilution factor is the oxidative charge of the material in the treated liquid. Common garbage contains this in organic matter that is incompletely oxidized into stable forms. Together with oxidizable, inorganic components, these substances contain the garbage's BOD load

The O ^ dilution may be necessary for the use of a subsequent spray. FIG. 5 shows this and also a series of test points in the flow line between the injection points for the O ,, which contain the sensors 214- which are used to regulate an energy source 204 to the generator 202. These sensors can be used to quantify the O ₃ concentration and the BOD reduction. Given a Reinold number, these data provide information about the time and place. This information is used to design the flow system and to determine the

- 58 -

6 0 9 8 4 3/0216

optimal (X matters. For the generalized Disinfection, it is important for the invention that the spraying speed and the spraying interval are dimensioned accordingly are that the concentration of the diluted 0, 0.5 mg ozone per liter of effluent at all points in the Plant on which the generalized disinfection is to occur · On the other hand, the special Disinfection as of obligatory anaerobic bacteria forms with air or oxygen containing only traces of ozone, as usually found in concentrations of 0.01 ppm or less have been established. This method and equipment are described in the referenced patent application.

The purpose of the following spraying is clear. The number the places or the distance or the time in the flow line depends on the charge imposed and their respective size. In normally operating systems, the treatment time exceeds 8 minutes not. The pipe system according to FIG. 5 runs more normally Way in the vertical direction in which the input 209 and the output at 216 are comparable to herizontal Locations so that there is essentially a hydraulic gradient when the system as a whole is looked at. The relative vertical position of these points is essential for the effectiveness of the disinfection system irrelevant.

The construction of a T-surface 208 with the opening 208 in a flat plate, the centrally arranged ⁰ O " ⁰ ^" injection device 212 and the oscillating pass 210 is shown in detail in FIG.

- $ 59 609843/027

2b52384 - 59 -

According to the invention, excess oxygen can be pumped 220 at point 218 are removed from the pipe system and into a dryer 222 for transfer from there through a control valve 224- can be added to the feed line of the source 200 of liquid oxygen to the ozone generator 202. One corresponding energy source 226 operates the dryer

An absorber 230 can output the generator 202 before the concentrated ozone enters the feed line 232 so that all of the excess Oxygen via line 234 and through the valve 236 is removed through to operate the generator 202. The absorber 230 can be selected if the 0, -Op concentration directly through the line passes through.

In some cases, it may be desirable that the treated liquid entering the piping 206 at point 209 pass through an aerator or absorber to degas or absorb the effluent, as one does not add new O to the fluid in an operating theater slide can when the fluid is saturated with Op _e The arrangement is indicated by the dashed line 240.

The system described calls for the preferred equipment that uses a liquid oxygen supply. Oxygenated air for ozone production can be with or without recirculation and oxygen to be used on work. Air and oxygen

- 60 -

609843/0278

can be separated, which includes recirculation, drying and recovery of oxygen. Continuous recirculation cannot take place and in this case there is obviously a desired one Outflow velocity for the oxygen source. The speed should meet the DO needs The effluent and the argon dilution problem suffice, increasing the efficiency of ozone recovery as the concentration increases of dirty gases can decrease. Also, the installed capacity of the Oo outflow source at

expected average need of O ₂ - O _{0,. Λν} ,

5 2 lie

This keeps the necessary capital investment very low.

Regarding the passage of the effluent through the vent or absorber 230, it has been determined that 7 to 40 ppm from the effluent prior to dispensing Use in the oxygenation process in the waste treatment plant can be recovered. Other techniques or other ventilators or absorbers can be used, either causing heating or blistering where the blistering could be the ultrasonic excitation according to the patent application mentioned may contain.

The whole disinfection process uses oxygen-enriched air and not air, which results in the high Nitrogen concentration at an ozonator efficiency using oxygen-enriched air or oxygen becomes very low. As described, it is when using oxygen-enriched air or oxygen a significant improvement. For expanded oxygen it is a known fact that

- 61 -

■ 2 b 5 2 3 8

the potential solubility of oxygen in water is five to six times as great when it is in equilibrium for oxygen is introduced, which enables a higher concentration of ozone to be injected, while less oxygen is required. The elimination of oxides from nitrogen provides security and air pollution control. Furthermore, the oxygen decreases for the recirculation and increase process the cost of the oxygen increased by an order of magnitude or more while the scaling process increased will, as will be explained.

There can also be recovered oxygen in the sprinkler filter or activated during processing Sludge by oxygen outflow injection or by oxygenating a basic air outflow injector be used. In this way, a filter bed is said to have aerobic-metalobic rates at maximum Comply with quantity values over its entire depth. A similar effect is activated when editing Mud possible. The effect of the increased BOD reduction is striking.

The ventilation for the mesh injection is in the area from 4 parts of air from 10,000 to 100,000 parts by weight Fluid has been practiced. The volume concentrations do not have to exceed 50% air in the liquid. For mesh injection, you can get common results with much higher values, perhaps 1 to 5 "volume percent be achieved. Wet aeration can be effective at much slower feed rates. The limit in this case depends on the exit on

- 62 $ 09843/0270

Wing eye and leads to a possible loss of the pump effect. This problem is mentioned in the Patent application also dealt with in detail.

The saturation values for aeration of water are 20 to 30 parts by weight per million. In the case of waste, slightly lower saturation limits with regard to additional pollutant gases and shredded materials, ie for ventilation, can be expected. In terms of oxygen production, water saturation values are in the face range from 4-0 to 50 ppm. For ozonation with oxygen as the carrier, the saturation at 6% weight of ozone in oxygen corresponds to the ozone in liquid concentrations of 2.5 weight ppm. The preceding ranges can be used to represent preferred gas concentration ranges.

As is known, the network works according to the speed of influence to the wet source and the value to regulate of the pumps intermittently. When the pumps are switched off, a pressure wave is reflected by the system then returns and oscillates periodically until it is finally dampened. The pressure swings come under and above the static pressure in the pipe. The pressure differences can match the dynamic pressure differences be compared or exceed this difference. These pressure waves act as a water hammer. Air in the main line for ventilation to control the putrefaction affects these pressure waves. Air reduces the pressure differentials and also the speed of the pressure waves in the main line, from one end to the other and the air lets the air oscillation die away quickly in a few cycles, everything in comparison to the main line speaks

609843/0270

- 63 -

to switch off the pump without spraying air into the main line. All of these results are beneficial and result from the practice of spraying air into the main line. The one for garbage, water or Liquid such as oil used in the main line in general can come from aeration or from gas injection take advantage of engine or burner exhaust, nitrogen or carbon dioxide. Preferred gases are those that are not overly reactive and show low levels of saturation in the liquid being transported. Through this the capacity of the gas compressor is reduced, which is necessary for spraying above the saturation concentration addition, excess gas is necessary. The beneficial results in pressure reduction are shown predominantly from undissolved gas.

The surge suppression

The pipe hammer or boil suppression can be canceled or be greatly reduced by injecting a gas into an excessively saturated gas in one Liquid. A large excess of about 5 to 10 times saturation is generally preferred twice the saturation value is necessary to obtain suitable results. Preferably is used to ensure the reaching of the saturation value the gas in a highly turbulent flow area in a liquid pipe system sprayed like a main or transmission line · In general, can also be a facility can be used to create high turbulence. A particular example of such a facility is in Figure 6 shown. Although this figure shows a T with a blocked part, the same

- 64- 609843/0276

Direction also in a curvature or the like. Or also are in a straight pipe part. According to the invention, the device 212 sprays a gas into the central part of the flow pipe of a main line or transmission line in the area of a facility for generating high turbulence such as a check valve or in the contractile vein caused by the flow through the opening 208a is formed, or something behind it. In such an area the longitudinal and axial concentration gradients kept very small. A second mixing opening located behind it is suppressed at the transmission length radial concentration gradients

Yet another turbulence device or limb which includes a gas injection device is shown in FIG. The short tube 145 in a flow tube 147 causes an area of high turbulence mixing · The entry into the short pipe section 145 is a flat or truncated annular 90 ° flange

· The position of the injection device 153 is preferably located at the vena contracta of the flow. Preferably the tip of the tube I5I is in the center of the short tube 145.

Another example of a turbulence device, which here includes a gas injection device, is shown in FIG 15 shown. Figure 15a shows an injection mixer elbow 222 with an opening 224 which is at the beginning of the radius of the elbow and at which a tube 225 in usual way is attached. A tube 226 passes through the bend and opening 224 so that the peak 232 in the turbulence and at or near the Location of the vena contracta, behind which the full

609843 / 027S

-65-

25523Ü4

- op -

le mixing takes place in the flow line 225.

The location of the tip 232 of the small tube 226 is important with regard to the mixing and the suppression of the concentration gradients. In general Tip 232 may be about 0.25 to 0.5 tube diameter behind or at a preferred distance from about 0.36 to 0.39 diameter with about 0.375 diameter as the optimum.

An opening in a flat plate in the curve is shown in i'igur 15c. The diameter of the opening is generally between about 0.7 to 0.9 times the line diameter and can be a peak (at about 60) that is led away from the opening. In Figure 15B, opening 224 is in a coupling or union 310 connecting the pipes or lines 301.

FIG. 15B shows the opening in the flat plate in FIG a coupling, but also in many other places, such as the T-flanges, bends and the like. Or can simply be on a straight part of the pipe «,

Also, many types of turbulence devices with gas injectors such as small pipes can be used. In Situations where the cost of injecting gas into a pipe or the like is low, needs a high one Mixing efficiency, i.e. openings in flat plate with coaxial spraying not to be required. Rather, it is sufficient to spray an amount of gas into a liquid that accounts for the total amount of gas required for the Saturation required in the flow tube exceeds. That

609643 / 02Ϊ6 - 66 -

Gas can thus pass through a normal straight part of a Pipeline or other places such as a check valve that is behind a pump, in tees, elbows, valves or bends, and turbulence-generating fittings.

The turbulence devices are preferably located far behind the liquid flow system, which preferably At least by a transmission length e.g. 25 to 40 times the pipe diameter for turbulence Flow and preferably by more than 40 times the diameter is removed to the saturation value of the To hold liquid or to allow it to reach where it would otherwise not be reached by the addition of gas through a non-highly turbulent area, such as a bend will. The number of such facilities depends largely on the system used.

The sheer effect of adding an excessive amount There is a gas above the saturation value of the liquid along the entire length of the flow pipe and the system Provide chamber for distributed air, which as a chamber for distributed convolution-suppressing air and less acts as a discrete air chamber. As already mentioned, preferred gases are those that are not excessive are reactive and show low saturation values for the respective transported liquid. It can thus many gases are used. Preferred gases generally contain oxygen, preferably ozone in a carrier gas, i.e. air, nitrogen, etc., nitrogen, carbon dioxide, air, neutral gas, e.g. from a pump driven by a diesel engine, distillation gases such as propane, butane, pentane, etc., and the like. more.

609843/0276

- 67 -

Although the turbulence suppression system described is generally used in a system for fluid flows can be used, it has been shown that it is particularly useful for suppressing flush pressures in a system for the transfer of liquids such as the flow system of a waste treatment facility described here can be used and connected to a main line.

Ventilation of an urban collection facility

A widespread municipal collection system was provided with a ventilation device · Before ventilation was the garbage picked up in the treatment plant septically showed no or only traces of dissolved oxygen and did not require any oxygen saturated in the garbage after entering the facility.

On the other hand, after all the main lines and wet sources were ventilated, the dissolved oxygen was in the garbage picked up 3 to 4 ppm. The garbage could as of its oxygen need of more than 10 oppm per hour shown to be treated. The dissolved oxygen content was sufficient to maintain the aerobic level Conditions due to the primary sedimentation. The effluent from this first stage treatment showed nor a dissolved oxygen concentration greater than 1.0 ppm. These results clearly demonstrated the effectiveness these teachings of ventilation. The desired suppression of odor and septic precipitation was a remarkable further result.

The ohlorization

The invention also contemplates that the mixing of

SG9843 / 0276

- 68 -

2bb2384

Chlorine using the openings in flat plates and spraying in many places under high moment exchange mixing conditions is clearly possible. The use of chlorine in a gaseous state for spraying a gaseous mixture or as a liquid Solution is concerned with the invention. Figure shows better places for a solution of chlorine and Water through line 40 into line 36 to outflow from the secondary settling tank 24. Further concerns the invention quite definitely the spraying of chlorine into the disinfection part 38 of FIG.

The sedimentation

The invention relates to the spraying in of aluminum chloride or another corresponding sedimentation agent into the effluent at a point in the treatment from the final disinfectant contact element to help clear the water when it is finally released into a stream, river or the like will. When using aluminum chloride, the invention relates to injecting 25 to 100 parts each Million, this being a polymer spray after a A delay of two or three minutes follows. For example, the aluminum chloride injection is carried out in a right angle Vessel 135 »clased to the bottom of the sprinkler filter canister 120 of Figure 4 is located. The container 135 would collect all of the water that passed through the filter media trickled and then flowed through the outlet line. For spraying aluminum chloride in For the outflow at this point, a plurality of transverse tubes 137 are provided, which run transversely to the container 135 (Figure 14), with the aluminum chloride injection

- 69 -

S09843 / 0276

_ ₆₉ _

through a tube 139 which is individually connected to each of the four tubes 137 of Figure 4 is connected.

Further mixing of aluminum chloride is then followed by passage through tube 138 and entering a section a plurality of short tubes 141 designed primarily for mixing. Also, because of the slow Flow rate the injection of polyelectrolyte resin take place with the coaxial injection in the vena contracta into the end of section 141, to act as a flaking agent known way to achieve. The short tube enables a very effective mixing arrangement. A single pipe 14-3 is shown schematically in FIG. The pipe contains a short pipe section 145 with a smaller diameter, the coaxial in the pipe section 147 with normal Outside diameter is arranged. The entrance to the section 145 takes place with a splash 151 with butt 90 ° angle, so that considerable and extreme turbulence arises in section 145. Spraying the Polyelectrolyte resin or other equivalent Resin can be passed through a small injection tube 153 which is arranged to be about 0.75 the diameter of the small pipe 145 is removed from the entrance, the flow being in the direction of arrow 155 .

With the short pipe, the inlet of the pipe creates a mixture. Such short tubes can be arranged coaxially or normally located in existing lines or extensions of existing lines. For example, three short tubes are to be arranged side by side in bundles in section 141, the

- 70 60984 3/0276

Flow goes down through one of the ends and reverses its direction a third time to see through a third short tube, running parallel. The respective arrangement of the short pipe can have an overall length in the three short pipes of that of the twenty times that of a single tube and should preferably not be shorter than ten times the diameter his

However, it is thus desirable that the mixture under a low thrust, especially in the case of Polyelektrolytharζ is carried out between 2 to 6 ppm and between 1 1/2 to 3 1/2 minutes after spraying is introduced by aluminum chloride.

It is said to be at a concentration of 0.1% or less can be added in water. The transition length of the short Pipe should be greater than 0.5 and preferably between 0.75 and 0.9, these figures showing the ratio the diameter of the opening to the diameter of the large flow tube 147 in FIG. You, the length of the pipe should be close to 25 to 40 times the diameter. This is a full possible transmission length .

In fact, the flow in the short pipe is shown in the figure 13 contracted a little more under high pressure for a given water depth or printhead. It has been found that the best length for tube 14-5 is likely to be about 2.5 times the diameter. Under these conditions the main loss is 0.328H, where H is the main hydraulic flow in front of the pipe when the pipe is deflated. It can be a full flow

- 71 809843/0276.

2552284

by, the tube will be contracted as the one mentioned Let flow through. It has been found, however, that these pipes do not need to be emptied. Pure for the most efficient mixing, non-laminar flow through tube 145 is at most desirable.

The use of the short tube also effects mixing under a hydraulic gradient rather than under a gravity gradient and in this way a high efficiency as well as a saturation is opposed achieved the values existing in gravity systems.

Another important aspect of introducing gas into the plant is by introducing more gas than to saturate The "fluid behind the pump is necessary is that the pump cost is not lost, but that." in this way, a pipe surge as a result of the pumping is considerably dampened.

The nitrification

Standard procedures contain carbonaceous BOD reduction. But there are new government regulations for the reduction of nitrogenous oxygen or NOD or for NOD has been enacted. This method and especially that according to FIG. 1 as optimal uses either the whole Nitrification doctrine or the whole falling point chlorination or a gap somewhere in between. The system should preferably be based on a two-stage sprinkling filtering Recycle more stabilized purification supernatant based · This leaves the filters with all of the nitrogen in Ammonia or NH, convert. NH, is then separated to nitrate or NO, or by falling point chlorination to Monochloramine oxidizes.

- 72 609843/0278

■ _ 2652384

The oxidation of KH, to NO, requires four to four six times the KEU nitrogen concentration in is continuously available to the current systems. In particular, these quantities were overlaid in the plant 140 ppm oxygen. Purely properly ventilated garbage with oxygen would result in an extensive fall pipe Allow use of oxygen to get NjEU to NO breakdown. This is preferably done before disinfection and is carried out by the OLo + HoO - spraying via the line 4-0 in Figure 1 shown. Then disinfection would take place after nitrification. It seems to be a more practical one to use the supplementary aerobic process and the aerobic nitrifying device described.

In this device the outflow can also be under a pressure in its flow path so that it is e.g. a gravity load is located. Much larger concentrations of gas or liquid can be used here become saturated. The effluent would be kept under pressure until the treatment is complete. Ventilation is more effective and easier under such pressure.

The individual exemplary embodiments according to the invention can be used to achieve an optimal method for converting from ammonia to ammonium nitrates, especially in waste or wastewater treatment plants. In general, the secondary treatment effluent from the garbage or sewage treatment plant may be sent to a Nitrification tower and treated in a way and by a process that is described in "Water ans Sewage Works, "August, 1974" pages 92 to 94,

β Ö 9 8 4 3 / Q 2 7 6 - 73 -

2B52384

around using a weak ammonia effluent a plastic sprinkling filter, such as from "Surpac" of the Dow Chemical Company. The use of each device, procedure and technique according to the Invention provide an improved method of producing ammonia effluent concentrations that exceed are the same low all year round.

According to the invention, the outflow of the secondary treatment can be fed to the nitrification tower via the distribution arm described are fed. The primary benefit of using this arm is the distribution of an equal Amount of discharge to each area or per unit area of the tower regardless of whether it is near the Tower center, on the central part of the tower or at a point located radially on the outside. This makes one improved efficiency and an improved distribution and thus a better use of the for the nitrifying available contact area.

The secondary treatment effluent can be aerated for delivery to the nitrification tower. The ventilation or the introduction of dissolved oxygen into the effluent can be done as follows:

A preferred introduction is the use of an injection nozzle in the conduit in the part of the vena contracta Turbulence causing the device to be like an opening in a flat plate. A preferred amount of oxygen is between 2 and 5 parts per million parts of secondary treatment discharge. The oxygen promotes nitrification or conversion of ammonia to nitrate.

- £ 74 0984 3/0276

Another aspect of improving the conversion of ammonia to nitrate involves the use of a pact By means of the nitrification tower, such as Berl Saddles, Cross rings and the like. Or the particular means described in which the hydraulic radius of the outer Flow channels is practically equal to the hydraulic radius of the inner flow channels.

This ensures effective mixing and thus better conversion, although the Plastic sprinkler filters or a rotating device (BIOSURF) can be used being a pact Device with the hydraulic parameters of the same internal and external hydraulics is preferred.

In general, it is more difficult to get a sufficiently low level of ammonia effluent because of the temperature difference to be achieved during the winter period than in the summer. Thus, one way involves isolating the nitrification tower to keep the outflow temperatures high and this makes it easier to keep the ambient air flow low through the packed base, which would otherwise would suppress the reaction rates because of the cooling. This air flow is in a ventilated one It is not necessary to flow into the nitrification process.

The system integration

The arrangement of all devices according to Figure 1 can work in the waste treatment. One way of working is to allow of all elements for flowing in a pipe, if the hydraulic and organic influence

-75-60984 3/0276

charge changes. The changes in these two charges are high. With an average charge, the range can - 75. Legal regulations state that the prescribed limits of the discharge quality must not be exceeded at any time. At a high fluctuating input load this means either that the procedure over most of the waste processing time must be regulated or that a difficult regulation to achieve the necessary degree of treatment constant is necessary. In the latter case, capital and operating costs are lower. The device, however, the conventional technique tends towards the earlier technique. This is the approximate and the simplified one Scheme for obtaining adequate treatment on an existing construction. With another Charge fluctuates the quality of the discharge.

Tests have shown that in the system with the sedimentation tank described, the DO value to the tank is between 2 and 3 ppm and from the tank between 1 and Λ 1/2 ppm to maintain the aerobic condition. This aerobic state persists between 20 and 40 minutes after it has flowed out of the sedimentation tank.

The scrubber

According to the invention, the scrubber, which contains an air washer, can be used for cleaning as well as with the ento · zoning of an ozonated gas. That is, the remaining or unreacted ozone from the wastewater treatment plants can be used to remove the ozone from the gas - if a scrubber is used a scrubber can also be used.

- 76 609843/0276

A two stage scrubber 250 shown in FIG can be of the general type and thus a packed medium 252 such as Rashig rings, Pal rings, Berl saddles, individual spiral media and the like. Included. The treatment medium can be at the top of the first stage of the scrubber through the reagent supply line 253 are introduced and drips through the first stage and collects in the drain 254-, from which it through drain line 255 to fill a container 256 flows out. The medium can then circulate again through a recirculation pump 257 or a part can can be delivered via the garbage line 258. The preparation can be added to container 258. A reagent container 259 with a pump 260 can be used for unloading at an injection mixing system on the pressure side the pump 257 are located. The reagent preparation for measuring the pump sump can be carried out by a swimmer or controlled by another scanning device. The scan can be a reagent or a treatment medium parameter determine.

The fluid to be treated in the scrubber turns on the end of which is given, as shown in FIG. 16, and has been mixed beforehand and the dirt is through the Using highly dissolvable fluids, precipitating fluids, or for conveying the Deposits catalyzed fluids or oxidizing or reducing agents removed. That too removing gas can be ozone with regard to the cited publication. From this stage onwards added the ozone-free fluid to the second stage.

- 77 -809843/0

.2 b 5 2 3 8

Although not shown, the second stage may be identical to the first in that it is packed media and the necessary containers, lines, and pumps to provide venting of the reagents and the reagent or media preparation for the second stage. The treatment medium can either be a highly soluble one Be a fluid, an oxidizing agent or a reducing agent. After treating the Both stages in the scrubber the fluid is cleaned well and then discharged by a fan 261. The first stage is separated from the second in the usual way and may contain eliminator plates 262, remove and mist the liquid droplets and thus prevent the liquid or treatment medium from entering the second from the first stage.

A conventional scrubber can be used instead of a scrubber This consists in particular of three elements: spray nozzles, scrubber plates and eliminator plates. The nozzles are located in a row along the path of the air and water flowing through them from one Pump pressed and in a fine spray or mist preferably in the distribution of the air flow is delivered. Counter-flow and cross-flow sprays can also be used. In some cases two and three rows of nozzles are used. The air is forced through the scrubber by a fan and thus brought into intimate contact with the water. Dry and soluble gases and crushed material being deleted. The correct clarification takes place however through the scrubber plates, which the flow direction so change that the dryness out of the air through its moment and through the rubbing of the air over the wet surface.

609843/0276 -78-

comes. The panels are either through the spray nozzles or kept flooded by a special row of nozzles above this. The scrubber plates follow a series of eliminator plates that remove the withdrawn water from the air. The lower part of the The scrubber forms a container into which the water flows and from which it is taken by the circulation pump will. A flood valve supplies fresh water to replace the evaporated water. It can also be one of the garbage Part of the container sump volume can be added via a waste line in order to discharge it from the system cause.

The air washer must prevent currents from the large amounts of dry matter that is washed out of the air and has settled in the container. This is a function of the trash pipe. At the suction line zujc Pump may also need a sieve for samples to prevent dust from entering the circulation system and in some cases special equipment may be necessary to cycle the spray nozzles through Rinse clean. The accumulated dirt must be cleaned out of the container at smaller intervals. In the case of a ventilation system in which the outside temperature falls below freezing point, the air washer must be used from frost either by a heater in the air stream in front of it or by an anti-freeze solution in the sprays be protected yourself. The air washer is well suited for cleaning the air from dust, but still has two other very important functions. It can be used as a humidifier or dehumidifier and as a cooler and as such is important in air conditioning. In the

- 79 609843/0276

2b52384

A freezing element is necessary for dehumidification and the spray liquid can very well be an anti-freeze solution with a preferred solubility for dirty gases that are primarily concerned.

Whether a cross-flow scrubber or a scrubber is used, another embodiment must include the aforementioned packing or the special packing Use Pall rings, Berl saddles, etc., the hydraulic radii of the inner and outer channels being practical are the same. This is described in U.S. Patent 3,730,881.

When the fluid to be cleaned is mixed with ozone from a garbage or wastewater treatment plant the ozone concentration must be reduced so that less than 1/10 part per million parts of gas is out the scrubber are ozone, as more than this concentration of ozone is toxic. The scrubber described with packed The pad and the characteristic hydraulic radii have been found to be very effective in cleaning either by solubility or by a chemical reaction at or below the critical limit, i.e. at 0.1 ppm O ^ shown in the fluid.

The scrub fluid is generally different at each scrubber stage in order to provide the best cleaning achieve. Although the scrubber can be used to remove or purify ozone, in general it will used in purifying a gas passing through a liquid in a fluid phase operation should be treated. Examples of other gases include ammonia, chlorine, hydrogen sulfide, sulfur dioxide

609843/0276 - ⁸⁰ -

and the like. Depending on the type of gas to be removed, this can first be carried out with a removable fluid, an oxidizing agent or a reducing agent are treated. Specific examples more solvable Fluids or absorbent agents that can generally be used contain liquid acids with 1 to 6 carbon atoms, such as acetic acid, propionic acid, aliphatic alcohols with 1 up to 8 carbon atoms such as isopropyl, butyl, amyl and the like. Glycol mixtures with 1 to 10 carbon atoms such as propylene glycol, anhydrides with 4 to 12 carbon atoms such as acidic anhydride and propionic anhydride, carbon tetrachloride and 3? reons that are at the operating temperature of the scrubber are liquid.

The oxidizing active ingredients can generally contain an active ingredient such as sulfurous acid, ethylene oxide, potassium permeate, Solutions of chlorine or chlorine dioxide, ozone and air or ozone and oxygen, nitric acid, various Metal dichromates, potassium perchlorate, hydrogen peroxide contained in water, sodium nitrite and the like. The oxidizing actives are relative to the component of the gas to be treated is generally known. Ethylene oxide is for sterilization with inert diluent gases (e.g. carbon dioxide and nitrogen) to suppress explosion hazards is desirable.

There can be a wider range of reducing compounds in the purification of a gas and especially one Component of a gas phase can be used. Special reducing agents contain sulfur dioxide, metal metabisulphite like sodium metabisulphite, cesium compound

- 81 -

6Ö98U / 0278

gen and the like .. Several compounds are known which act as reducing agents with respect to the desired component of the gas to be treated. Preferred reducing compounds for cleaning ozone contain sulfur dioxide and sodium metabisulphite.

For the removal of ozone, the first stage of the scrubber preferably contains an absorbent agent and since ozone tends to be an oxidizing agent, the second stage scrubber is preferred a reducing agent. Usually, ozone would be eliminated in the first stage. Then the second could Use a chlorinated spout or a very weak chlorine solution that is self-deodorizing is. However, the initial stage can use a reducing agent as the treatment liquid before second stage containing a releasable fluid compound as a treating agent. It so there are many variations. Preferred fluids for ozone include acetic acid, acetic anhydride, Proionic acid, propionic anhydride, carbon tetrachloride and hydrogen peroxide in water.

When using and cleaning a toxic gas such as ozone in air, chlorine in air, or the like, safety Provide barriers in the entire plant to avoid hazards and dangerous effects on people from ozone or to prevent chlorine explosions in the cleaning and operating areas. Furthermore, for security reasons as well as the need for effective spray mix and contact the location of the first injection of a toxic gas into the treatment process, preferably remote from the Scrubber business arranged.

609843/0276

.82-2b52384

The fluid-fluid treatment

According to the invention, a fluid, expediently a gas, can also be processed by another fluid be treated in the event of high turbulence, i.e. a Reynolds number of at least JOOO to achieve a corresponding Mix or ensure a moment transfer. In general, a cleansing treatment can be used with high turbulence affect a type of gas, although in the purification of ozone as it does in the treatment used by garbage, e.g. sulfur dioxide in particular suitable is.

Figure 17 shows the purification or treatment of a gas, which can take place in a preferably round flow line, such as a pipe 301 »The gas is fed into the Flow channel, as indicated by the arrow, given and conveyed through the channel according to the arrow and pushed out. It is very desirable that the Reynolds number be above 300 to ensure good turbulence. Preferably, to maintain a reproducible speed profile at the beginning of the Treatment, the grid 304- to suppress and decrease used by velocity gradients in the incoming gas. Usually the grid can be made of wire, plastic or the like. exist and be a coarse sieve. For example, there can be a sieve grid with parts of about 1.6 to be. The size of the grid and wires can vary. It is important that a grid is used which reduces the speed gradients. These Gradients have also been found in the delivery compartments of fans and fittings such as manifolds.

- 83 609843/0278

"" 2b5238A

Behind the grille 304 is a facility for creating high turbulence, which is an opening 306 in a flat plate. Generally can the device for generating high turbulence is located at a bend, a connection, a T-piece or the like. The treatment agent is preferably sprayed in near the opening, see above that rapid and good mixing can take place. This is achieved via a nozzle 308 which is in the middle part goes into the opening in the flat plate or into the turbulence device a little behind the vena contracta, which is conditioned by the opening. In general, the orifice diameter is in the range from about 0.7 to 0.9 times the pipe diameter. A minimum ratio of 0.5 can be used when there are high pressure drops. The position of the vena contracta is usually about at 0.25 to 0.5 times the line diameter behind the orifice plate, preferably at 0.3 to 0.39 and lies in the area in which the nozzle is preferably also located. Furthermore, to ensure complete mixing to ensure, at least one or a second turbulence device such as an orifice plate 310 behind it be arranged. The wide turbulence device 310 the first can be identical and is preferably located at least at a distance of 25 to 40 times Diameter or more, preferably at least 40 times the diameter behind. This is done in order to ensure the correct length for thorough mixing. The second turbulence device also ensures good mixing and thus provides the best contact for cleaning the gas. That treated or purified Gas can then in the usual way by longer con-

- 84 -

■ -609843 / 02 7 6

tact, before being expelled into the atmosphere by recirculation or by being added to the process or the like.

Although the nozzle may generally be a thin tube, a preferred nozzle 350 is shown in Figure 19, the a first part 352 with an average Having thickness. The diameter of the nozzle of the second part increases proportionally until a thinner one Ring 353 at the tip is formed as indicated by arrow 354 on the manifold. The slope of the cusped part is less than 7 ° and lies approximately at 2 to 3 ° · The thickness of the ring should be about 0.25 mm at the tip of the manifold. The diameter increases in proportion to accommodate a pressure drop of a fluid such as a gas and around to give good strength and rigidity to the manifold. Such a distributor tends to reduce the Flow of gas. Because of the very thin ring at the tip of the nozzle, the fluid that is injected becomes kept in very close proximity to the fluid in the line, creating eddies that normally occur occur with thick-walled nozzles. In addition, because of the lack of vertebrae, an additional one is made Thrust that ensures good mixing of the injected fluid in the area of the vena contracta the turbulence device promotes.

In general, the high turbulence cleaning -or Treatment system with one fluid and with a sufficient amount of a second fluid be treated for the purpose of cleaning .. This is done through

609Ö43 / 0276

Absorption, or by, a highly soluble fluid by chemical reaction or the like. And contains detoxification, odor control and the like .. In addition, can the fluids can be either liquids, liquid and gas, or gases.

The cleaning or treatment plant with high turbulence is of particular importance for waste or wastewater treatment, where harmful and poisonous gases such as ozone, chlorine, hydrogen sulfide, various organic odors, Ammonia and the like. Occur. After sterilization or deodorization, the treated should therefore Fluids contain ozone in oxygen or ozone in air. It can be oxidizing or reducing Active ingredient or an absorbent or high-quality agent Fluid active such as that relating to use in a cross-flow scrubber or scrubber has been described. An absorbent compound such as propionic acid can be added via nozzle 308 and in the vena contracta part behind the first turbulence device ejected with further turbulence or further mixing at least 25 times the flow line diameter that is provided by a second device 310 is effected with an opening in the flat plate. In the same way, other compounds can be used to treat of the ozone can be added through the nozzle 308 and sulfur dioxide can also be purified.

The invention is explained with the aid of the tables below, in which the smallest flow velocity for turbulent flow or mixing is given in Table I for a fluid system in which the greater length corresponding to either the contact time of 40 seconds or a transition length of 40 times

- 86 609843/0278

Diameter is used.

Table II usually shows the specifications for a gas-liquid system in the case of the turbulence device
how to use a flat plate opening.
Table III shows a particularly good mixture obtained using a turbulator in a line of a dual fluid plant. To determine the extent of the mixture, five samples at 30 times the diameter were taken behind the point of the system at which water vapor (gas) was sprayed into the air (gas) in the vena contracta part of a flat plate opening.

- 87 609843/0276

Minimum flow parameters for injection mixing systems for two Fluid:

diameter

in cm 20 40 60 90 125 152

in dm ⁵ / see. 1) 80 158 236 555 500 600

in dmVmin. 2) 4700 9500 13700 20500 29750 36300

in m max. 3) 97.548.8 48.8 21.8 15.5 13.1

in m min. 8.3 16.1 24.4 36.8 50.9 61.0

Speed

in m / min. 146.0 73.5 48.8 48.8 23.4 19.5

Pressure drop

in H ₂ O / m 0.189 0.018 0.0045 0.0012 0.00041 0.00246

Pressure drop

in H ₂ O / Ind. Min. 0.35 0.11 0.06 0.03 0.01 0.005

Pressure drop
in H ^ O / contact
^d total

Ozone requirement

ⁱⁿ dm ⁵ / h 4) 36.4

Oxygen cond.

ⁱⁿ dm ⁵ / m 5) 3.1

1) is based on the limitation of the Reynolds number for turbulent flow DY = 5

2) is based on a contact duration of 40 seconds

3) is based on 150 times the diameter

4) based on 2.5% in air and a can equivalent to that

609843/0276 " ⁸⁸ "

Nitrogen saturation which results in 0-, in a liquid concentration of 0.56 ppm.

5) based on 5% 0 * in Op, 40 ppm saturation of oxygen.

603043/0276

_ 89 -

Characteristic parameters for oxygen or air, gas-
Liquid injection mixing systems.

These data apply to the minimum capacity to secure the turbulent flow

diameter

in cm 2.5 5.1 10.2 15.2 30.5 45.7

Q min,

in dmVsec. 1) 0.76 1.53 3.05 4.58 9.15 13.7

Q min -z

in dmVmin 3.45 6.00 1350 2100 4150 6100

length

in m 2) 60 30 25 10 5 3.4

length

in my-

spray mixing

Speed min. In
m / sec. 1) 1.5 0.75

Air requirement

No - saturated

in dm ⁵ / min 4) 0.87 1.78

Ozone supply

in kg / day 0.37 0.07

Oxygen demand
O ₂ saturated

in dm ⁵ / min 5) 1.4 2.8 3.0 8.5 17.0 34.0

0.38 0 , 25 0.13 0, 085 3.5 5 , 3 10.5 15th ,8th 0.15 0 , 22 0.40 0, 68

(O ₃ at 0.56 ppm) 0.83 1.68 3.3 5.0 10.0 15th , 0 Ozone supply
in kg / day 435 0.2
208 0.045
45 21 9 1 , 5 Pressure drop
in cm in
spray mixing stage 490
5300 340
9,550 0
45 0
21 0
9 1 0
, 5 Pressure drop
in cm
Contact level
Pressure drop
in cm. Total

-90-

1) based on the Reynold number limit for turbulence

flow DV = 5

2) is based on a contact duration of 40 seconds

3) is based on 150 times the diameter

4) based on 2.5% 0, in air and a dose equivalent Nitrogen saturation, the one / O ^ in a liquid concentration of 0.56 ppm.

5) based on 5% o, in Op »40 ppm - saturation of oxygen,

The first point is on the radius at which the area of the following circle or ring equals a quarter of the total area is. The ratio of opening to pipe diameter was 0.75 The following values were obtained:

Table III

Digit R-Test / R 0 0.354 0.61. 0.788 0.932

Total DBT, ⁰ C 18.2 18.2 18.2 18.2 18.2

WBT, ⁰ C 15.8 15.8 15.9 15.9 15.0

Grains, Kg 32.6 32.0 32.2 32.2 32.2

link

ppm 10286 10286 10157 10157 10157

As can be seen from Table III, very small differences in concentration were obtained at the various locations on a radius. In addition, the concentration fluctuation was generally Λ% less than the average concentration. This table thus shows that an excellent mixture is achieved even after a transition length of 30 times the diameter. This is done with the preferred minimum transition

- 91 -

609843/0278

length of 4-0 times the diameter compared that necessarily results in a better mixture · The invention thus relates to the inclusion of an additional downstream turbulence device to ensure mixing through the entire system. It also shows that a flat-plate opening with an opening ratio of 0.75 »d.as on the pipe diameter based, good turbulence mixing conditions »- gene granted.

Several types of fluids, such as gases, can also be treated. There is also a particular advantage of the reactor in the line for generating chemical reactions with gas-liquid systems in the ability to change the pressure and / or temperature in the pipeline reactor compared to what is in the reaction vessel, packed documents or the like. Is available. Major industrial processes involving gas-liquid reactions are the individual examples after "Examples of Processes of Industrieal Importance where Gas Absorbtion is Accompanied by Chemical Reaction ", Gas-Liquid Reactions, P.V. Danckwerte, F.R.S. McGraw-Hill Series in Chemical Engineering 1970, to which reference is made for the individual reactions. An excerpt from this article with examples is as follows:

- 92 -

SG9843 / Q27S

1. GO ₂ , COS, H ₂ S, Eq ₂

(i) Absorption of GO ₂ and GIp in aqueous solutions of barium sulphide for the production of BaCO ^ or BaCl ₂ , see Gupta, EK and MM Sharma: Ind. former Engr. 9 (1967) Trans 98.

(ii) absorption of CO ₂ in aqueous suspensions of calcium oxide to produce precipitated CaGO: see Morris, EH and ET Woodburn: South African Chem. Processing (June - July 1967) CP 88

(iii) Absorption of CO ₂ in aqueous suspensions of MgO to produce basic MgCO ₅ , see

(a) Shreve, E.N .: Chemical Process Industries, 5th edition McGraw-Hill, 1967.

(b) IFaith, W.L., D.B. Keyer, and H.L. Clark: Industrial Chemicals, 1965 "J. Edition, John Y / iley and Sons, Inc. New York.

(iv) absorption of CO ₂ in aqueous suspensions of gas, see Chem. Engng. 75 (1968) 94.

(v) Absorption of CO ₂ in aqueous solutions of silicic acid soda, see Dalmatskya, EJ: J. Appl. Chem. USSR 40 (1967) 464 (English translation).

(vi) absorption of CO ₂ in aqueous solutions of Na ₂ S.

(vii) Absorption of CO ₂ in aqueous solutions of carbonate of potash or amines to remove SO ₂ from synthetic gas, see Danckschwerts, PV. and MM Sharma: Chem. Engr. (October 1966) CE 244 (see 10-1).

SQ9B43 / 027S

2. CS ₂

Absorption in aqueous ^ miolösungen for the production of dithiocarbamates, see Kothari, PJ and M ₀ M. Sharma: Chem. Engng, Sci. 21 (1966) 391.

(i) Absorption in aqueous solutions of GuGl for conversion into CuCl ₂ and copper oxychloride: see Ihaveri, AS and MM Sharma: Chem “Engng. Sci 22 (1967) 1 (see 10-3).

(ii) oxidation of Na ₀ SO, by air or oxygen, used to construct the characteristics of the absorption device (see 10-3).

(iii) Air oxidation of acetaldehyde, butyraldehyde, etc. to the For the preparation of corresponding acids and acidic anhydrides, see

(a) Marshall Sittig: Organic Chemical Process Encyclopedia, Noyes Develop. Corp., USA, 1967

(b) Vrbaski, T., and I. Brihta: Arhiv. Kern 24 (1952) 111; Approx. 49 (1952) 163.

(C) Kostyck, N.G., Loov, S.V., Falkovski, V.B., Starkov, A.V., and N.M. levona: Zh. Procl. Khim. 35 (1962) 2021, J.Appl. Chem. USSR 35 (1962) 1939 (English translation).

(iv) oxidation of cyclohexane to adipic acid; see Steemann, J.W.M., S. Kaasemaker, and P.J.Hoftizer; 3rd European Symposium Chem.Engng, Chem. Reaction Engng. Oxford, Pergamon Press, 1961, pages 72-80 =

609843/0276

(ν) Air oxidation of cumene to cumene hydroperoxide (precursor of phenol), see

(a) Low, D.T.R .: Ganad. J. Chem Engngo 45 (196?) 166,

(b) Maninov, O ₀ V. et al .; Khimiya i Tkh. Topliv., Masel (1967) (12), a (Brit. Ghem. Eng, Abstact 1968 May, p. 712).

(vi) air oxidation of toluene to phenylformic acid; see Faith, EL, DE Keyes and HLClark: Industrial Chemicals, 3rd Edition, 1965 ₅ John Wiley and Bons, Inc. New York.

4. Eq ₂

A. Additive Chlorination

(i) reaction between Cl ₂ and C ₂ H ₁ - in a C .- ^ LClp medium; see Balsubramanian, SN, DH Rihani, and LK Doraiswamy; Ind. Engng.Chem. (Basics) 4 (1965) 184.

(ii) Re & ktion between Cl ₂ and C ^ H ^ in a GJiL-Gl ₂ medium see Goldstein, FR; Petroleum Chemicals Industries, 2nd Edition, 1958, London, E. & F.N.Spon Ltd.

(iii) reaction between Gl ₂ and OpHp to form tetrachloroethane; see Marshall Sittig; Oranic Chemical Process Encaclopedia, Noyes Develop. Corp., USA 1967

(iv) Reaction between Cl ₂ and trichlorethylene to give pentachloroethane ("precursor of perchlorethylene); see Goldstein, RF, Petroleum Chemicals Industries, 2nd Edition, 1958", E. & FN Spon Limited.

6Ö98U / Q27S

B. Onset of chlorination

(i) Chlorination of a variety of organic compounds such as benzene, toluene (side chain as well as, nuclear), phenols, etc. see e.g. Hawhins, P.A .: Trans. Instn. Chem. Engrs. 4-3 (1965) T. 287.

0. Miscellaneous

(i) Reaction of CIp with sulfur or sulfur monochloride for obtaining sulfur monochloride and sulfur dichloride

(ii) reaction of CIp with SCU to obtain sulfur chloride, see Eirk and Othmer: Encyclopedia of Chemical Technonoly, Volume 13, 2nd Edition. 1967 »New York, Interscience Publisher, pages 319 »4-03.

(iii) reaction of CIp with PCI, for obtaining FeCl, see Gilliland, ER, BF Raddour and PLT briam: AKChem. EJ 4- (1958) 223 (see 10-2)

Absorption of SO, in HpSO. for the manufacture of oleum, see Duecker, WW and J ₀ R. West: The manufacture of sulfuric acid, Reinhold Publishing Corp., New York 1959

6. ₂

Absorption in water for ENT recovery, see

(a) Andrew, S.P.S. and D. Hanseon: Chem. Engg. May be. 14 · (1961) 105;

(b) Kramers, H., M.P.P. Blind and E. Snoeck; Chem. Engng. May be. 14- (1961) 115.

7. COCl ₂

Absorption of GOCIp in alkaline solutions; see Monague, V / .H. and R.L.Pigford: A.I.Chem.E.J. (1960) 4-94-.

8. H ₂ hydrogenation of a variety of unsaturated organic compounds in the presence of catalysts; please refer

(a) Satterfield, CN. and T.K.Sherwood: The Role of Diffusion

in Catalysts, Addion Wesley. 1963.

8098 £ 3/07 75

(b) DeBoer, J.H. et al .: The Mechanism, of Heterogeneous Catalysts, Amsterdam, Elsevier Publishing Co., 1960.

deuterium

Ammonia-hydrogen process for separating deuterium; see (a) Bourke, P.J. and J.C. Lee: Trans Instn.Chem.Engrs.

39 (1961) 280.

(b) Bourke, P.J. and D. Pepper: Trans Instn. Chem. Engrs 41 (1963)

10. Olefins

(i) absorption of sobutylene in aqueous solutions of HpSO ^ to produce tertiary butanol and to polymerize to di-iso - and tri - isobutylene; see Gehlwat, JK and M ₀ M. Sharma; Chem. Engng, Sci. 23 (1968) 738.

(ii) Absorption of isobutylene in phenols and phenols used in the presence of HoSO ₂ . as a catalyst to produce the corresponding alkylated products 5

(a) DeJong, J.I .: Rec. Trav. Chem 83 (1964) 469.

(b) Whitney, W _0: Ind.Eng, Ghem. 35 (1943) 264.

(c) Jelinek, J .: Chem. Prrumysl 9 (1959) 398; Approx. 54 (I960) 8696,

(iii) absorption of butadiene in coppery ammonium kamplexen; see Morell et al., Trans. A.I.Chem. E 42 (1946) 473

(iv) absorption of butenes in sulphurous acid for conversion to secondary butanol; see Rustanov, HE and MN Chirkov: Zhur.Fiz.Khim 30 (1956) 261;
Approx. 50 (1956) 11081.

(v) Absorption of acetylene in aqueous CuCl solutions for Convert to Vilylazetylenj

see Marshall Sittig Organic Chemical Process Encyclopedia, Noyes Develop.Corp. UNITED STATES. 1967.

609843 / 021Ö

(vi) Absorption of ethylene in benzene to produce ethyl benzene using AlCl, catalysts see Marshall Sittig: Organic Chemical Process Encyclopedia, Noyes Develop. Corp. USA 1967

(vii) Absorption of acetylene in arsenic trichloride dissolved in CpHpCl ₂ . for the production of chlorovinyldichlorarsine: see Whitt, FR: Brit.Chem.Eng. 12 (1967) 554.

609843/0276

(viii) Absorption of ethylene in sulfur mono- or dichloride dissolved in benzene chloride to make you! oridinäthysulfid: see Whitt, F.R .: Brit. Chem. Eng. 12 (1967) 554- (there are also further examples)

11th SO ₂

(i) Absorption of SO ^ in aqueous solutions of NaHS (X and NapSO, in the presence of zinc dust to produce Dithionite: see Suzuki, Ε., Ε.Ο. Shima, and S. Yagi: Kogyo Kagaku Zasshi 69 (1966) 1841.

(ii) Reduction of SO ₂ in SO, »/ HSO ₅ ■ * - buffer by Na Hg amalgam.

(iii) Absorption of SO ₂ in aqueous solutions of NaNO ₂ and zinc dust to produce hydroxylamine.

12. HGl and HBr

(i) absorption of HCl and HBr in higher alcohols to produce the corresponding alkyl halide (e.g. lauryl alcohol in lauryl chloride or bromide); see Kingsley, H ₀ E. and H. Bliss, Ind. Eng. Chem. 44 (1952) 2479.

(ii) Addition of HBr. to alpha-olefins for the production of alkyl bromide with starting bromine atom, e.g. methylundecylenate reacting with HBr ₀

(iii) Addition of HGl to vinyl acetylene to produce Chloroprene.

Instead of a conduit with means for generating multiple turbulence, further embodiments include suddenly changing the diameter of a Pipe or a flow line as well as a multiple branch. Any of these devices are supported reducing the overall length that would otherwise be necessary for mixing, and thus the significant Reducing the necessary physical space. Regarding the sudden change in diameter is located a turbulence device is preferably at the end of a tube with constant diameter, which is with a pipe of constant ^ diameter or a flow channel of larger diameter is connected. For example can be a four inch pipe with a flat plate opening at its end with a diameter ratio, sufficient to remove the boundary layer, be connected to a 2 or 2.5 m diameter pipe. Such an opening at a sudden change in diameter ensures mixing and thus a suppression of radial concentration gradients. In such a situation there is a downstream turbulence device at a distance of at least 4-0 times the pipe diameter.

The multiple branch consists of a pipe or a flow line that suddenly turns into several pipes smaller diameter with a large total conduit flow area skips if the same pressure drop per meter is to be maintained on the long line. For example, a single pipe with a diameter of 1.22 ι can suddenly branch off into 24 · pipes with a diameter of 0.3 m. The first turbulence device is preferably located in each branch relatively close to the transition from

- 100 Θ09843 / 0276

a single tube into the multiple tubes. After this Embodiment can have the transition length of 40 times the diameter, i.e. 12 m χ 12 m to 12 χ 0.3 m, which is a reduction of 40 m. Thus, other turbulence devices be arranged behind it.

Regardless of the respective exemplary embodiment, the addition of a treatment agent according to the aforementioned Publication will take place.

In conveying the fluid from one area of the plant such as a treatment part to another The diameter of the flow channels can be changed »For gradual transitions to the area If the subsonic flow is delayed, the diffuser transition should not exceed an inclination of about 7 °, in order to be able to suppress boundary layer separation. However, this tendency is not critical for Transition nozzles that accelerate the subsonic flow.

Preferably after a fluid phase treatment station with downstream mixing, e.g. by a second or third turbulence device a contact chamber may be provided, the purpose of which is the Lengthening the attack time of the fluid being treated after ideal mixing has arisen.

The ozone generation

An improved method of generating ozone can be used in accordance with the invention. Generally required an ozone gate the supply of oxygen with a gas, a voltage potential and a very low one Pressure. When the voltage is applied, the oxygen in the supplied gas is partially converted into ozone under pressure. It is known to contribute to the production of ozone

S098 & 3 / Q278 _ ₁₀₁

high gas feed rates can be maximum. These result relatively low concentrations of ozone in the gas. It is also known that ozone changes by changing the supply rate of oxygen and the voltage can be generated. It has been shown to work on this such a way as maximizing the concentration of ozone that can be done in a treated Fluid is dissolved. Electrical energy is required in kilowatts per kg of ozone generated. In particular, the supply or amount of oxygen with gas that is given in the ozonator with the respective device increased to the largest possible amount. This will be less than the maximum or sized Maintain ozone production.

This reduction in ozone production is greater than a gain in efficiency in gas-liquid injection and the mixing which can be derived in the following step is achieved. This way of working an ozonator increases ozone production by allowing higher concentrations of ozone in a treated fluid within the limit of the saturation amount of a component of the carrier gas in the treated Fluid. For example, an ozone concentration of 2.5% is possible with air supply. From the air the nitrogen solubility in water is 18 ppm. The air supply is proportional to this amount of nitrogen, which would be 22.5 ppm air, 2.5% of which would be ozone. The supplied Op and Ο ,, would at Stabilize 4.5 ppm, except exhaust oxidation reactions the ozone. The corresponding concentration of ozone in the fluid being treated would be 0.56 ppm.

- 102 -

S09843 / 027S

Ozone fluid solutions are bactericidal and viricidal at ozone concentrations of 0.5 ppm and higher. This technique thus achieves a disinfection without due to the gas-fluid saturation in the treated Fluid to result in a loss of ozone in the gas that is blown through the flow system.

Gas supplies at rates above that of saturation Gas component in the fluid is corresponding and must be followed by a gas blowing. When blowing through ozone and unsaturated gas components are lost. It follows that the working principle is feeding of gas or gas mixtures at the lowest possible rate, preferably at limits of gas component saturation or less. Is potential loss of ozone from an ineffective gas-fluid mixture many times greater than the loss of ozone generating capacity caused by the ozonator operation at maximum practical ozone is induced in oxygen-containing gas concentrations. It thus follows that the at Cold from kwh / kg ozone focused ozonator enhancements where the ozone is at the highest possible ozone concentrations is generated in the oxygen-containing gas, are mostly desirable. The ozone can thus with a subsequent process, e.g. in garbage or wastewater treatment plants as well as for other common purposes be used. An important factor is that the process only uses the smallest possible amount of oxygen required so that a maximum concentration and amount of ozone is generated when the voltage is applied.

- 103 -

609843/0276

2S52384

The characteristics of the ozonator

The production rate of an ozonator depends primarily on the applied energy - »· Operating regulations result usually a wide range of incoming gas that must contain oxygen. An increase in the Oxygen concentration to twice that for air roughly doubles the ozonator production rate. at The addition of 100% oxygen will cause a small increase in the production rate over that for oxygenated Air observed at 4-0% oxygen concentration.

When the gas supply rate to the ozonator increases, the concentration in the ozonated output flow decreases " The decrease is mostly inversely proportional to the input feed rate. At a gas supply rate Wg in Kg per minute and an ozone concentration C in parts per million is the ozonator production rate in the output gas W in kg per minute almost constant. This is shown in FIG. The volumetric feed rate becomes used in place of the weight feed rate. The relationship at the log-log coordinates is mostly linear. the Relationship w. C = W would be a straight line

result. The dashed line shows this relationship.

The diagram also shows how reducing the energy supplied to the ozonator can reduce the rate of ozone production. In practice it is this is the only control of the ozone output with the exception of changing the oxygen enrichment of the Ozonator feed gas.

- 104- -

609843/0276

FIG. 36 also shows the energy requirement for ozone production only. Additional energy is required to dry and compress the ozonator feed gas. From this it follows that a maximum ozone production takes place near the central area of the representation. The ozone production in the lowest area of a display is therefore not significantly less than that for the maximum state. The lowermost portion of a gas supply rate corresponds to the maximum concentration of ozone _o It has been shown that the efficiency of gas-liquid is potentially at the highest achievable Ozonatorausgangskonzentration greatest. The overall efficiency of the applied ozone is derived by operating the ozonator at minimal gas flow rates which somewhat offset the ozone production. The compensation is higher than the compensation due to the improved injection-mixing efficiency.

With this recommended method of operation, the total energy requirement per kg of ozone generated is also used in the overall system decreased · This is because of the considerable decrease in the gas supplied for drying and the energy for compression necessary with the ozonator gas feed rates kept to a minimum. A The contributing factor to this fortuitous circumstance is the modest effect of nitrogen in the ozonator gas. To about 60% nitrogen in the feed gas does not significantly reduce the rate of ozone production.

Usually the comparable formation of an ozonator with the supply of enriched air in the recommended low gas supply rate with that for normal Considered flow rate. The comparable ozone

- 105 -

609843/0276

concentrations are 55 mg / 1 and 25 mg / 1 and correspond the concentrations at the outlet of the ozonated gas of 1.69% or 2.1%.

This comparison appears in the table below. There the production rate column shows the ozone output slightly above the relatively low ozone concentration of 2.1% with 25 mg / 1. This happens at the highest rate. The specific energy column shows that this high gas rate of high energy determinations for drying and compressing the ozonator feed gas.

These states are the same as those for production at 55 mg / 1 or 4-6% ozone concentration in the ozonator outlet compared. The lowest feed rates prevail there. At 200 watts, the ozone production rate is 14.6 g / h at low gas rates and 17 »3 at high gas rates, which is a reduction of 16%. The specific Energy for the low gas rate is 18.5 kWh / kg. and that of the high gas rate 25 kWh / kg. Here is the decrease 25%. So 16% of production is sacrificed for 25% savings in energy.

In addition to this economic advantage, the ozone concentration enables a noticeably increased ozone inlet to the fluid being treated. The overall efficiency the system becomes significantly larger, while the energy requirement is reduced by 24%. Ultimately, that results Feed gas with oxygen-enriched air further advantages. Enrichment with 4-0% oxygen and 60% In comparison, nitrogen doubles the ozonate primary production with production at Lufto

-

609843/0276

Lower oxygen enrichment is proportional advantageous. A particular enrichment is of interest. It should be noted that water saturated with air shows a dissolved gas distribution of one part oxygen to two parts nitrogen. This has turned out to be shifted from the exit of the gas distribution in air from one part oxygen to four parts nitrogen.

It can be expected that the oxygen enrichment from air to 33% oxygen, 66% nitrogen in equilibrium with which one to two ratio would be. When the oxygen concentration in the saturation gas of the As the fluid increases, so does the oxygen concentration in the dissolved gas. Because of this, lies the preferred range of oxygen-enriched supply air for ozonation is between one third and two fifths of oxygen.

Under these conditions, the desorbed, ozonated carrier gas recirculates as much as possible a minimal supply of oxygen to the desired enrichment of the feed gas upright. This type of ozonator operation, i.e. low feed gas, Flow, recirculation, high ozone concentration and oxygen enrichment of the supply desire contains the optimum the overall system for generating and dissolving ozone in the fluids being treated. These working conditions of the system are the optimum of the total cost of ozonation per unit weight of the treatment agent dissolved ozone.

Small amounts of treatment oxygen may be required in this facility. This can consist of one-page

- 107 S09843 / 027S

Oxygen generators from LOX storage or from one Gas phase storage devices are supplied. Because the equilibrium concentrations of dissolved gas in air-saturated water is 33% oxygen, 66% is nitrogen from another source of treatment feed gas possible. Pressurized water is mixed with air saturated, and then depressed. Desorbed gases are recovered and consist of 33% oxygen and 66% nitrogen. They represent an almost ideal ozonator feed gas that is enriched with oxygen can be.

A typical plant for generating ozone is shown in FIG. A compressor 710 carries the fluid, preferably air through a length of drilling rig with turbulence devices to ensure a complete mixing, such as the flat-plate openings described, which are separated from each other by at least 40 times the diameter of the pipe. The fluid is then held in a high pressure vessel 715, which contains nitrogen enriched with the atmosphere. The fluid then passes through an expansion valve 716, which can be a hydraulic turbine generator, for recovery in electrical energy or in mechanical form. To a low pressure absorber 720 that contains an atmosphere-enriched nitrogen. Each container contains water, part of which is taken from the second or low pressure absorber by a pump 721 and a pipe system 722 revolves around. The air or fluid then goes through line 723 to the dryer 725, which can be iron acid deposits, in where the air is alternately directed to one container and not to the other.

- 108 -

9843/0278

Characteristics for ozonator and feed gas compressors

Feed Gasra Ozonator Ozone con Ozone pro gas te power centering duction IA watt mg / 1 Rate W SA °

Energy consumption in kwh / kg. Ozone gas dryer overall compressor

Oxygen 265

200

I. angerei
chert 207 160 £ T> air 152 120 O
CD 40% 0 98 80 CD ozone -C ^
CO dd 480 200 > «S
O "1 382 160 to »I. 307 120 σ) Il 194 80 ti 694 200 ti 550 160 Il 419 120 It 292 80 air 282 ' 200 It 208 160 Il 158 120 dd 104 80

55

55
55

35
35
35
35
25th
25th
25th
25th
25th
25th
25th
25th

14.6 10.4

8.4 5.4

16.8 13.4

10.7 6.8

17.3

13.7

10.5

13.4
15.4

14.4
14.8

11.9

11.9

11, 1
11.8
11.8

11.7
11.5

11.0
28.7
30.9
30.9
30.9

5.1

4.0

2.9 1.8

9.0

7.3

5.7

3.7

13.3

10.4

7.9 5.5 5.3 4.0

3.1 2.0

18.5 19.4

17.3 16.6

20.9 19.2 16.8 15.5 25.1 22.1 19.4

16.5 34.0

34.9 34.0

32.9

This method is generally used for drying by freezing below dew point. With regard to the Liquid in reservoirs 715 and 720 can use water but in general liquid of higher solubility for oxygen than nitrogen is used. The air is then after. Drying is applied to an ozonator via pipeline 728. The one High concentration of ozone-containing fluid is then supplied via conduit 735. a contact container 74-0 led, in the mixing devices how flat plate openings are included. After the contact container, part of the gas or fluid flows back to the dryer, while the liquid e.g. water can be pumped out in the contact tank.

The rotating distributor arm and the nozzle for the sprinkling filter

In a sprinkler filter, the bed under the distributor arm is said to be with a uniform flow above it Area, expressed in liters per square meter and day, can be dosed with liquid. A common maximum rate is 40,000 liters per square meter per day. It's for efficiency and economy of operation, that the dose rate is necessary with a total flow pressed onto the system is uniform with the radius. The reason for this is that when the flow rate is depressed, the Flow from the distributor the filter medium must be metered with the same flow rates per area. Since the Filter area changes with the square of the radius, the flow on the outer edge is with a cutting edge Mistake. Except when the current is channeled

- 110 -

609843/0276

if the filter is in operation, the Tendency towards speed-dependent flow distribution i This tries the middle section of the arms to dry and to move the larger flow to the outer radii of the arm. It's a special one Problem of ensuring uniformity at low flow rates.

Figures 20 to 23 show the distributor arms 399. A dashed line 400 in Figure 22 runs below the center line of the arm 399 and represents a closure that isolates a channel that only the Half of the total channel available for flow in the filter manifold for a lower portion of the section holds. FIG. 25 shows the cross-sectional formation better and clearly shows the manifold section 400 as well a horizontal manifold section 402, which will be discussed in detail. In Figure 25 lies the top surface of the manifold 402 is substantially at the same level as the centerline 404 of the opening 405 (the opening 410 cannot be seen in FIG. 25). The places of the opening are in the greatest number, is available for the hem and allows the effluent to be removed from the distributor arm.

The construction of Figure 25 serves to isolate the effluent flow until the level moves to the upper surface of the distributor 402 builds up. It must be assumed that the flow occurs at a variable rate, when it is distributed through the distributor arm. This flow rate depends on the speed of rotation of the arm. A usual maximum rate is 90,000 liters per square meter per day. By doubling the width

- 111 -

609843/0276

of the channel above the manifold 4-02 that has actually been achieved, however, will be a further increase the current, with a reduced change in height at the discharge opening. This will make the area decreased in one variable. Other means that can be used and the rate of distribution change, change independently the diffuser nozzle to regulate the axial pressure, the speed of rotation and to improve the diffuser flow so that the dose rate is at an imposed total flow is uniform within the radius. Unless the flow is channeled, one tends to the filter in operation is the flow distribution velocity to make dependent. It has therefore been shown that by blocking the lower part of the section through divider 402, flow is assured at a low rate and at high rates the effect of increased flow is reduced by accommodating it with a smaller change head.

An additional feature of the distributor arm 399> What is of interest is that the diffuser openings (Figure 24), which are located in different places on the Length along the manifold arm in Figures 22 and 2J are in elevation, i.e., rotatable. The flow passage can therefore be changed by turning the opening. That way you can accordingly the opening design uses the rotation to change the head and the flow or to change the moment will. The change in moment results in a contact pressure. This causes the distribution speed, which in turn affects the head at the distributor radius.

609843/0276

. na. 2bb2384

It is thus important that the head, flow and moment in an orifice be changed independently can. The openings 210 (Figure 28) contains a hex nut 212 to allow the openings to be changed can be mechanically rotated in the direction of their bearing pressure.

Figures 29 and 50 show a modified opening with a 90 ° knee »This can in turn by means of a hexagon nut 212a using a wrench or rotated by hand pressure. It can be turned vertically up or down for unloading will. This changes the head and the current significantly. The change in moment is a function of the speed the liquid as well as the angular position of the opening.

Each nozzle 210 in FIG. 28 contains a gap 214 which is ground into a round pipe section 216 containing the nozzle. Furthermore, an end cap 218 has a gap 220 which is cut so that there are two separate columns for control purposes. Preferably, the gap 220 is elongated and round at the ends but offset eccentrically from the center line 222 · By turning the gap 214 upwards, the Flow decreased because the head got smaller. In this case (Figure 28) a flow from the Exit gap 210, but not from gap 214 ·. When the gap 214- is rotated downward, the gap becomes 220 at the end of the cap turned up so that there is no flow directly from the end of the cap, but the all or almost all of the flow to the filter bed

- 113 -

609843/0276

25S238 *

drains from gap 214. Independent changing the relative flow and the pulsating force at the same time can be changed by mutually changing the Angular positions of the two rotatable elements, namely the cap 218 and the nut 212 and the pipe section, 216 done with the nozzle 210 ,,

The rotation of the nozzle elements can be done by hand, but more conveniently using a key. Primarily the idea of adjusting the angle position should be the column for the regulation contain changes in the flow that occur progressively in a system, can, usually an increase in flow, which over a long period and less daily increase changes without causing the radial dose uniformity to the filter bed.

The speed of the distributor arm is therefore important because the distributor moves because of the propulsive force turns. Like the changes in speed, there is an effect on the pressure distribution in the arm from the fact that the liquid surface is paraboloid in a rotating vessel. Approaching the head the tip of the distributor is higher than that in the figure due to the difference in the sizes of the parabolic ordinates Center. The general effect of the head enlarged to the tip of the arms would be the current in that area enlarge disproportionately. This is one of the reasons why the measurements are in relation to the nozzle gap for regulating the relative speed of the distributor and also the measurements for regulating the flow channel according to FIG. 26 have been made, which has already been done has been mentioned. This mailing list contains the

-11 4-

B09843 / 0278

2552284

illustrated embodiment independent means and gives the need for adjustment to achieve the basic goals for unifying the correct ones Flow distribution per unit area of the absorbing medium under the arm over the area and radius.

As a further result, the rotatable cap 418 makes it easier to clean up material that has got into the openings or column 414 and 420 has reached. Figure 24 shows that the nozzles 410 are arranged very closely, so that the number of gaps or openings in an arm can be very large.

It is further in connection with FIGS. 20 to 23 Note that the nozzles appear on the upward side of the manifold arm as well as on the downward side. The purpose of the up jet is to further regulate the propulsive force and the speed to allow the flow in the distributor without compensating for the uniformity of the flow metering per Area unit of the absorbing medium is created under the filter.

Another option with the type of distributor arm is to insert a plug lock instead of spray head nozzles (Figure 28) to adjust the flow regardless of the openings. That is, by removing the nozzles and placing them in a replacement row of nozzles, which is a standard pipe plug, the flow can be regulated.

Another detail of the construction of the manifold is a hole 4JO (Figures 22 and 23) to prevent the

- 115 -

809843/0278

The creation of a vacuum and another feature of the arm's structural requirements are the retaining struts 432 (Figures 20 and 21) used by various Points along the arms back to the center beam 4-34- for the arms in the cantilever style from the center distribution head 436 run out. The retaining struts 4-32 compensate for the horizontal forces caused by acceleration and the construction of the Arms itself is such that it acts as a variable section module beam from the radius of Hull to the radius of the Pointed act so that they are carried at independent points by the rods 4-32, which are so inserted This means that the manifold can be tuned when it is intended to operate in a horizontal position Level is installed with no stress that could occur in a cantilever arm.

The variety of retaining struts and the stress analysis of such a distributor is based on approximation of the intermediate structures with a continuous beam, which is held on three intermediate beams will. It can be used analytically at least as a bar with a constant section. After that she has to Analysis to be refined for checking. The section module changes from one to the length of these arms Large cross section formation near hub 436 to a much smaller cross section formation at the top and thus the section modulus and stress analysis need to be better thought out in order to record the change in the section module as a function of the radius of the manifold. In other words, it is a feature of the invention that the arms

■ 609843/0276

are pointed or uniform along their entire length have decreasing cross-sectional area. The pointed training makes the arms less sensitive to it Changes in the speed of rotation of the manifold and the brief changes in the manifold flow and responds to the effect of a larger flow volume from the nozzles, the further they are from removed from the center of the hub because it is the area of the filter media that requires greater flow because a larger area is covered the further they are from the center of the honeycomb.

As FIG. 25 shows, the cross section of the arm is practically rectangular and the manifold 400 is also used as reinforcement between the upper and lower flange 401 and 403 of the arm which served as a stiffening beam. The sheet 400 is periodic with holes 405 that carries fluid in the upper channel of the unlocked section as well as in the normal Canal enter.

FIG. 26 shows the same cross section as FIG. 25, except that it is practically twice the height with the unlocked Areas 440 and 442 that are blocked in both the upper and lower channels. The upper channel (overflow channel) is separated from the lower channel (normal flow channel) by a horizontal partition 445. the The intention is to have the upper section working under high plant flow conditions and the ensure correct distribution of the flow at the radius of the manifold regardless of the height of the flow. This results from the fact that an extremely high

- 117 -

609843/0 2 76

The flow rate normally rotates an irrigation filter excessively fast. The high speed knocks the liquid out of the outer radius of the distributor, which distributes the flow through the medium can not flow uniformly per unit area. In the embodiment according to Figure 26, however, holds the manifold is about the same width or height ratio in cross section as in Figure 25 for the normal Distributor. The height and width ratio is the same for the double channel distributor arm as for the Single channel.

To understand the operation of the double-channel or overflow design according to i'igur 26, FIG. 27 serves, in which the central column 435 is a filter with the flow in the direction of arrow 4-50. The normal flow of the effluent is in the normal flow channel according to arrow 4-52. However, if the current builds up above the overflow pipe section 4-54, an overflow occurs in the seal of arrow 4-56 and from there into the overflow flow channel of the distributor arm (Figure 27).

The equation for this is Ge = 3 »33 · c. H ^ The sketch of the diagram in FIG. 27 shows h which does not flow over when the upper part of the overflow is raised will. Basically, the above equation gives the overflow flow taken into the upper channel when the flow goes over the overflow. The flow then increases in the lower channel or in the channel the normal flow at a flow value around what is cut off for the respective head h.

After reaching the upper part h, it would overflow

in the upper or overflow channel in quantities or at

- 118 -

609843/0276

Get flow rates given by the equation. The top of the overflow is then the actual top of the water level at the edge of the overflow, as marked as tu in Figure 27 is what the top of the liquid means.

The flow in the rotating distributor arm is thus dominated by two things. These are the nozzles and the speed of rotation of the distributor. These are the only factors that affect the pressure distribution affect the length of the arm. So this procedure of regaining an overflow and guiding into the upper level of a two-level distributor with the same pointed design for the cross-section of the bar as Figures 20 to 23 show at a single level or a double level distributor arm.

In the case of the other turning knee according to FIGS. 29 and 29a, the distance in FIG. 29 represents the displacement of the End of the nozzle from the center line of the entrance to indicate that rotating the nozzle will open the top changes. Figure 29A shows that the end of the nozzle at 460 is flattened to broaden the flow of fluid as it is dispensed from the nozzle, so that the falling streams of adjacent nozzles overlap.

The diagram of FIG. 30 shows a curve 470 with the The ordinate, the percentage of turbidity, and the abscissa, the concentration values of the electrolyte feed represents. This curve therefore shows the optimal concentration of the polyelectrolyte supply to the maximum removal of suspended matter »This is

- 119

£ 09843/0276

with regard to the other operational versions important for a system that uses polyelectrical feed to remove suspended matter!?.

The injection mixing system with the contact tank

The injection mixing system with a contact container 500 is shown in Figures 3I through 34. The container 500 has a practically rectangular cross-section with an inlet container 502 (FIG. 32), with a contact container 504 and with an outflow container 506. A flow tube 5Ο8 directs the influence through a corresponding one Y-valve manifold assembly 512 in one Tube bundle 510. Tube bundle 510 removes from the tube 5Ο8 on the influence and first conducts it through a corresponding injection mixing elbow 514 (FIG. 34) there through downstream flat plate openings 516 and 518 and thence to the hold tank 502 for dispensing through a hypobolically reshaped diffuser 520. The flow from the inflow container 502 into the contact chamber 504 takes place through appropriate locking gates which are controlled by an operator station 524. The flow from the contact container 504 into the outflow container 5Ο6 lies behind an overflow device 526.

The details of the injection mixer elbow 514 (Figure 34) are a 90 ° elbow 530 with a flat plate opening 532, which is at the rear end of the pipe separation between connected to the flanges between the knee 530 and the next pipe section 534 behind it. In order to achieve an effective mixture of ozone, e.g. as a common disinfectant, spraying takes place through an injection tube 536 on the flow axis

- 120 -

6098U / 027S

of the tube 534, but that of the knee 530 (Fig goes out. This type of spray mixing is mentioned in US Pat Patent application described. The flow is indicated by arrow 538.

Because of the system parameters for which the respective spray mixing system according to FIGS. 31 to 34 is intended was, the inflow pipe 508 has a diameter of 120 cm and is branched into twelve independent lines indicated by the tubular handle 510 are. The branch has a width of about 135 cm at the bottom of the contact container 504-. The pipe collar 510 consists of a tube with a diameter of 30 cm made of polyvinyl chloride. You can by 30 cm offset from its centerline above the bottom of the container. Except for the injection mixing opening in the knee 514 are 15 »3 m behind, which is 50 times the diameter of the tube is (just over 40 times diameter is preferred) flat plate mixing ports 516 and 518 intended.

Influence then has after having a full spray mix through knee 512 and the orifices 516 and 518 has given a full concentration of Ozone or some other injected medium, and from there the flow arrives at the location of the container for the normal influence at the end of the contact container. The inflow mix lines are vertical through the contact chamber 504, guided upwards and cross the wall between the inlet container and the contact container. At the lower edge of the injection mixing line the flow in the inflow tank 502 goes through the

- 121 -

609843/0276

hyperbolic reshaping diffuser 520 that controls the flow from the pipeline to the wall directed outwards and a hyperbolic layer on the wall with the Mixing of the material in the hold tank 502 is created. The resulting mixed product then crosses the Shutter gates 522 in each of the four independent channels , which by partition walls 504-a (Figure 31) in Contact container 504- are divided.

The spout 506 discharges into a spout 560 (Figures 31 and 32) 1.8 m in diameter. Sample connections can be made on tube bundle 510 for the Check the dissolved oxygen and pressure to be established. Usually the outflow channel would even for dissolved oxygen and / or biological tests to confirm the absence of fecal coliforms that exceed the provisions. A typical determination could be 200 fecal coliforms per 100 ml. This is a very high value and it it is possible to achieve less than 2 faecal coliforms per 100 ml if a one percent concentration of ozone is injected is used on knee 512. The section of the hyperbolic diffuser 520 is a reshaped hyperbolic section that decelerates the flow. The flow hits the inlet tank wall where it mixes with the contents of the container, before the mixture passes through the lock gates of the inlet container into the correct contact container ter has arrived. The diffuser enlarges in the area on the flow path and the knee portion to decelerate the current. The deceleration is intentional as is the creation of a hyperbolic layer on the impact wall. The diffuser should not exceed 7 °

- 122 -

609843/0276

-122- 2552284

Channel diverge, otherwise a boundary layer separation occurs on. However, for practical and economic reasons, it is more common to use an ordinary knee diffuser rather than making a specialty piece to use the equipment for the purpose. Most necessary spray mix and contact In the previous sections, pipes with a diameter of 30 cm were made, that is, the tube bundle 510 which is the real elements for spray mixing and the contact of whatever disinfectant used, either the described ozone systems or chlorine solutions in water.

In the embodiment described in connection with Figures 31 to 34, the number of elements that pass through the contact container in the system design is based on an available head of 0.88 kg per square centimeter, which corresponds to a water column of 66 cm . Of the 66 cm water head available, 40 cm is used for the pressure drop in the 30 cm pipes, of which there are 12 when the flow for the system is at its maximum. The maximum flow for this version is 378.5 million liters per day. Thus the pressure drop is below
under these circumstances a relatively conservative figure under the circumstances o the overpressure is obtained because this is a physical treatment plant. If the
Pressure drop could be more conservative, the pressure can be controlled and a reduction in the number of pipes is possible, ie for the 12 pipe elements
by inducing the diameter from, for example, 30 cm to perhaps 40 cm or more. But it also has to

- 123 -

609ÖU / 0276

_ ₁₂₃ - 2bb2384

Requirement of preferably 40 times the diameter must be observed between the mixing openings, so that the total length of the system is in the order of magnitude from 120 to 150 times the diameter.

Another limitation and consideration that must be placed in all plant designs is a possible need for many ways. One way would be to inject sulfur dioxide which would deoxidize the ozone or chlorine in the final effluent and would also remove the excess oxygen. A second option is to use thiosulfate, a chemical reagent that destroys ozone and reduces oxygen levels, and / or chlorine. A third possibility is the use of a mechanical ventilator, such as a Cöchrane-feed water deaerator, which is used in boiler feed water systems _o The maximum of the determination for dissolved oxygen is for this construction is present at a nominal value of 20 milligrams per liter. This would either limit the ozone capacity available for delivery or require de-oxidation by the equipment described below.

The aeration system for activated sludge

FIG. 35 shows an aeration system for activated sludge in schematic form. For normal ventilation about 848 cnr / kg are used in such a system. This means 100 kg air per kg BOD or 20 kg oxygen per kg BOD and actually represents an efficiency of 5%. With this system, 8.2 to 16.4 kg Air per kg used, which is up to 10 kg of air per kg of BOD or

- 124 -

609843/0276

1 to 2 kg of oxygen per kg of BOD or an efficiency of 50 to 100% means »

Activated sludge (Figure 35) is generated from one or more locations on container 600 near the lower outer edge from one or more corresponding deep head centrifugal pumps 602 sucked through suction lines 504-. The pump then returns via lines 606 to a practically in the middle and back upward outlet or discharge line 603 near the lower center of the container 600. This creates a vortex flow in the elliptical orbits of arrows 601 and ensures that all of the liquid tries to flow or move around the web in the container. There shouldn't be any stagnating Areas are located.

In order to then spray air into this embodiment, appropriate air compressors 610 are on the line to level the air into the discharge line 606 approximately the same type of injection mixing system as the injection elbow 514 connected according to FIG. 34. This gives a maximum diffusion of the air in the outflow from the pumps 602, suppresses radial concentration gradients and makes an extremely effective way of aerating the activated sludge, normally the pump is 602 a deep head, high volume pump that is widely available is ο

- patent claims -

- 125 -

609843 / Ö276

Claims (1)

Patent claims: A surge suppressor system for steaming Boiling pressures with a main line that carries a liquid, characterized by an injection device for introducing a gas into the main line a gas into the main line (14), the amount of which exceeds the amount required to saturate the liquid, and so do the boiling pressures dampens. 2β system according to claim 1, characterized in that the amount of gas is at least twice the saturation value. 3. Plant according to claim 2, characterized in that the device for introducing a gas is a short Pipe (210) is in the main line. 4. Plant according to claim 2, characterized in that the main line (14) has a device for generating of high turbulence, so that an area of high (turbulence is created. 609843/0276 BORO MÖNCHEN: 8 MÖNCHEN 22 ST. ANNASTR. 11 TEL: 089/22 85 44 TELEX: 1-85844 INVENd TELEGRAM: INVENTION BERLIN TELEPHONE: BERLIN 030/885 60 37 030/888 23 82 BANK ACCOUNT: BERLINER BANK AQ. BERLIN 31 3695716000 - 126 - POST CHECK ACCOUNT: W. MEISSNER, BLN-W 12282-109 5. Attachment to. Claim. 4, characterized in that the unit for introducing a gas into the main line is in the high turbulence area. 6 .. Plant according to claim 4, characterized in that the high turbulence device is an opening and the insertion device is a small pipe » 7. Plant according to claim 4, characterized in that the main line has at least one more high one Has turbulence generating device, which is located behind the first turbulence device. 8. Plant according to claim 7 *, characterized in that the downstream turbulence device by the length of 40 times the diameter of the main line behind it lies. 9. Plant according to claim 1, characterized in that the gas from a group of oxygen, ozone in a carrier gas, nitrogen, carbon dioxide, air, natural gas, Exhaust gas and distillate gas consists. 10. Plant according to the preceding claims, characterized by the use in a plant for Dirt suppression and through a main line for guiding a discharge. 11. Plant according to claim 10, characterized in that the main line is in a wastewater treatment plant is « _ 127 - 609843 / 027S 12o method for cleaning a gas with an installation according to claims 1 to 10, characterized in that the gas is a scrubber with a packed base is added, Process according to Claim 12, characterized in that a two-stage scrubber is used, in which each stage has a compacted bed, and the gas
is guided through each stage. Process according to claim 12, characterized in that the reducing agent is from the class of
Sulfur dioxide, a lietallbisulph.it and cesium compounds is taken. 15ο The method according to claim 12, characterized in that the oxidizing agent from the class
Sulfuric acid, potassium permangnate, chlorine solutions, nitric acid, metal dichromates, potassium perchlorate,
Hydrogen peroxide and sodium nitrite comes from. 16. The method according to claim 12, characterized in that the solubility agent from the class of
Acids with 1 to 6 carbon atoms, aliphatic alcohols with 1 to 6 carbon atoms, glycol mixtures with 2 to 10 carbon atoms, anhydrides
with 4 to 12 carbon atoms and carbon tetrachloride is taken. 17. The method according to claim 12, characterized in that
that the gas is also obtained from a waste or wastewater treatment process « - 128 609843/0276 18. Procedure according to. Claim. 17, characterized in that that the gas is an ozone-air mixture. 19. The method according to claim 18, characterized in that that the active ingredient of high solubility is added to a stage of the scrubber and an oxidizing active ingredient is added to the other stage. 20. The method according to claim 19, characterized in that that the reducing agent is one of the stages of the scrubber and the oxidizing agent is the other Level is added. 21. The method according to claim 12, characterized in that the packed support contains a packing medium and the hydraulic radius of the medium approximately equal to the hydraulic radius of the outer flow channels is. 22. The method according to claim 21, characterized in that the medium from the class of Pall rings, Berl, saddles, single spiral media and Rasching rings are selected. 23ο Method according to claims 12 to 22, characterized in that that it is used to treat one fluid (gas or liquid) by another Fluid is used that the fluid is supplied to a flow line so that the Reynold's number is at least 3000, and the flow line has a device for. Creation of turbulence contains that the treating fluids the flow - 129 809843/0276 added flow channel and a treated fluid is expelled. 24 _β method according to claim 23, characterized in that the treating fluid flow line is added in the vicinity of the turbulence means ο 25. The method according to claim 24, characterized in that that the turbulence device is an opening in a flat plate and the spray point for the treating fluid is located in a vena contracta of the opening. 26. The method according to claim 24, characterized in that that the flow channel has at least one downstream turbulence device, which is in a Distance at least 25 times the cable diameter is located. 27. The method according to claim 24, characterized in that the disruptive agent is a gas and the treating agent Fluid is a gas. 28ο Method according to claim 26, characterized in that that the downstream turbulence device at a distance of at least 4-0 times the pipe diameter is arranged and both turbulence devices are openings in flat plates and that the spray point is in an area of the Venacontracta the opening lies. - 130 809843/0276 29o method according to claim 28, characterized in, that the diameter of the opening of the turbulence devices between 0.7 to 0.9 times the pipe diameter lies" 30. The method according to claim 29, characterized in that the injection parts approximately at a distance of 0.36 to 0.39 times the cable diameter is behind the flat plate opening. 31. The method according to claim 17 »characterized in that the treated liquid from the class of 0, NIL ,, COp, GOS, HpS, GIpGS ₂ , SO- ,, NO ₂ , GOGl ₂ comes from ₀ 32. The method according to claim 26, characterized in that the treated fluid comes from the class of O ₅ , Gl ₂ , H ₂ S, NH ₅ and SO ₂ . Process according to claim 26, characterized in that the treating fluid is from the class of CaS, NapS, potassium carbonate, potassium amines, HpSO ^., NaHSO ^, amines, GUCl, compounds from the class of Na ₂ SO ^, acetaldehyde, butyraldehyde, cyclohexane , Cumene, toluene, G ₂ H ₅ in CgH ^ Glg medium, C ₅ H ₆ in C ^ HgGl medium, GpH ₂ , trichloroathane, benzene toluene, phenols, phenol substitutes, sulfur, sulfur monochloride, sulfur dioxide, PCI, FeCl ₂ , H ₂ SO ^, water, alkali solution, coppery ammonium complexes, arsenic trichlorides dissolved in C ₂ H ₂ Gl, SO ₅ , FaNO ₂ , HBr, vinyl acetylene and higher alcohols. 33 · The method according to claim 17 »characterized in that that the treating fluids from the class of sulfur dioxide, a metal bisulfite, cesium compounds, Sulfuric acid, potassium permanganate, chlorine solutions, 809843/0276 -131- _, ₅₁ _ 2S52384 Ethylene dioxide, chlorine dioxide solutions, ozone, nitric acid, metal dichromates, calcium perchlorate, hydrogen peroxide, Sodium nitride, acids with 1 to 6 carbon atoms, aliphatic ^ alcohols with 1 to 8 carbon atoms, glycosyl mixtures with 2 to 10 Carbon atoms, anhydrides with 4 to 12 carbon atoms and carbon tetrachloride. 34. The method according to claim 26, characterized in that that a grid is provided in front of the turbulence device. 35 »Method according to claim 24, characterized in that that the line has a suddenly increasing diameter behind it or behind a branch with larger overall line area * 36. The method according to claim 35 »characterized in that the treated fluid from the class of O ₃ , NH ₅ , COS, H ₂ S, Cl ₂ , CS ₂ , O ₂ , SO ₅ , COCl ₂ , H ₂ , SO ₂ , HGl, HBe and olefins is taken. 37 · The method according to claim 35 »characterized in that the fluid treated is taken from the class of O ^, Cl ₂ , H ₂ S, NlU, and SO ₂ . 38 »Method according to claim 24, characterized in that that the treating fluid is from a manifold with a tapered wall thickness of less than 7 ° is added. that the taper is around 2 ° to 3 °, 39 · The method according to claim 38, characterized in that - 132 809843/0: 76 40. The method according to claim 38, characterized in that the thickness of the wall at the tip of the distributor is about 0.075 to 0.15 ™ &. 41. The method according to claim 38, characterized in that that in the turbulence device the ratio of Opening in the flat plate to the flow line is between 0.7 and 0.9. 42. The method according to claim 38, characterized in that the flow channel has at least one downstream Has turbulence device at a distance of at least 25 times the pipe diameter will be arranged » 43. The method according to claim 42, characterized in that that the fluid comes from a garbage or sewage treatment plant and from the class of ozone and chlorine o 44. Plant according to claims 1 to 11, characterized in that that in a two-stage disinfection of material that a distribution of ammonia-ammonium compounds contains a primary oxidizing agent for the material to be disinfected and for reducing the pH of the material and a secondary oxidizing agent to maintain a very small number of bacteria and a substantial amount of ammonium compounds are added. 45. Plant according to claim 44, characterized in that the primary oxidizing agent of the first stage and the secondary oxidizing agent of the second stage are added becomes β 609843/02 76 46. Plant according to claim 45, characterized in that that the primary oxidizing agent from the class of chlorine iron and aluminum chloride and the secondary Oxidizing agent is taken from the class of chlorine, chlorine dioxide, ozone and sodium hypochlorite. "Plant according to claim 45, characterized in that that the treated material is garbage or sewage discharge is. 48. Plant according to claim 47, characterized in that the pH value is below 0.7 and the ratio of Ammonium compounds to ammonic compounds is at least 97%. 49 · Plant according to claim 47, characterized in that the amount of the primary oxidizing agent of the first Level is added in at least 50 parts per million. 50. Plant according to claim 49, characterized in that the tightness of the secondary oxidizing agent of the second Level in at least 0.7 parts per million is added. 51. Installation according to claim 48, characterized in that the ammonia nitrogen is 95% plus ammonium. 52. Plant according to claim 49, characterized in that the number of faecal coliforms is less than 2 per 100 ml. 53. The method according to claims 1 to 11, characterized in that that when used to generate ozone - 134 609843/0276 a feed gas containing pressurized oxygen, and a voltage potential is used, a maximum voltage is applied to the potential, that a minimal amount of a gas containing oxygen is supplied and generated for ozone generation Ozone is sprayed into the fluid. 54-, method according to claim 53 »characterized in, that the feed rate of the gaseous oxygen is at the saturation limit of the gas. 55 · System according to claims 1 to 4-1 and 4-5 to 53 » characterized in that a nitrification tower with a pacted base is provided for generating ammonia is, to which a secondary treatment effluent is led from the waste treatment plant, which with Oxygen is vented into the outflow through a small pipe near the turbulence device is introduced. 56. Plant according to claim ^ _9, characterized in that the added amount of oxygen is 2 to 5 parts per million of the outflow. 57 · Plant according to claim 55 »characterized in that the outflow through a distributor, which is practically the same amount per unit area over the entire area the packed document is fed to this document. 58. Plant according to claim 55 »characterized in that the packed medium has a hydraulic radius of the outer flow channel, the practical 609843/0276 -135- is equal to the outer flow channels « 59 · Plant according to claim 55 »characterized in that that the nitrification tower is insulated. 60. System according to claims 55 to 59 »characterized in that that when using a ■ distributor for the influence of a wastewater treatment plant in connection with a sprinkler filter a central rotatable distributor head takes up the influence of an elongated rod from the top of the Head assumes that at least two distributor arms are connected to the head and are horizontally symmetrical starting from it balanced, with each arm being a constantly changeable section module as Function of the radius of the arms and that of several rods from different places along the length of each Armes to the rod to support the arms in a horizontal plane without stress, and that along the length of each arm there is a nozzle through which the influence is discharged. 61 · Installation according to claim 73 »characterized in that the arms have a practically rectangular cross-section with the longer sides running horizontally, and that the nozzles are on the shorter vertical sides. 62.-Plant according to claim 61, characterized in that a central vertical stiffener is provided between the lower sides to obtain two channels, and the stiffener has holes to allow an inflow between the channels and a - 136 609843 / C276 wrong soil is made possible in one of the channels, so that the flow path is vertical across the channel . 63 · Installation according to claim 62, characterized in that the nozzles are in a channel next to the false floor and on the usually front side of the arm and that the nozzles in the other channel next to the bottom side and on the normally rear side of the Armes are arranged. 64. System according to claim 63? characterized in that the nozzles contain at least two inlet discharge ports and means for independently "varying the height of each aperture with respect to the flow path of the arm are provided. 65ο System according to claim 64, characterized in that the nozzles have a rotatably mounted pipe section with a hat on one side and a rotatable closure for the end of the pipe section with an eccentrically arranged slot included. 66. Plant according to claim 62, characterized in that the nozzles have a pipe section with a practical 90 ° knee included and that the end of the section is open but shaped into an elliptical diffuser which overlaps the spray of adjacent nozzles. 67 · Plant according to claim 46, characterized in that to achieve a disinfectant mixture using a contact container into the inflow inlet - 137 S098A3 / 0276 leads, a branch is led from the inlet opening that is led through the tube bundle that in each tube of the bundle a mixing device with a flat plate opening and high moment exchange it is provided that a device for spraying a disinfectant into each tube the point of the highest moment exchange is provided that a device for causing the influence flow from the source of influence to the contact container and the means for effecting the connection from Contact container to the outflow and a hyperbolic reshaped diffuser to deliver the influence the tube bundle is intended for influence. 68. System according to claim 67? characterized in that Each tube of the bundle by a length of 120 to 150 times the diameter from the point of disinfectant injection is removed and at least two flat panel opening devices behind the The spray point is 4-0 times the diameter away. 69. Installation according to claim 68, characterized in that the diffuser in addition to a vertical wall is arranged in the outflow container so that a hyperbolic layer of influence on this wall which mixes with the fluid in the inflow tank. 70. Plant according to claim 69 »characterized in that the diffuser is in the form of a reshaped hyperbolic section to decelerate the flow. - 138 609843/0276 71. Plant according to claim 69 »characterized in that that the diffuser is arranged in a 90 ° knee that is seven degrees divergent in cross section expands from the flow path of the fluid. 609843/0276 Blank page