CA1090488A - Apparatus for on-site renovation of sanitary waters - Google Patents
Apparatus for on-site renovation of sanitary watersInfo
- Publication number
- CA1090488A CA1090488A CA308,943A CA308943A CA1090488A CA 1090488 A CA1090488 A CA 1090488A CA 308943 A CA308943 A CA 308943A CA 1090488 A CA1090488 A CA 1090488A
- Authority
- CA
- Canada
- Prior art keywords
- chamber
- bioreaction
- waste water
- chambers
- submerged
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1242—Small compact installations for use in homes, apartment blocks, hotels or the like
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
A B S T R A C T
A self-contained apparatus for on-site renovation of sanitary waters comprises of three bio-reaction chambers, a mineral storage and dispensing container, a submerged suspended solids separator located in the third bio-reaction chamber, a flow equalizer, a chemical oxidizing agent dispensing system, a chemical oxidation-clarification chamber and a charcoal containing chamber, all enclosed in a single tank designed for use as on-site single or multiple family waste water renovation system.
A self-contained apparatus for on-site renovation of sanitary waters comprises of three bio-reaction chambers, a mineral storage and dispensing container, a submerged suspended solids separator located in the third bio-reaction chamber, a flow equalizer, a chemical oxidizing agent dispensing system, a chemical oxidation-clarification chamber and a charcoal containing chamber, all enclosed in a single tank designed for use as on-site single or multiple family waste water renovation system.
Description
T I T L E O F I N V E N T I O N
"Apparatus for On-site Renovation of Sanitary Waters"
S P E C I F I C A T I O N
This invention relates to an apparatus for on-site renovation of sanitary waters and has for it's object a provision of an improved apparatus capable of unattended an reliable operation when purifying sanitary waters to a high quality effluent suitable for limited reuse.
'~' -.
",.~: :. ~
1~90~8~
BACKGROUND TO THE INVENTION
It has become evident that nitrogen and phosphorus affect the productivity of aquatic life - nitrogen being the limiting nut-rient in eutrophic waters and phosphorus in oligotrophic waters.
It is also known that domestic waste waters contain from 10 to 100 times the nutrient concentration of agricultural or forest drainage. COnsequently in densely populated areas overfertil-ization of surface waters, algae growth and chemical pollution have been noticed along with degradation of potable water sources and the need for more efficient removal of all pollutants from waste waters has become more obvious.
While removal of phosphorus can be achieved reliably by chemical precipitation and removal of organics by biological followed by physical-chemical processes, removal of nitrogen is more comp-licated.
The biological transformations of nitrogenous compounds occur through biological processes of ammonification, nitrification and denitrification. The first two require presence of oxygen, the denitrification require absence of oxygen. The two distinct mechanisms responsible for removal of nitrogen and reduction of nitrite and nitrate are (a) - formation of ammonia followed by transfer of ammonia into the anabolic cell metabolism which is of minor importance since C:N ratio in cell tissue is 5 - 6, whereas in domestic wasteiwaters only 2 to 2.5 and (b) -microbial denitrification, which is a respiratory reduction in which nitrite and nitrate replace oxygen as the final electron acceptors in the respiration chain.
Bio-oxidation of organic matter, ammonification and nitrification cause no problem. Nitrification is efficient and reliable if organic loadings are maintained below 0.3 lb BOD per lb of mixed liquor suspended solids per day, sludge age is maintained above 3 -4 days and dissolved oxygen in the mixed liquor is maintained above 1.0 - 2.0 mg/lit. The higher is the concent-ration of mixed liquor suspended solids, the more efficient is ~090~
the transformation of ammonia to nitrite and nitrate. The overall rate of denitrification is a function of the concent-ration of the heterotrophic facultative bacteria present in mixed liquor suspended solids and their activity in the absence of oxygen. To maintain the activity the denitrifying bacteria must be supplied with suitable organic material - source of energy.
From the process point of view to accommodate the different food and oxygen requirements of bio-oxidation of organic matter, ammonification and nitrification of nitrogenous compounds and decomposition of nitrite and nitrate by microbial respiration and to achieve acceptable reaction rates and efficiencies, the various biochemical reactions are currently being carried out in separate process stages. While the conventional activated sludge process is capable of removing nitrogen with efficiency of 50 -60 per cent, the current multistage processes can achieve the removal of nitrogen with efficiency of up to 80 -90 per cent.
The multistage processes currently in use in large municipal treatment plants require treatment facilities that are too com-plex to be scaled down to small package pla~ts to serve small developments or single family dwellings. Because of the number of process steps required for removal of the various pollutants renovation and reuse of domestic waste waters at present seems feasible only if practiced on a large scale.
A large waste water treatment -renovation plant however requires ~ .
large underground sewage collection -transportation network, and in case the renovated water is to be reused also a large under-ground water distribution networ~. Such networ~s are expensive to build and even more expensive to maintain and to operate.
It is therefore obvious that on-site renovation and reuse of waste water would be economically more attractive than renovat-ion and reuse of waste waters via central collection-treatment distribution. However because of the complexity of the involved treatment on-site renovation and reuse of domestic waste waters as yet can't be practiced.
1090"~
Although at present small package sewage treatment plants are available, they do not provide the required degree of purific-ation that would permit reuse of the purified effluent and in general they also lack the required mechanical reliability.
It is therefore the prime object of this invention to provide an apparatus in which the various processes to remove all poll-utants present in sanitary waters could be carried out reliably, unattended and at acceptable cost when serving.single or multiple family dwellings.
More particularly it is the object of this invention to provide an apparatus that would reliably maintain all conditions required for efficient bio-oxidation of organic mat`ter, biological nitrif-ication, biological denitrification, chemical precipitation of soluble phosphates, chemical oxidation of the residual and ref-ractory organics and toxic compounds, efficient kill of bacteria and viruses and efficient removal of the residual chemical oxid-izing agents so as to render the effluent non-toxic to aquatic life and suitable for reuse.
Another object of this invention is to provide an inexpensive and reliable method for storing and proportioning of the various chemicals to the unsteady or batchwise flow of the incoming waste water.
Another object of this invention is to provide an apparatus in -~
which efficient separation of suspended solids from the effluent is achieved inside the reactor so that a separate clarifier and the associated sludge return pumping is not required.
A~other object of this lnvention is to provide an apparatus capable of reliable and unattended operation when processing waste waters on ships under condition of ship motion and vib-ration.
Another object of the invention is to provide an improved suspended solids separator that would not be affected by "sloshing" that normally occurs on ships during heavy roll and pitch conditions.
1090~t88 Another object of this invention is to provide an apparatus that would require only once per year replenishment of the used chemicals and only once per year withdrawal of the excess sludge when serving single family or multiple damily dwellings.
It is also an object of this invention to provide an apparatus capable of reliable and unattended operation when operating with wood particles such as saw dust, powdered minerals, powdered activated carbon, powdered charcoal or their mixtures in reaction chambers.
Another object of the invention is to provide an apparatus that would be easy to scale up or down to use as standardized waste water renovation system to serve small communities, camps, air-ports, commercial developments, recreation centers, parks and industrial plants either as a permanent or temporary install-ations.
Other objects and features of the invention will be set orth ; fully hereinafter.
The full nature of the invention will be understood from the accompanying drawing and the following description of claims.
SUMMARY OF THE INVENTION - ~-The present invention provldes an apparatus permitting the ~ .
various biological, chemical and physical processes required to : .
remove the various pollutants from raw sanitary waste water to be carried out within a single tank.
The tank is divided by partitions into three bio-reaction chambers and two chemical reaction chambers and in a preferred embodiment the tank is made of steel and equipped with manways permitting entrance into each individual chamber.
The tank may be located below or above the ground when serving single or multiple family dwellings or installed on ships as a marine.sanitation deviae.
The first bio-reaction chamber contains a suspension of pro-cessed waste water,nonbiodegradable suspended solids and mixed microbial population, the suspension being recirculated within ~0904~8 the first reaction chamber by a mechanical mixer without addition of oxygen.
The second bio-reaction chamber contains a suspension of partially processed waste water, non-biodegraaable suspended solids and mixed microbial population, the-suspension being recirculated in this chamber by a mechanical mixer which sim-ultaneously injects into the suspension atmospheric air to keep the liquid in this chamber saturated with oxygen.
The third bio-reaction chamber contains a submerged multi-channel suspended solids separator and the suspension contain- -ing purified waste water, nonbioaegradable suspended solids and mixed microbial population in this chamber is recirculated over and under the multichannel suspended solids separator to maintain the suspended solids in suspension and to enhance flocculation. The recirculation of the suspension in this chamber is by mechanical mixer without addition of oxygen.
The fourth reaction chamber is a chemical oxidation-clarification chamber and contains a submerged multichannel chemical reactor ~; ~ to prevent shortcutting of the chemically treated effluent with-in the fourth reaction chamber, to provide the required contact time for chemical oxidation of the residual organics and/or toxic chemicals, to provide the required contact time for effic-ient kill of bacteria and viruses and to simultaneously separate ` ~
the formed precipitate and the residual suspended solids from `~ 25 ~the chemically purified effluent.
The fifth reaction chamber is for~ final polishing of the purif-ied waste water and contains charcoal or activated carbon to de-compose the residual oxidizing agents and to render the effluent ~ nontoxic to aquatic life and suitable for reuse.
-~ 30 The dosage of the various chemical agents is by disolution o~
granulated chemicals into the recirculated liquor, the level of which is rising in bioreaction chambers when the waste water is fed into the system and then slowly falling to normal operating level when there is no flow of the incoming waste water.
--` 1090~88 BRIEF DESCRIPTION OF DRAWING:
Fig. 1 is an overall view through a preferred embodiment of the apparatus of the present invention.
DETAILED DESCRIPTION OF THE APPARATUS
A cut away perspective view of the complete apparatus of the present invention is shown in Fig. 1. The apparatus comprises of first bio-reaction chamber 100 formed by partition 112 and the outside walls and the floor of the tank 10 and equipped with ~-a submerged mechanical mixer 117 and containing a suspension of purified waste water, non-biogradable suspended solids and mixed microbial population 103; the second bio-reaction chamber 200 formed by partitions 112, 212 and 412 and one outside wall and floor of the tank 10 and equipped with a submerged mechanical mixer with an air injector 217 and containing a suspension of purified waste water, non-biodegradable suspended solids and mized microbial population; the third bio-reaction chamber 300 --formed by partitions 112, 212 and 412 and the second outside wall and floor of the tank 10 and equipped with a submerged mechanical mixer 317 and~a submerged multichannel suspended ~ solids separ~ator 310; the flow equalizer 402; a chemical oxid-izing agent storage-dispensing chamber 410; a mineral storage-dispen~sing container 101; an organic material storage-dispensing~
container 201; chemical oxidation-clarification chamber 400 formed by partitions 412 and 413 and the side walls and floor of the tank 10 and equipped with a submerged multichannel reactor 415; and polishing chamber 420 containing charcoal or activated carbon formed by partitions 412, 413 and the side walls and floor of the tank 10.
Referring to the system's hydraulics, at periods of zero flow :
of the incoming waste water the height of the suspension in the first 100, second 200 and third 300 bio-reaction chambers is at 103, 203 and 303 levels with the suspension containing waste water non-biodegradable suspended solids and mixed microbial population being continuously recirculated within the three bio-reaction chambers by submerged mechanical mixers 117, 217 and 317 1090~38 100 and 300 and with injection of the atmospheric air into the suspension in chamber 200, the suspension being also con-tinuously circulated from the third ~ioreaction chamber via channel 340 located in partition 112 into the first bioreaction S chamber 100, from first bioreaction chamber 100 via a screened opening 115 in partition 112 into the second bioreaction chamber 200 and from second bioreaction chamber 200 via restricted open-ing 205 in parti~ion 212 back into third bioreaction chamber 300.
Under conditions of zero flow of the incoming waste water the mineral storage dispensing container 101 located in second bio-reaction chamber 200 and the organic material storage dispensing container 201 located in third bioreaction chamber 300 are just above the liquid levels 203, 303, the mineral and the organic material not being in contact with the rerirculated suspension maintained in bioreaction chambers 200 and 300 and therefore not being dissolved into the recirculated liquid. As the waste water enters via opening 104 into first bioreaction chamber 100 the liquid level in first, second and third bioreaction chambers rises, the increase in the height of the recirculated suspension being proportional to the difference between the flow of incoming : waste water and the flow of the clarified waste water from theflow equalizer 402. The higher the flow rate of the incoming waste water, the higher is the liquid level in the three bio-reaction chambers and consequently more of the mineral and the organic material is submerged into the recirculated suspension ~ -and dissolved.
As the incoming waste water is mixed in the first bioreaction chamber 100 with the suspension containing purified waste water, non-biodegradable suspended solids and mixed microbial populat-ion, the activity of the mixed microbial population rises and the nitrite and/or nitrate present in the suspension are removed by respiration of the mixed microbial population. At the same time, portion of the organic matter from the waste water is bio-ozidized, portion of organic matter is adsorbed on the non bio-degradable suspended soilds and the nitrogenous compounds trans-~90~38 formed to ammonia. The suspension containing partially purified waste water, suspended solids and mixed microbial population then flows from the first bioreaction chamber 100 via screened opening 115 located in partition 112 into second bioreaction chamber 200 to be mixed with diffused air supplied by mechanical mixer 217, mixed microbial population, non bio-degradable suspended solids and mineral dissolved into the re-circulated suspension to precipitate phosphates. Enough contact time is provided in second bioreaction chamber 200 to completely bio-oxidize the dissolved bio-degradable organic matter and to transform the an~nonia present in the waste water to nitrite and/
- or nitrate and a portion of nitrite and/or nitrate to nitrogenous gas and to precipitate phosphates.
The suspension containing the treated waste water, the ramaining nitrite ana/or nitrate, suspended solids and mixed microbial population is then flown from second bioreaction chamber 200 through restricted opening 205 located in partition 212 into third bioreaction chamber 300 to be mixed with the suspension present in bioreaction chamber 300 and containing nondegradable suspended solids, mixed microbial population and zero dissolved oxygen ln the liquid, the suspension being continuously recir-culated by a submerged mechanical mixer 317. The activity of the mixed microbial population in third bioreaction chamber 300 ;
is~ maintained by suspended organic matter and by soluble organic ;~ 25 matter adsorbed on non-biodegradable suspended solids present in this chamber and by ~the added soluble organix material and by the nitrite and/or nitrate entering into bioreaction chamber 300 from bioreaction chamber 200. Due to the activity of the mixed micro-`~ bial population present in third bioreaction chamber 300 in the absence of dissolved oxygen, the remaining dissolved bio degrad-able organic matter is bio-oxidized with the nitrite and/or nitrate being transformed by the respiration of the mixed microbia;
population to nitrogen gas. The mixture of purified waste water _ 9 _ 1090'1~8 , and suspended solids then enters into the submerged multi-channel suspended solids separator 310 via openings 320 located at the lower end of the separator 310, then flows upward in channels 321 in direction of arrows 309, then into a centrally located collection line 323-and out of bioreaction chamber 300 into flow equalizer 402 located in chamber 410. On the way up in channels 321 suspended solids are settled out on the walls of the inclined channels, then continuously slid down into the recirculated liquor.
----- - The separated suspended solids are circulated in the third bioreaction chamber downwardly in the space formed between partition 112 and the wall of the suspended solids separator 310 and upwardly in the space formed between partition 412 and the other wall of the suspended solids separator 310. Portion of the separated suspended solids is continuously recycled into bio-reaction chamber 100 via channel 340 located in partition 112.
The flow equalizer 402 located in the chemical oxidizing agent dispensing chamber 410 consists of a vertical pipe with a narrow opening 403. The flow equalizer maintains the flow of the processed waste water through the three bioreaction chambers and through the suspended solids separator within the designedrange by means of the opening 403 and relatively independent of the flow of the incoming waste water. At a surge flow of the incoming waste water, the flow equalizer causes to rise the liquid level in bioreaction chambers 100, 200 and 300 to a level which is limited only by the height of equalizer pipe 402, accumulating the surge of the waste water in bioreaction cham- -bers and then slowly at relatively constant rate, releasing the p~ocessed waste water through the submerged suspended solids separator via opening 403 into chemical oxidizing agent dispen-sing chamber 410. In this way, the detrimental effects of the surge of the incoming waste water on the involved biological processes and on the separation of suspended solids is eliminated. `
The clarified effluent containing the residual refractory organ-ics, bacteria and viruses and residual suspended solids, over-flows from opening 403 of the flow equalizer 402 into the chcm-ical ozidizing agent dispensing chamber 410. To flow out from chamber 410, the effluent must pass through a narrow opellin-~ ~l4 :1090~38 .
in one wall of chamber 410 which controls the flowrate out of ch~mber 410 into the chemical o~idation -clarification chamber 400. At the varying flow of the effluent from the flow equal-izer 402, the level of the liquid in chamber 410 rises and varies within the height of the opening 414. A mixture of gran-ulated chemical oxidizing agents is stored in perforated cont-ainer 430 located in chamber 410 with the container's bottom touching the level of the li~uid in the chamber 410 at zero flow of the effluent through flow equalizer 402. The liquid level in chamber 410 rises proportionally to the flow rate of the effluent fxom this chamber submerging the perforated container 430 contalning chemical oxidizing agents into the liquid and dissolving the oxidizing agents into the effluent through chamber 410. Thus the amount of chemical oxidizing agents dissolved into a unit volume of the effluent~in the apparatus of this invention is constant and is controlled by the dimensions of the opening 414.
The effluent containing~dissolYed chemical oxidi~zing agents ; then flows into the lower portion;of the chemical oxi~dation ~ - clarification chamber 400 and via opening 425 into~a~sub-merged~multlchannel reactor 410.~ The multichannel reactor prevents short-cutting of the chemically~pxidized effluent within the chemical oxidation-clar~ificatlon chamber thus pro-viding~condltions~for efficient oxidation of the residual mpurlties, efficient kill of bacteria and viruses and si~mul-taneously also efficient removal~f the formed precipitate and residual suspended sollds entrained from the third bioreaction chamber. In~channels 421 the chemically oxidized effluent flows upwardly into a centrally located collection line 422 and , .
then out of chamber 400 into chamber 420 for final purification and decomposition of the remaining oxidizing agents. In chamber 420 the purified effluent flows by gravity through a bed of char-coal, then via opening 423 and pipe 424 out of the apparatus for surface disposal or for reuse.
~090~88 While the described apparatus is particularly useful for stand-ardized single or multiple family waste water renovation units, or as a marine sanitation device, it has application to sewage treatment systems and sewage renovation systems of various sizes. It is particularly useful as a standardized package plant for use on l,and or off-shore in various permanent or temporary installations.
While the apparatus of the present invention has been described for use with steel, it is obvious that the apparatus may be constructed of any convenient material such as reinforced con-crete or fiber glass.
Although the present invention has been described in part with reference to specific example, modifications may be constructed or used without departing from the scope of the invention which ; 20 is defined in the following claims.
, ,
"Apparatus for On-site Renovation of Sanitary Waters"
S P E C I F I C A T I O N
This invention relates to an apparatus for on-site renovation of sanitary waters and has for it's object a provision of an improved apparatus capable of unattended an reliable operation when purifying sanitary waters to a high quality effluent suitable for limited reuse.
'~' -.
",.~: :. ~
1~90~8~
BACKGROUND TO THE INVENTION
It has become evident that nitrogen and phosphorus affect the productivity of aquatic life - nitrogen being the limiting nut-rient in eutrophic waters and phosphorus in oligotrophic waters.
It is also known that domestic waste waters contain from 10 to 100 times the nutrient concentration of agricultural or forest drainage. COnsequently in densely populated areas overfertil-ization of surface waters, algae growth and chemical pollution have been noticed along with degradation of potable water sources and the need for more efficient removal of all pollutants from waste waters has become more obvious.
While removal of phosphorus can be achieved reliably by chemical precipitation and removal of organics by biological followed by physical-chemical processes, removal of nitrogen is more comp-licated.
The biological transformations of nitrogenous compounds occur through biological processes of ammonification, nitrification and denitrification. The first two require presence of oxygen, the denitrification require absence of oxygen. The two distinct mechanisms responsible for removal of nitrogen and reduction of nitrite and nitrate are (a) - formation of ammonia followed by transfer of ammonia into the anabolic cell metabolism which is of minor importance since C:N ratio in cell tissue is 5 - 6, whereas in domestic wasteiwaters only 2 to 2.5 and (b) -microbial denitrification, which is a respiratory reduction in which nitrite and nitrate replace oxygen as the final electron acceptors in the respiration chain.
Bio-oxidation of organic matter, ammonification and nitrification cause no problem. Nitrification is efficient and reliable if organic loadings are maintained below 0.3 lb BOD per lb of mixed liquor suspended solids per day, sludge age is maintained above 3 -4 days and dissolved oxygen in the mixed liquor is maintained above 1.0 - 2.0 mg/lit. The higher is the concent-ration of mixed liquor suspended solids, the more efficient is ~090~
the transformation of ammonia to nitrite and nitrate. The overall rate of denitrification is a function of the concent-ration of the heterotrophic facultative bacteria present in mixed liquor suspended solids and their activity in the absence of oxygen. To maintain the activity the denitrifying bacteria must be supplied with suitable organic material - source of energy.
From the process point of view to accommodate the different food and oxygen requirements of bio-oxidation of organic matter, ammonification and nitrification of nitrogenous compounds and decomposition of nitrite and nitrate by microbial respiration and to achieve acceptable reaction rates and efficiencies, the various biochemical reactions are currently being carried out in separate process stages. While the conventional activated sludge process is capable of removing nitrogen with efficiency of 50 -60 per cent, the current multistage processes can achieve the removal of nitrogen with efficiency of up to 80 -90 per cent.
The multistage processes currently in use in large municipal treatment plants require treatment facilities that are too com-plex to be scaled down to small package pla~ts to serve small developments or single family dwellings. Because of the number of process steps required for removal of the various pollutants renovation and reuse of domestic waste waters at present seems feasible only if practiced on a large scale.
A large waste water treatment -renovation plant however requires ~ .
large underground sewage collection -transportation network, and in case the renovated water is to be reused also a large under-ground water distribution networ~. Such networ~s are expensive to build and even more expensive to maintain and to operate.
It is therefore obvious that on-site renovation and reuse of waste water would be economically more attractive than renovat-ion and reuse of waste waters via central collection-treatment distribution. However because of the complexity of the involved treatment on-site renovation and reuse of domestic waste waters as yet can't be practiced.
1090"~
Although at present small package sewage treatment plants are available, they do not provide the required degree of purific-ation that would permit reuse of the purified effluent and in general they also lack the required mechanical reliability.
It is therefore the prime object of this invention to provide an apparatus in which the various processes to remove all poll-utants present in sanitary waters could be carried out reliably, unattended and at acceptable cost when serving.single or multiple family dwellings.
More particularly it is the object of this invention to provide an apparatus that would reliably maintain all conditions required for efficient bio-oxidation of organic mat`ter, biological nitrif-ication, biological denitrification, chemical precipitation of soluble phosphates, chemical oxidation of the residual and ref-ractory organics and toxic compounds, efficient kill of bacteria and viruses and efficient removal of the residual chemical oxid-izing agents so as to render the effluent non-toxic to aquatic life and suitable for reuse.
Another object of this invention is to provide an inexpensive and reliable method for storing and proportioning of the various chemicals to the unsteady or batchwise flow of the incoming waste water.
Another object of this invention is to provide an apparatus in -~
which efficient separation of suspended solids from the effluent is achieved inside the reactor so that a separate clarifier and the associated sludge return pumping is not required.
A~other object of this lnvention is to provide an apparatus capable of reliable and unattended operation when processing waste waters on ships under condition of ship motion and vib-ration.
Another object of the invention is to provide an improved suspended solids separator that would not be affected by "sloshing" that normally occurs on ships during heavy roll and pitch conditions.
1090~t88 Another object of this invention is to provide an apparatus that would require only once per year replenishment of the used chemicals and only once per year withdrawal of the excess sludge when serving single family or multiple damily dwellings.
It is also an object of this invention to provide an apparatus capable of reliable and unattended operation when operating with wood particles such as saw dust, powdered minerals, powdered activated carbon, powdered charcoal or their mixtures in reaction chambers.
Another object of the invention is to provide an apparatus that would be easy to scale up or down to use as standardized waste water renovation system to serve small communities, camps, air-ports, commercial developments, recreation centers, parks and industrial plants either as a permanent or temporary install-ations.
Other objects and features of the invention will be set orth ; fully hereinafter.
The full nature of the invention will be understood from the accompanying drawing and the following description of claims.
SUMMARY OF THE INVENTION - ~-The present invention provldes an apparatus permitting the ~ .
various biological, chemical and physical processes required to : .
remove the various pollutants from raw sanitary waste water to be carried out within a single tank.
The tank is divided by partitions into three bio-reaction chambers and two chemical reaction chambers and in a preferred embodiment the tank is made of steel and equipped with manways permitting entrance into each individual chamber.
The tank may be located below or above the ground when serving single or multiple family dwellings or installed on ships as a marine.sanitation deviae.
The first bio-reaction chamber contains a suspension of pro-cessed waste water,nonbiodegradable suspended solids and mixed microbial population, the suspension being recirculated within ~0904~8 the first reaction chamber by a mechanical mixer without addition of oxygen.
The second bio-reaction chamber contains a suspension of partially processed waste water, non-biodegraaable suspended solids and mixed microbial population, the-suspension being recirculated in this chamber by a mechanical mixer which sim-ultaneously injects into the suspension atmospheric air to keep the liquid in this chamber saturated with oxygen.
The third bio-reaction chamber contains a submerged multi-channel suspended solids separator and the suspension contain- -ing purified waste water, nonbioaegradable suspended solids and mixed microbial population in this chamber is recirculated over and under the multichannel suspended solids separator to maintain the suspended solids in suspension and to enhance flocculation. The recirculation of the suspension in this chamber is by mechanical mixer without addition of oxygen.
The fourth reaction chamber is a chemical oxidation-clarification chamber and contains a submerged multichannel chemical reactor ~; ~ to prevent shortcutting of the chemically treated effluent with-in the fourth reaction chamber, to provide the required contact time for chemical oxidation of the residual organics and/or toxic chemicals, to provide the required contact time for effic-ient kill of bacteria and viruses and to simultaneously separate ` ~
the formed precipitate and the residual suspended solids from `~ 25 ~the chemically purified effluent.
The fifth reaction chamber is for~ final polishing of the purif-ied waste water and contains charcoal or activated carbon to de-compose the residual oxidizing agents and to render the effluent ~ nontoxic to aquatic life and suitable for reuse.
-~ 30 The dosage of the various chemical agents is by disolution o~
granulated chemicals into the recirculated liquor, the level of which is rising in bioreaction chambers when the waste water is fed into the system and then slowly falling to normal operating level when there is no flow of the incoming waste water.
--` 1090~88 BRIEF DESCRIPTION OF DRAWING:
Fig. 1 is an overall view through a preferred embodiment of the apparatus of the present invention.
DETAILED DESCRIPTION OF THE APPARATUS
A cut away perspective view of the complete apparatus of the present invention is shown in Fig. 1. The apparatus comprises of first bio-reaction chamber 100 formed by partition 112 and the outside walls and the floor of the tank 10 and equipped with ~-a submerged mechanical mixer 117 and containing a suspension of purified waste water, non-biogradable suspended solids and mixed microbial population 103; the second bio-reaction chamber 200 formed by partitions 112, 212 and 412 and one outside wall and floor of the tank 10 and equipped with a submerged mechanical mixer with an air injector 217 and containing a suspension of purified waste water, non-biodegradable suspended solids and mized microbial population; the third bio-reaction chamber 300 --formed by partitions 112, 212 and 412 and the second outside wall and floor of the tank 10 and equipped with a submerged mechanical mixer 317 and~a submerged multichannel suspended ~ solids separ~ator 310; the flow equalizer 402; a chemical oxid-izing agent storage-dispensing chamber 410; a mineral storage-dispen~sing container 101; an organic material storage-dispensing~
container 201; chemical oxidation-clarification chamber 400 formed by partitions 412 and 413 and the side walls and floor of the tank 10 and equipped with a submerged multichannel reactor 415; and polishing chamber 420 containing charcoal or activated carbon formed by partitions 412, 413 and the side walls and floor of the tank 10.
Referring to the system's hydraulics, at periods of zero flow :
of the incoming waste water the height of the suspension in the first 100, second 200 and third 300 bio-reaction chambers is at 103, 203 and 303 levels with the suspension containing waste water non-biodegradable suspended solids and mixed microbial population being continuously recirculated within the three bio-reaction chambers by submerged mechanical mixers 117, 217 and 317 1090~38 100 and 300 and with injection of the atmospheric air into the suspension in chamber 200, the suspension being also con-tinuously circulated from the third ~ioreaction chamber via channel 340 located in partition 112 into the first bioreaction S chamber 100, from first bioreaction chamber 100 via a screened opening 115 in partition 112 into the second bioreaction chamber 200 and from second bioreaction chamber 200 via restricted open-ing 205 in parti~ion 212 back into third bioreaction chamber 300.
Under conditions of zero flow of the incoming waste water the mineral storage dispensing container 101 located in second bio-reaction chamber 200 and the organic material storage dispensing container 201 located in third bioreaction chamber 300 are just above the liquid levels 203, 303, the mineral and the organic material not being in contact with the rerirculated suspension maintained in bioreaction chambers 200 and 300 and therefore not being dissolved into the recirculated liquid. As the waste water enters via opening 104 into first bioreaction chamber 100 the liquid level in first, second and third bioreaction chambers rises, the increase in the height of the recirculated suspension being proportional to the difference between the flow of incoming : waste water and the flow of the clarified waste water from theflow equalizer 402. The higher the flow rate of the incoming waste water, the higher is the liquid level in the three bio-reaction chambers and consequently more of the mineral and the organic material is submerged into the recirculated suspension ~ -and dissolved.
As the incoming waste water is mixed in the first bioreaction chamber 100 with the suspension containing purified waste water, non-biodegradable suspended solids and mixed microbial populat-ion, the activity of the mixed microbial population rises and the nitrite and/or nitrate present in the suspension are removed by respiration of the mixed microbial population. At the same time, portion of the organic matter from the waste water is bio-ozidized, portion of organic matter is adsorbed on the non bio-degradable suspended soilds and the nitrogenous compounds trans-~90~38 formed to ammonia. The suspension containing partially purified waste water, suspended solids and mixed microbial population then flows from the first bioreaction chamber 100 via screened opening 115 located in partition 112 into second bioreaction chamber 200 to be mixed with diffused air supplied by mechanical mixer 217, mixed microbial population, non bio-degradable suspended solids and mineral dissolved into the re-circulated suspension to precipitate phosphates. Enough contact time is provided in second bioreaction chamber 200 to completely bio-oxidize the dissolved bio-degradable organic matter and to transform the an~nonia present in the waste water to nitrite and/
- or nitrate and a portion of nitrite and/or nitrate to nitrogenous gas and to precipitate phosphates.
The suspension containing the treated waste water, the ramaining nitrite ana/or nitrate, suspended solids and mixed microbial population is then flown from second bioreaction chamber 200 through restricted opening 205 located in partition 212 into third bioreaction chamber 300 to be mixed with the suspension present in bioreaction chamber 300 and containing nondegradable suspended solids, mixed microbial population and zero dissolved oxygen ln the liquid, the suspension being continuously recir-culated by a submerged mechanical mixer 317. The activity of the mixed microbial population in third bioreaction chamber 300 ;
is~ maintained by suspended organic matter and by soluble organic ;~ 25 matter adsorbed on non-biodegradable suspended solids present in this chamber and by ~the added soluble organix material and by the nitrite and/or nitrate entering into bioreaction chamber 300 from bioreaction chamber 200. Due to the activity of the mixed micro-`~ bial population present in third bioreaction chamber 300 in the absence of dissolved oxygen, the remaining dissolved bio degrad-able organic matter is bio-oxidized with the nitrite and/or nitrate being transformed by the respiration of the mixed microbia;
population to nitrogen gas. The mixture of purified waste water _ 9 _ 1090'1~8 , and suspended solids then enters into the submerged multi-channel suspended solids separator 310 via openings 320 located at the lower end of the separator 310, then flows upward in channels 321 in direction of arrows 309, then into a centrally located collection line 323-and out of bioreaction chamber 300 into flow equalizer 402 located in chamber 410. On the way up in channels 321 suspended solids are settled out on the walls of the inclined channels, then continuously slid down into the recirculated liquor.
----- - The separated suspended solids are circulated in the third bioreaction chamber downwardly in the space formed between partition 112 and the wall of the suspended solids separator 310 and upwardly in the space formed between partition 412 and the other wall of the suspended solids separator 310. Portion of the separated suspended solids is continuously recycled into bio-reaction chamber 100 via channel 340 located in partition 112.
The flow equalizer 402 located in the chemical oxidizing agent dispensing chamber 410 consists of a vertical pipe with a narrow opening 403. The flow equalizer maintains the flow of the processed waste water through the three bioreaction chambers and through the suspended solids separator within the designedrange by means of the opening 403 and relatively independent of the flow of the incoming waste water. At a surge flow of the incoming waste water, the flow equalizer causes to rise the liquid level in bioreaction chambers 100, 200 and 300 to a level which is limited only by the height of equalizer pipe 402, accumulating the surge of the waste water in bioreaction cham- -bers and then slowly at relatively constant rate, releasing the p~ocessed waste water through the submerged suspended solids separator via opening 403 into chemical oxidizing agent dispen-sing chamber 410. In this way, the detrimental effects of the surge of the incoming waste water on the involved biological processes and on the separation of suspended solids is eliminated. `
The clarified effluent containing the residual refractory organ-ics, bacteria and viruses and residual suspended solids, over-flows from opening 403 of the flow equalizer 402 into the chcm-ical ozidizing agent dispensing chamber 410. To flow out from chamber 410, the effluent must pass through a narrow opellin-~ ~l4 :1090~38 .
in one wall of chamber 410 which controls the flowrate out of ch~mber 410 into the chemical o~idation -clarification chamber 400. At the varying flow of the effluent from the flow equal-izer 402, the level of the liquid in chamber 410 rises and varies within the height of the opening 414. A mixture of gran-ulated chemical oxidizing agents is stored in perforated cont-ainer 430 located in chamber 410 with the container's bottom touching the level of the li~uid in the chamber 410 at zero flow of the effluent through flow equalizer 402. The liquid level in chamber 410 rises proportionally to the flow rate of the effluent fxom this chamber submerging the perforated container 430 contalning chemical oxidizing agents into the liquid and dissolving the oxidizing agents into the effluent through chamber 410. Thus the amount of chemical oxidizing agents dissolved into a unit volume of the effluent~in the apparatus of this invention is constant and is controlled by the dimensions of the opening 414.
The effluent containing~dissolYed chemical oxidi~zing agents ; then flows into the lower portion;of the chemical oxi~dation ~ - clarification chamber 400 and via opening 425 into~a~sub-merged~multlchannel reactor 410.~ The multichannel reactor prevents short-cutting of the chemically~pxidized effluent within the chemical oxidation-clar~ificatlon chamber thus pro-viding~condltions~for efficient oxidation of the residual mpurlties, efficient kill of bacteria and viruses and si~mul-taneously also efficient removal~f the formed precipitate and residual suspended sollds entrained from the third bioreaction chamber. In~channels 421 the chemically oxidized effluent flows upwardly into a centrally located collection line 422 and , .
then out of chamber 400 into chamber 420 for final purification and decomposition of the remaining oxidizing agents. In chamber 420 the purified effluent flows by gravity through a bed of char-coal, then via opening 423 and pipe 424 out of the apparatus for surface disposal or for reuse.
~090~88 While the described apparatus is particularly useful for stand-ardized single or multiple family waste water renovation units, or as a marine sanitation device, it has application to sewage treatment systems and sewage renovation systems of various sizes. It is particularly useful as a standardized package plant for use on l,and or off-shore in various permanent or temporary installations.
While the apparatus of the present invention has been described for use with steel, it is obvious that the apparatus may be constructed of any convenient material such as reinforced con-crete or fiber glass.
Although the present invention has been described in part with reference to specific example, modifications may be constructed or used without departing from the scope of the invention which ; 20 is defined in the following claims.
, ,
Claims (6)
1. A self-contained apparatus for renovation of sanitary waters comprising:
(a) a closed waste water storage - reaction tank provided with manways and a vent, (b) three or more bioreaction chambers within said reaction tank formed by the tank walls, cover and common partitions respectively, between the first, second and third bio-reaction chambers, said common partitions each having upper ends extending above the liquid level in bioreaction chambers and lower ends extending to the reaction tank floor, said bioreaction chambers equipped with submerged mechanical mixers for recirculating and mixing the non bio-degradable suspended solids and mixed microbial population with the processed waste water in each bioreaction chamber, said submerged mechanical mixers having the capability to inject or not to inject the atmospheric air into the re-circulated suspension to maintain the desired process con-ditions within each bioreaction chamber, (c) restricted opening in partitions between bioreaction chambers for flowing the suspension containing non bio-degradable suspensded solids, mixed microbial population and the processed waste water from chamber to chamber in the direction from first bioreaction chamber to the third bioreaction chamber and a restricted opening for flowing the suspension from third bioreaction chamber into first bioreaction chamber distributing the suspended solids and the mixed microbial population evenly through the three bioreaction chambers, (d) a submerged multichannel suspended solid separator located in the third bioreaction chamber for separation of the solids-liquid mixture into purified liquid and sludge, said sludge being retained in the three bioreaction chambers and the purified liquid flown out of the third bioreaction chamber, (e) a flow rate equalizer to control the flow of the waste water through the three bioreaction chambers and to control the flow of the purified waste water through the submerged multichannel suspended solids separator.
(a) a closed waste water storage - reaction tank provided with manways and a vent, (b) three or more bioreaction chambers within said reaction tank formed by the tank walls, cover and common partitions respectively, between the first, second and third bio-reaction chambers, said common partitions each having upper ends extending above the liquid level in bioreaction chambers and lower ends extending to the reaction tank floor, said bioreaction chambers equipped with submerged mechanical mixers for recirculating and mixing the non bio-degradable suspended solids and mixed microbial population with the processed waste water in each bioreaction chamber, said submerged mechanical mixers having the capability to inject or not to inject the atmospheric air into the re-circulated suspension to maintain the desired process con-ditions within each bioreaction chamber, (c) restricted opening in partitions between bioreaction chambers for flowing the suspension containing non bio-degradable suspensded solids, mixed microbial population and the processed waste water from chamber to chamber in the direction from first bioreaction chamber to the third bioreaction chamber and a restricted opening for flowing the suspension from third bioreaction chamber into first bioreaction chamber distributing the suspended solids and the mixed microbial population evenly through the three bioreaction chambers, (d) a submerged multichannel suspended solid separator located in the third bioreaction chamber for separation of the solids-liquid mixture into purified liquid and sludge, said sludge being retained in the three bioreaction chambers and the purified liquid flown out of the third bioreaction chamber, (e) a flow rate equalizer to control the flow of the waste water through the three bioreaction chambers and to control the flow of the purified waste water through the submerged multichannel suspended solids separator.
2. Apparatus according to claim 1 and comprising in addition:
(f) a container with perforated bottom for storing and dissol-ving chemical oxidizing agents into the effluent flowing out from the third bioreaction chamber, (g) a chemical oxidizing agent dissolving chamber equipped with restricted opening causing to rise the level of the liquid in the chemical oxidizing agents dissolving chamber in pro-portion to the flow rate of the liquid flowing through said chemical oxidizing agents dissolving chamber, (h) a chemical oxidation-clarification chamber formed by the tank walls, cover and common partitions between the chemical oxidation-clarification chamber and the second and third bioreaction chambers, said chemical oxidation-clarification chamber having sufficient reaction volume to provide the required contact time to chemically oxidize the residual pollutants and to efficiently disinfect the purified waste water
(f) a container with perforated bottom for storing and dissol-ving chemical oxidizing agents into the effluent flowing out from the third bioreaction chamber, (g) a chemical oxidizing agent dissolving chamber equipped with restricted opening causing to rise the level of the liquid in the chemical oxidizing agents dissolving chamber in pro-portion to the flow rate of the liquid flowing through said chemical oxidizing agents dissolving chamber, (h) a chemical oxidation-clarification chamber formed by the tank walls, cover and common partitions between the chemical oxidation-clarification chamber and the second and third bioreaction chambers, said chemical oxidation-clarification chamber having sufficient reaction volume to provide the required contact time to chemically oxidize the residual pollutants and to efficiently disinfect the purified waste water
3. An apparatus according to Claim 2 and comprising in addition:
(i) a submerged multichannel reactor located in the chemical oxidation-clarification chamber, said submerged multi-channel reactor preventing short-cutting of the chemically treated effluent within the chemical oxidation-clarification chamber and said submerged multichannel reactor permitting simultaneously efficient separation of the formed precip-itate and the residual suspended solids entrained from the third bioreaction chamber and said multichannel reactor permitting retention of the separated suspended solids in the chemical oxidation-clarification chamber.
(i) a submerged multichannel reactor located in the chemical oxidation-clarification chamber, said submerged multi-channel reactor preventing short-cutting of the chemically treated effluent within the chemical oxidation-clarification chamber and said submerged multichannel reactor permitting simultaneously efficient separation of the formed precip-itate and the residual suspended solids entrained from the third bioreaction chamber and said multichannel reactor permitting retention of the separated suspended solids in the chemical oxidation-clarification chamber.
4. An apparatus according to Claim 3 and comprising in addition:
(j) a mineral storage - dispensing container located in one or more bioreaction chambers, said mineral storage-dispensing container having a perforated bottom located above the lowest level of the liquid in the bioreaction chambers at zero flow of the incoming waste water, said mineral storage-dispensing container being partially submerged into the re-circulated liquid during the flow of the incoming waste water to dissolve the mineral into the recirculated liquid in proportion to the incoming waste water.
(j) a mineral storage - dispensing container located in one or more bioreaction chambers, said mineral storage-dispensing container having a perforated bottom located above the lowest level of the liquid in the bioreaction chambers at zero flow of the incoming waste water, said mineral storage-dispensing container being partially submerged into the re-circulated liquid during the flow of the incoming waste water to dissolve the mineral into the recirculated liquid in proportion to the incoming waste water.
5. An apparatus according to Claim 4 and comprising in addition:
(k) an organic material storage-dispensing container located in third bioreaction chamber, said organic material storage-dispensing container having a perforated bottom located above the lowest level of the liquid in third bioreaction chamber at zero flow of the incoming waste water, said organic material storage-dispensing container being partially submerged into the recirculated liquid during the flow of the incoming waste water to dissolve the organic material into the recirculated liquor in proportion to the incoming waste water.
(k) an organic material storage-dispensing container located in third bioreaction chamber, said organic material storage-dispensing container having a perforated bottom located above the lowest level of the liquid in third bioreaction chamber at zero flow of the incoming waste water, said organic material storage-dispensing container being partially submerged into the recirculated liquid during the flow of the incoming waste water to dissolve the organic material into the recirculated liquor in proportion to the incoming waste water.
6. An apparatus according to Claim 5 and comprising in addition:
(l) a purification chamber formed by the tank walls, cover and common partition between the chemical oxidation-clarification chamber and said purification chamber and a common partition between the second bioreaction chamber and said purification chamber, said purification, chamber filled with charcoal or activated carbon, said chemically oxidized purified waste water being flown by gravity through the bed of charcoal in said purification chamber removing the residual chemical oxidizing agents from the purified waste water to render the purified waste water non-toxic to aquatic life and suitable for reuse or for surface discharge and disposal.
(l) a purification chamber formed by the tank walls, cover and common partition between the chemical oxidation-clarification chamber and said purification chamber and a common partition between the second bioreaction chamber and said purification chamber, said purification, chamber filled with charcoal or activated carbon, said chemically oxidized purified waste water being flown by gravity through the bed of charcoal in said purification chamber removing the residual chemical oxidizing agents from the purified waste water to render the purified waste water non-toxic to aquatic life and suitable for reuse or for surface discharge and disposal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA308,943A CA1090488A (en) | 1978-08-09 | 1978-08-09 | Apparatus for on-site renovation of sanitary waters |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA308,943A CA1090488A (en) | 1978-08-09 | 1978-08-09 | Apparatus for on-site renovation of sanitary waters |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1090488A true CA1090488A (en) | 1980-11-25 |
Family
ID=4112081
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA308,943A Expired CA1090488A (en) | 1978-08-09 | 1978-08-09 | Apparatus for on-site renovation of sanitary waters |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1090488A (en) |
-
1978
- 1978-08-09 CA CA308,943A patent/CA1090488A/en not_active Expired
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