EP0000230B1 - Procédé pour la purification biologique d'eau résiduaire - Google Patents

Procédé pour la purification biologique d'eau résiduaire Download PDF

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Publication number
EP0000230B1
EP0000230B1 EP78200057A EP78200057A EP0000230B1 EP 0000230 B1 EP0000230 B1 EP 0000230B1 EP 78200057 A EP78200057 A EP 78200057A EP 78200057 A EP78200057 A EP 78200057A EP 0000230 B1 EP0000230 B1 EP 0000230B1
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EP
European Patent Office
Prior art keywords
process according
hydrolysate
hydrolysis
sludge
waste water
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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
Application number
EP78200057A
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German (de)
English (en)
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EP0000230A1 (fr
Inventor
Bernardus Henricus Nicolaas Dassen
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Stamicarbon BV
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Stamicarbon BV
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Publication date
Application filed by Stamicarbon BV filed Critical Stamicarbon BV
Publication of EP0000230A1 publication Critical patent/EP0000230A1/fr
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/001—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from waste materials, e.g. kitchen waste
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S426/00—Food or edible material: processes, compositions, and products
    • Y10S426/807—Poultry or ruminant feed

Definitions

  • the invention relates to a process for biological purification of waste water, in which an aqueous suspension of the surplus sludge formed during the purification is hydrolyzed in a basic medium and at an elevated temperature.
  • a process of this kind is known from the Netherlands Patent Application 6, 911,163.
  • the sludge formed is hydrolyzed with the aid of sodium hydroxide or, possibly, calcium oxide.
  • the resulting solid matter mainly consisting of inorganic salts and waterinsoluble organic substances, like cell walls which are not, or only partly, hydrolyzed, is filtered off and subjected to further processing.
  • the hydrolysate which consists of an aqueous solution of mainly organic material and sodium salts, is returned to the purification plant.
  • Sodium hydroxide is here used for hydrolysis of sludge, as a result of which the hydrolysate contains rather large quantities of sodium ions.
  • the hydrolysate which mainly consists of an aqueous solution of amino acids, oligopeptides and hydrolysis products of carbohydrates and fats, these sodium ions present problems.
  • the basic amino acids are commercially important components of the hydrolysate. If one wants to recover these from the hydrolysate by means of selective ion exchange, all sodium ions present should be removed first, owing to which this process becomes unattractive economically.
  • the purpose of the invention is to provide a process in which these disadvantages do not occur.
  • the process according to the invention is characterized in that the suspension of the sludge is given a pH value of between 8 and 11 and that hydrolysis is carried out in the presence of a volatile base at a temperature of between 90 and 300 °C, which base is expelled from the hydrolysate formed after the hydrolysis has been terminated.
  • a volatile base at a temperature of between 90 and 300 °C, which base is expelled from the hydrolysate formed after the hydrolysis has been terminated.
  • ammonia or a bound form thereof e.g. ammonium carbonate
  • the ammonia that has been removed from the hydrolysate is returned to the hydrolysis stage.
  • the hydrolysis is, preferably, carried out at a temperature of between 90 and 200 °C.
  • a process of this kind brings great advantages over known processes. Since, at the pH value applied, practically no racemization of amino acids occurs, a hydrolysate is obtained which mainly contains the amino acids and oligopeptides occuring in nature.
  • the process according to the invention has the great advantage that it entails practically no extra costs for chemicals.
  • the volatile base used like ammonia, is recovered by stripping the liquid, e.g. with an inert gas or gasmixture like air or steam, and can be refused. Without much trouble the residual content of ammonia can be reduced to 10 ppm after the stripping. If sodium hydroxide or calcium oxide is used, new chemicals must continually be supplied, which places a heavy financial burden on the waste water purification. Moreover, it may be necessary first to neutralize the hydrolysate before it can be used further. It is preferred that, after the solid matter and the volatile base have been separated off, the hydrolysate be further processed to economically attractive products.
  • hydrolysate may be the processing into cattle feed, while, in certain cases, it may be the best solution to use the hydrolysate as carbon source in the denitrification step of an industrial waste water purification plant, possibly after one or more nitrogen compounds have been separated off.
  • the hydrolysate may also be mixed with the raw waste water and be passed through the entire plant, during which, contrary to the known process, no disturbance of the pH equilibrium in the plant occurs. Returning of the hydrolysate to the waste water purification plant, however, is only possible if one has a waste water purification in which also nitrogen compounds are removed, because otherwise an unacceptable amount of nitrate will be discharged into the surface water.
  • the process according to the invention can be realized at the usual pressures for handling aqueous NH 3 solutions.
  • the pressure lies between 0.1 - 5 MPa.
  • the concentration of ammonia and/or ammonium carbonate amounts preferably to 2 to 14 N. It is possible to carry out the hydrolysis under such conditions that complete or partial de-amination of the amino acids present occurs. In the case of a return of the hydrolysate to the waste water purification plant this brings the advantage that a substantially smaller nitrogen load occurs.
  • For deamination to be achieved it is necessary to work at higher temperatures and NH 3 concentrations, for instance a temperature above 150 °C and a concentration of between 4 and 14 N NH 3 . If it should not be the intention to deaminate, it is to be preferred to work at temperatures of between 90 and 180 °C and at an NH 3 concentration of between 2 and 6 N NH 3 .
  • the sludge suspension to be hydrolyzed contains, depending on the type of plant of origin, varying contents of sludge (dry matter). This may vary between less than 1 % by weight and more than 35 % by weight.
  • Figure 1 of the drawing shows a possible embodiment of the process according to the invention
  • Figure 2 shows another embodiment thereof.
  • FIG. 1 shows a diagram for a process for purification of waste water according to the invention.
  • Waste water here enters via line 1 biological purification plant 2, here indicated as a block.
  • the purified waste water which contains suspended biologically activated sludge, is led through line 3 to section 4, where the sludge settles and thickens.
  • Via line 5 purified water is discharged into surface water or for further treatment, for instance with chlorine.
  • Via line 6 a sludge suspension from section 4 is recycled to the biological purification plant.
  • Via line 7 a concentrated sludge suspension is passed to heat exchanger 8.
  • Via line 9 the heated suspension is led into hydrolysis column 10.
  • Via line 11 a gas mixture of NH 3 and steam originating in heater 12 is supplied.
  • hydrolysis column 10 In heater 12 the mixture of NH 3 and steam is heated with the aid of steam coil 13.
  • the hydrolyzed sludge suspension leaves hydrolysis column 10 via line 14.
  • filtration equipment 15 which may, for instance, consist of filters, sieve bends or centrifuges, this suspension is split up into a hydrolysate and solid matter.
  • the solid matter is discharged via line 16.
  • the hydrolysate proceeds to desorption column 18.
  • FIG 2 in which the various reference numbers have the same meaning as in Figure 1, shows another embodiment of the process according to the invention.
  • Waste water here enters biological purification plant 2 via line 1.
  • the purified waste water which contains suspended activated sludge, is led through line 3 to section 4, where the sludge settles and thickens.
  • Via line 5 purified water is discharged.
  • Via line 6 part of the sludge suspension from section 4 is recycled to the purification plant.
  • a concentrated sludge suspension is led to static mixer 23, in which this suspension is mixed with hydrolyzed sludge that is supplied through line 24.
  • the mixture is passed to heat exchanger 8 via line 25.
  • the heated suspension is led into hydrolysis column 10 via line 9.
  • Via line 26 a steam/NH 3 mixture is led into hydrolysis column 10.
  • Via line 14 the treated sludge suspension is discharged. Part of this suspension is mixed with the sludge suspension from section 4, another part is supplied to desorption column 18 via line 27. Via line 19 the steam required for the desorption and the hydrolysis is supplied.
  • the chemical oxygen demand (COD) is given in the last column. This is a measure of the hydrolysis of the biologically active sludge.
  • Waste water from a chemical complex is supplied to a plant as described in Figure 1.
  • 32.0 tons/h of sludge suspension is produced, which is discharged from section 4 via line 6.
  • the sludge suspension contains 20 % of sludge (dry matter), approximately 75 % of which is inorganic material and approximately 25 % organic material.
  • the organic material mainly consists of microorganisms and these principally contain amino acids, carbohydrates and fats in a ratio of 5 : 4 : 1.
  • This suspension is hydrolyzed in hydrolysis column 10 with the aid of 2 tons/h of NH 3 and steam at a temperature of 130°C and a pressure of 0.7 MPa.
  • the hydrolyzed sludge is separated, in 15, into 2.4 tons/h of solid matter and 35.6 tons/h of hydrolysate, which contains 0.8 ton/h of organic material and 32.8 tons/h of water.
  • the solid matter contains 90 % of the heavy metals which were present in the sludge suspension.
  • the hydrolysate is treated in desorption column 18 with steam of 1.6 MPa, all NH 3 escaping and being recycled via line 20.
  • Waste water from a chemical complex is supplied to a plant as described in Figure 2.
  • the sludge suspension contains 20 % of sludge (dry matter), approximately 75 % of which is inorganic material and approximately 25 % organic material.
  • the organic material mainly consists of microorganisms and these principally contain amino acids, carbohydrates and fats in a ratio of 5 : 4 : 1.
  • This suspension is hydrolyzed in hydrolysis column 10 with the aid of 56.8 tons/day of NH 3 /steam mixture at a temperature of 130°C and a pressure of 10 ats abs.
  • the hydrolysate is treated in desorption column 18 with steam of 1 MPa, all NH 3 and part of the steam escaping and being recycled via line 20.
  • the hydrolyzed sludge is separated in 15 into 37.5 tons/h of solids matter and 296.7 tons/day of hydrolysate, which contains 17.5 tons/day of organic material and 279.2 tons/day of water.
  • the solid mater contains 90 % of the heavy metals that were present in the sludge.suspension.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Polymers & Plastics (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Biochemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Food Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Sludge (AREA)
  • Removal Of Specific Substances (AREA)
  • Fertilizers (AREA)
  • Feed For Specific Animals (AREA)
  • Fodder In General (AREA)

Claims (11)

1. Procédé de purification biologique d'eaux résiduaires, selon lequel une suspension de la boue formée pendant la purification est hydrolysée dans un milieu basique et à des températures élevées, lequel procédé se caractérise en ce que l'hydrolyse est effectuée à un pH de 8-11 et à des températures situées entre 90-300°C alors qu'on utilise une base volatile qui, l'hydrolyse étant terminée, est dégagée du produit d'hydrolyse formé.
2. Procédé selon la revendication 1, caractérisé en ce que l'hydrolyse est effectuée à une température située entre 90 et 200°C.
3. Procédé selon l'une des revendications 1 à 2, caractérisé en ce que de l'ammoniaque est utilisée comme base volatile.
4. Procédé selon l'une des revendications 1 à 2, caractérisé en ce que du carbamate d'ammonium est utilisé comme base volatile.
5. Procédé selon l'une des revendications 1 à 4, caractérisé en ce que la base volatile dégagée du liquide est ramenée à l'hydrolyse.
6. Procédé selon l'une des revendications 1 à 5, caractérisé en ce que un ou plusieurs mélanges de N sont récupérés du produit d'hydrolyse formé.
7. Procédé selon l'une des revendications 1 à 6, caractérisé en ce que le produit d'hydrolyse formé est transformé entièrement ou partiellement en fourrage.
8. Procédé selon l'une des revendications 1 à 7, caractérisé en ce que le produit d'hydrolyse formé est ramené -après que -l'agent solide en est séparé- à l'installation de purification biologique.
9. Procédé selon l'une des revendications 1 à 7, caractérisé en ce que la base volatile est chassée du produit d'hydrolyse à l'aide d'un gaz inert ou d'un mélange de gaz.
10. Procédé selon l'une des revendications 1, 3 à 7, caractérisé en ce que le processus est exécuté sous des conditions dans lesquelles il se produit une désamination.
11. Procédé selon la revendication 10, caractérisé en ce que l'hydrolyse est normalement exécutée à une température située entre 150 et 300°C et à une concentration de NH3 située entre 4 et 14 normale.
EP78200057A 1977-06-27 1978-06-21 Procédé pour la purification biologique d'eau résiduaire Expired EP0000230B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL7707081 1977-06-27
NL7707081A NL7707081A (nl) 1977-06-27 1977-06-27 Werkwijze voor het biologisch zuiveren van afvalwater.

Publications (2)

Publication Number Publication Date
EP0000230A1 EP0000230A1 (fr) 1979-01-10
EP0000230B1 true EP0000230B1 (fr) 1981-01-21

Family

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EP78200057A Expired EP0000230B1 (fr) 1977-06-27 1978-06-21 Procédé pour la purification biologique d'eau résiduaire

Country Status (6)

Country Link
US (2) US4190528A (fr)
EP (1) EP0000230B1 (fr)
JP (1) JPS5413664A (fr)
DE (1) DE2860355D1 (fr)
IT (1) IT1105452B (fr)
NL (1) NL7707081A (fr)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4289625A (en) * 1980-01-18 1981-09-15 Institute Of Gas Technology Hybrid bio-thermal gasification
US4915840A (en) * 1988-06-07 1990-04-10 Bioprocess Engineering, Inc. Process for sludge reduction in an aerobic sludge generating waste treatment system
US5190655A (en) * 1989-01-11 1993-03-02 Karlsson Johan L I Water purification process 2
US5360546A (en) * 1992-04-01 1994-11-01 Ngk Insulators, Ltd. Method for treating organic sludge
US5525229A (en) * 1994-09-14 1996-06-11 North Carolina State University Process and apparatus for anaerobic digestion
JP3048889B2 (ja) * 1995-06-29 2000-06-05 神鋼パンテツク株式会社 活性汚泥処理方法及びそのための活性汚泥処理装置
RU2079454C1 (ru) * 1995-07-18 1997-05-20 Грудинин Владимир Павлович Способ обработки избыточного активного ила
DE19627875A1 (de) * 1996-07-11 1998-01-15 Bsbg Bremer Sonderabfall Berat Verfahren zur Behandlung von Schlämmen mit organischen Anteilen, insbesondere Klärschlämmen
US6013183A (en) * 1998-08-05 2000-01-11 Paradigm Environmental Technologies Inc. Method of liquefying microorganisms derived from biological wastewater treatment processes
EP1112971A4 (fr) * 1998-08-07 2002-01-02 Vladimir Pavlovich Grudinin Procede de production d'un carburant organique liquide et sans soufre
DE19940994B4 (de) 1999-08-28 2004-02-26 Clausthaler Umwelttechnikinstitut Gmbh, (Cutec-Institut) Verfahren zum Abbau von Klärschlamm
DE10014185A1 (de) * 2000-03-23 2001-09-27 Bsbg Bremer Sonderabfall Berat Verfahren und Vorrichtung zum Behandeln organischen Materials
DE10347476B4 (de) 2003-10-01 2018-07-26 Pondus Verfahrenstechnik Gmbh Vorrichtung und Verfahren zum Zellaufschluss in Schlämmen

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2012621A (en) * 1932-02-09 1935-08-27 Hercules Powder Co Ltd Method of producing anhydrous ammonia
US3522173A (en) * 1968-11-12 1970-07-28 Western Mechanical Inc Water purification method
NL6911263A (fr) * 1969-07-23 1971-01-26
DE2042785C3 (de) * 1970-08-28 1980-10-23 Nyby Bruks Ab, Nybybruk (Schweden) Verfahren zur Aufbereitung von verbrauchten HNO3 und HF enthaltenden Beizbädern
CH583525A5 (en) * 1974-01-16 1977-01-14 Wacker Chemie Gmbh Prodn of protein-contg feedstuffs - from activated sludge by shock drying
US4038180A (en) * 1974-11-22 1977-07-26 Agway, Inc. Process of dewatering sewage sludge
GB1533462A (en) * 1975-02-05 1978-11-22 Sterling Drug Inc Method and apparatus for ammonia removal from wastewaters
DE2553840C3 (de) * 1975-11-29 1981-01-29 Bayer Ag, 5090 Leverkusen Druckhydrolytische Behandlung von Abwasser
US4119495A (en) * 1977-01-21 1978-10-10 Vasily Dmitrievich Belyaev Method for processing activated sludge into useful products

Also Published As

Publication number Publication date
JPS5413664A (en) 1979-02-01
IT7849964A0 (it) 1978-06-21
IT1105452B (it) 1985-11-04
EP0000230A1 (fr) 1979-01-10
US4190528A (en) 1980-02-26
US4240904A (en) 1980-12-23
DE2860355D1 (en) 1981-03-12
NL7707081A (nl) 1978-12-29

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