[go: up one dir, main page]

WO2002083575A1 - Procede pour ajouter de l'eau salee a des compositions aqueuses avant ou pendant un traitement d'oxydation - Google Patents

Procede pour ajouter de l'eau salee a des compositions aqueuses avant ou pendant un traitement d'oxydation Download PDF

Info

Publication number
WO2002083575A1
WO2002083575A1 PCT/NO2002/000138 NO0200138W WO02083575A1 WO 2002083575 A1 WO2002083575 A1 WO 2002083575A1 NO 0200138 W NO0200138 W NO 0200138W WO 02083575 A1 WO02083575 A1 WO 02083575A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
ammonium
oxidation
addition
reactor
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.)
Ceased
Application number
PCT/NO2002/000138
Other languages
English (en)
Inventor
Eivind Lygren
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Puraq AS
Original Assignee
Puraq AS
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Puraq AS filed Critical Puraq AS
Publication of WO2002083575A1 publication Critical patent/WO2002083575A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/043—Treatment of partial or bypass streams
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/04—Disinfection
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment

Definitions

  • the present invention comprises a method for purification, and possibly disinfection, of a water containing composition containing ammonium. Further, the use of a water stream and an oxidant, possibly ozone gas, for oxidation of ammonium in a water containing composition, is described.
  • the present invention comprises a method for oxidation of ammonium to nitrate, comprising the addition to the water which is to be cleaned of a fraction of sea water or sea salt before or at the same time as an addition of ozone gas.
  • the water treatment will normally take place in a reactor with continuous through-flow, but can also take place in a reactor with batch operation.
  • Water, both sea water or sea salt and the water which is to be purified, can be fed to the reactor either by gravity or by the use of pumps. All of the known methods for transferring of gas to a liquid can be used for the addition of ozone.
  • the reactor can be open or closed.
  • Oxidation of ammonium by the addition of sea water or sea salt and ozone gas would be a unity process of interest for cleaning of municipal waste water, water in aquaculture plants, and industrial effluents containing ammonium.
  • Ammonium- nitrogen can have a number of unwanted effects bydischarge into water. It will be toxic to fish, even at very low concentrations.
  • Oxygen in the recipient will be consumed, by biological oxidation to nitrate (nitrification). It is a nutrient salt which can lead to excess fertilisation (eutrofication) in the recipient.
  • the present invention seeks to solve the problems caused by the presence of ammonium- nitrogen. After the oxidation from ammonium to nitrate the effect of nutrient salt will still be present, but the other two unwanted effects will be eliminated.
  • the oxidation of ammonium can be combined with other unity processes for the cleaning of water, so that produced nitrate is removed from the water by converting it to inert nitrogen gas.
  • Ozone gas is a well known disinfectant and oxidant. It is also known that nitrite (N0 2 " ) is rapidly oxidizing to nitrate (NO 3 " ) by the addition of ozone. However, oxidation of ammonium (NH + ) to nitrate by the addition of ozone is a process which normally proceeds very slowly, depending very strongly on the pH value and requireing high concentrations of ammonium (1 st order reaction). Consequently the oxidation of ammonium by the addition of ozone has until now not been competitive with biological processes (nitrification) for the oxidation of ammonium.
  • the present invention provides a method for purification, and possibly disinfection, of a water containing composition containing ammonium, where the oxidation of ammonium takes place by the addition of sea water, sea salt or brackish water before or at the same time as the addition of an amount of oxidant, possibly ozone gas, where the total water containing composition after the addition of water has a salinity of at least approximately 0.2 %o.
  • an oxidant possibly ozone gas
  • the actual invention consists of that the speed of reaction for oxidation of ammonium by the use of ozone, can be increased considerably by addition of some sea water or sea salt.
  • ions in the sea water or the sea salt evidently act as a catalyst, so that the oxidation only to a low degree is influenced by the pH value and of the concentration of ammonium (0 order reaction with regard to ammonium).
  • the utilization of the ozone gas was also increasing by the increase of salinity. With a salinity of 5 %o the mole ratio between the amount of supplied ozone gas and the amount of oxidized NH 4 -N was lower than 30 % of the equivalent mole ratio with fresh water.
  • sea water, sea salt or brackish water in the present invention are intended to mean water which has a salinity of at least approximately 0.2 %o, whether this salinity is achieved by the mixing of sea water and fresh water, or by the mixing of sea salt and fresh water.
  • Figure 1 shows the concentration as a function of time in a batch test with medium salinity.
  • Figure 2 shows reaction speed as a function of concentration of ammonium in the reactor.
  • Figure 3 shows concentrations of ammonium in a batch reactor as a function of time. Further, graphs for fresh water and for different mixtures of sea water and fresh water (different salinities) are shown.
  • Figures 4 to 7 show some examples of how a process for oxidation of ammonium by the addition of sea water or sea salt and ozone, can be adapted to other unity processes in novel or existing purification plants.
  • Figure 2 illustrates how oxidation speed of ammonium depends on the concentration of ammonium by the use of fresh water and mixtures of sea water and fresh water, respectively, with salinities from 1.05 to 7 % 0 .
  • Sea water in this context is intended to be atlantic sea water with a salinity of 35 %o. This means that a salinity of 7 % 0 in the oxidation reactor means that this contains 20 % sea water, whereas a salinity of 1.05 %o corresponds to 3 % sea water in the reactor.
  • Figure 3 shows how the ammonium concentration in a batch reactor decreases as a function of time.
  • sea water from 1.05 to 7 %o salinity
  • the graphs are straight lines to zero, whereas in a reactor with fresh water a curved line with gradual decrease in oxidation speed is obtained when the ammonium concentration is decreasing.
  • the transition range from 0 order reaction with regard to NH 4 -N, because of the presence of a part of sea water, to an approximately 1 st order reaction with regard to NH -N i fresh water, will depend on the salinity and concentration of ammonium in the reactor. At 0.2 %o salinity the transition will take place at about 1.2 to 1.3 mg NH 4 -N/I. At 1 %o salinity the transition will take place at about 9 mg NH -N/I.
  • Figures 4 to 7 show as previously mentioned a few examples of how a process for oxidation of ammonium by the addition of sea water or sea salt and ozone, can be adapted to other unity processes in novel or existing purification plants.
  • the number of possibilities of combinations are approximately infinite, and the optimum solution will depend on the composition of the water to be purified, the quality requirement for the cleaned water, and other local conditions.
  • Figure 4 shows an example of a novel or existing, conventional purification plant (1 ), with pretreatment, biological nitrification and separation of particles.
  • Some of such plants have gradually been imposed, or will be imposed, to very strong requirements as to effluents of ammonium.
  • Some plants have been imposed to a limitation of a maximum value per 24 hours or a maximum value per hour. This means that a biological cleaning stage for nitrification would have to be enlarged considerably to be able to handle the impact loads of ammonium.
  • high hourly loads normally occur a few hours out of the twenty-four, while irregular high 24 hour loads will occur a few times a year. This is particularly a problem where the aim is compact solutions, e.g. by biofilm processes.
  • the effluent from plants like this is close to zero ( ⁇ 0.1 mg/l) of ammonium in 18 to 22 hours out of the twenty-four, and typically 2 to 10 mg/l for the rest of the twenty-four hours period.
  • a unit (2) for oxidation of ammonium by addition of sea water or sea salt and ozone would be ideal for polishing the effluent from such a conventional plant (1 ).
  • sea water or sea salt and ozone can be added only in the periods where there is a need for additional removal of ammonium, and the added amounts can be controlled based on the oxidation speed which at any time is required in unit 2.
  • Figure 5 shows a purification plant which is almost equal to that which is previously shown in figure 4.
  • the conventional part (1 ) of the purification plant in figure 5 has a unit for biological pre-denitrification, so that most of the nitrate which is formed by biological nitrification can be removed.
  • the new unit (2) for oxidation of the water with ozone and sea water or sea salt will still be a polishing unit for removing any peaks of ammonium, which escape through the biological purification stage.
  • any nitrite produced in the biological stage will be oxidized to nitrate, and as long as ozone gas is measured out to the reactor the water will also be disinfected.
  • Figure 6 shows an example of a novel or existing purification plant (1), with pretreatment, addition of precipitation chemicals (koagulant and sea water or sea salt), and separation of particles.
  • precipitation chemicals koagulant and sea water or sea salt
  • a unit (2) for foam separation and a unit (3) for oxidation of ammonium by the addition of ozone are shown.
  • the waste gas from unit 3 will contain ozone, and this gas is feeded into the foam separation reactor (2), in order to have the most advantageous exploitation of ozone.
  • the addition of sea water or sea salt and ozone have been shown to have a very favourable effect for separating particles and organic material from water by means of a foam separation technique.
  • sea water or sea salt should be added so that a salinity of at least 3 %o is achieved. Consequently it can be necessary to add some sea water or sea salt to the foam separation reactor, in addition to the sea water or sea salt which is added in connection with the chemical flocculation step.
  • all of the ammonium has to be oxidized with ozone.
  • the unit (3) for oxidation of ammonium will need a reactor volume corresponding to a hydraulic time of residence of approximately 1 hour.
  • a plant as shown in figure 6 has the advantage of being completely without biological processes. The chemical processes kan be switched off and on. The plant reaches full efficiency after a few minutes, while the biological processes require waiting for the proper type and amount of bacteria to grow up during start-up and by great changes in the composition or amount of the waste waters.
  • Figure 7 shows an example of a purification plant with conventional pretreatment (1 ), a bio film reactor (2) for pre-denitrification of nitrate recirculated from the outlet, a foam separation reactor (3), and a reactor (4) for oxidation of ammonium by the addition of ozone.
  • the bacteria in the denitrifying biofilm reactor will consume the organic material in the incoming waste water, to be able to convert the recirculated nitrate to inert nitrogen gas.
  • Sea water or sea salt, air and ozone containing waste gas (from unit 4) have to be supplied to the foam separation reactor (3), while to the reactor (4) for oxidation of ammonium ozone has to be added.
  • Table 1 shows examples of reaction speeds, without and with the addition of sea water, respectively, and with two different concentrations of ozone i the water phase.
  • the reaction speed inceases nearly proportional with the concentration of sea water present in the reactor.
  • the oxidation speed of ammonium by the addition of ozone will be so high that a reactor with a hydraulic time of residence of 1-2 hours will be sufficient for treatment of municipal waste water.
  • An addition of sea water giving a reaction of 0 order with regard to ammonium also has the advantage that it is possible to reach low concentrations of ammonium, without having several reactors in series. This makes this process favourable in places with access to sea water. Places without sea water can achieve the same effect by the addition of sea salt.

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)

Abstract

Cette invention se rapporte à un procédé servant à épurer et, éventuellement, à désinfecter un mélange aqueux contenant de l'ammonium, l'oxydation de l'ammonium s'effectuant par addition d'eau préalablement ou simultanément à l'addition d'une quantité d'oxydant, éventuellement de l'ozone gazeux. Ainsi, le mélange aqueux total possède, après addition d'eau, une salinité d'au moins 0,2 ‰ environ. Cette invention décrit en outre l'utilisation d'un courant d'eau et d'un oxydant.
PCT/NO2002/000138 2001-04-11 2002-04-10 Procede pour ajouter de l'eau salee a des compositions aqueuses avant ou pendant un traitement d'oxydation Ceased WO2002083575A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO20011869A NO20011869L (no) 2001-04-11 2001-04-11 Separasjon av partikler og organisk materiale fra en vannholdig blanding
NO20011869 2001-04-11

Publications (1)

Publication Number Publication Date
WO2002083575A1 true WO2002083575A1 (fr) 2002-10-24

Family

ID=19912366

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/NO2002/000138 Ceased WO2002083575A1 (fr) 2001-04-11 2002-04-10 Procede pour ajouter de l'eau salee a des compositions aqueuses avant ou pendant un traitement d'oxydation

Country Status (2)

Country Link
NO (1) NO20011869L (fr)
WO (1) WO2002083575A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ES2321782A1 (es) * 2006-08-09 2009-06-10 Jose Juan Sanmartin Ruano Procedimiento para la obtencion de agua salada esterilizada.

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS567687A (en) * 1979-06-30 1981-01-26 Sumitomo Precision Prod Co Ltd Waste water ozonizing method
FR2511359A1 (fr) * 1981-08-17 1983-02-18 Trailigaz Procede de traitement d'eaux usees par l'ozone
GB2302869A (en) * 1995-07-05 1997-02-05 Mitsubishi Electric Corp Ozone purifying apparatus

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS567687A (en) * 1979-06-30 1981-01-26 Sumitomo Precision Prod Co Ltd Waste water ozonizing method
FR2511359A1 (fr) * 1981-08-17 1983-02-18 Trailigaz Procede de traitement d'eaux usees par l'ozone
GB2302869A (en) * 1995-07-05 1997-02-05 Mitsubishi Electric Corp Ozone purifying apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ES2321782A1 (es) * 2006-08-09 2009-06-10 Jose Juan Sanmartin Ruano Procedimiento para la obtencion de agua salada esterilizada.
ES2321782B1 (es) * 2006-08-09 2010-03-17 Jose Juan Sanmartin Ruano Procedimiento para la obtencion de agua salada esterilizada.

Also Published As

Publication number Publication date
NO20011869D0 (no) 2001-04-11
NO20011869L (no) 2002-10-14

Similar Documents

Publication Publication Date Title
She et al. Partial nitrification and denitrification in a sequencing batch reactor treating high-salinity wastewater
Dapena-Mora et al. Anammox process for nitrogen removal from anaerobically digested fish canning effluents
Mohseni-Bandpi et al. Denitrification of groundwater using acetic acid as a carbon source
Grommen et al. An improved nitrifying enrichment to remove ammonium and nitrite from freshwater aquaria systems
EP0826639A1 (fr) Traitement biologique des eaux usées
JP5211675B2 (ja) 安水からのアンモニア性窒素およびｃｏｄ成分の除去方法
JP6210883B2 (ja) 廃水処理装置の運転方法
WO2006115199A1 (fr) Procede de traitement des eaux usees contenant un compose organique
JP3460745B2 (ja) 生物学的硝化脱窒素方法と装置
Mažeikienė et al. Biotechnological wastewater treatment in small-scale wastewater treatment plants
JP6326230B2 (ja) 二酸化塩素を使用してｂ級のバイオソリッドを得るための廃水処理デバイス
CN112243428A (zh) 处理废水和提供a类污泥的系统和方法
JP2003047990A (ja) 生物脱窒装置
Malnou et al. Biological phophorus removal: Study of the main parameters
Akowanou et al. The combined effect of three floating macrophytes in domestic wastewater treatment
KR100403850B1 (ko) 액상부식법에 있어서 축산폐수 또는 분뇨 고도처리의 질소및 인 제거방법과 이에 따르는 슬러지 감량화 시스템
Willers et al. Nitrification limitation in animal slurries at high temperatures
Can-Dogan et al. Sulfide removal from industrial wastewaters by lithotrophic denitrification using nitrate as an electron acceptor
JP2003024987A (ja) アンモニア性窒素含有水の硝化方法
KR20010088714A (ko) 하·폐수로부터 질소와 인의 제거방법 및 그 제거장치
JP4867099B2 (ja) 生物脱窒処理方法
WO2002083575A1 (fr) Procede pour ajouter de l'eau salee a des compositions aqueuses avant ou pendant un traitement d'oxydation
KR100517095B1 (ko) 하수의 처리 장치 및 방법
JPH0691292A (ja) 嫌気−好気活性汚泥処理装置の運転制御方法
JP2005046697A (ja) 活性汚泥処理方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ OM PH PL PT RO RU SD SE SG SI SK SL TJ TM TN TR TT TZ UA UG US UZ VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP

WWW Wipo information: withdrawn in national office

Country of ref document: JP