FR2484990A2 - Purification of effluent water contg. sulphate and organic material - by anaerobic bacterial treatment and continuous desulphurisation of partial side stream - Google Patents
Purification of effluent water contg. sulphate and organic material - by anaerobic bacterial treatment and continuous desulphurisation of partial side stream Download PDFInfo
- Publication number
- FR2484990A2 FR2484990A2 FR8013514A FR8013514A FR2484990A2 FR 2484990 A2 FR2484990 A2 FR 2484990A2 FR 8013514 A FR8013514 A FR 8013514A FR 8013514 A FR8013514 A FR 8013514A FR 2484990 A2 FR2484990 A2 FR 2484990A2
- Authority
- FR
- France
- Prior art keywords
- gas
- mass
- liquid
- sulphate
- reaction mass
- 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.)
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Classifications
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/282—Anaerobic digestion processes using anaerobic sequencing batch reactors
-
- 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
- C02F3/28—Anaerobic digestion processes
-
- 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
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
- C02F3/345—Biological treatment of water, waste water, or sewage characterised by the microorganisms used for biological oxidation or reduction of sulfur compounds
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- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Physical Water Treatments (AREA)
Abstract
Description
Le brevet principal est relatif à un procédé pour l'épuration biologique d'eaux résiduaires à forte pollution organique et contenant des sulfates à l'aide de bactéries anaérobies, avec brassage de la masse en réaction, dans lequel les sulfures formés à partir des sulfates au cours du processus biologique sont éliminés à l'aide d'un gaz d'entraihement que l'on introduit dans la masse en réaction. The main patent relates to a process for the biological purification of waste water with high organic pollution and containing sulfates using anaerobic bacteria, with mixing of the reaction mass, in which the sulfides formed from the sulfates. during the biological process are eliminated using a entrainment gas which is introduced into the mass in reaction.
Le procédé suivant le brevet principal est caractérisé en ce que le gaz d'entrainement des sulfures est le gaz formé au cours du #processus biologique, que l'on désulfure avant de le réintroduire dans la masse en réaction. Ce gaz sert simultanément au brassage de la masse liquide. The process according to the main patent is characterized in that the sulphide entrainment gas is the gas formed during the biological process, which is desulphurized before being reintroduced into the reaction mass. This gas is used simultaneously for mixing the liquid mass.
L'excès de gaz est utilisable comme combustible.The excess gas can be used as fuel.
Le même brevet décrit une forme de réalisation d'une installation à 1' aide de laquelle on peut mettre en oeuvre l'invention. The same patent describes an embodiment of an installation with the aid of which the invention can be implemented.
Dans cette forme de réalisation l'installation comporte un digesteur dans lequel se déroulent les réactions d'acidification et de méthanisation au sein d'une masse liquide en réaction parcourue par les bulles de gaz provenant d'une part des activités biologiques en cours, d'autre part du gaz d'entrainement injecté dans la masse en réaction, cons#titué de préférence par une fraction du gaz formé dans le digesteur, mais désulfuré dans une installation annexe avant d'être recyclé dans la masse en réaction. In this embodiment, the installation comprises a digester in which the acidification and methanation reactions take place within a reacting liquid mass traversed by the gas bubbles originating on the one hand from the ongoing biological activities, d on the other hand, the entrainment gas injected into the reaction mass, preferably consisting of a fraction of the gas formed in the digester, but desulphurized in an additional installation before being recycled into the reaction mass.
On a maintenant trouvé que la surveillance de la teneur en sulfures au sein de la masse en réaction est grandements facilitéesi l'on effectue l'évacuation des sulfures formés au cours du processus biochimique dans une installation annexe. It has now been found that the monitoring of the sulphide content within the reaction mass is greatly facilitated if the sulphides formed during the biochemical process are evacuated in an auxiliary installation.
A cet effet, on fait passer en continu la masse réactionnelle dans une colonne de strippage qui fonctionne de préférence avec le gaz issu de la réaction même, après désulfuration. To this end, the reaction mass is passed continuously through a stripping column which preferably operates with the gas resulting from the reaction itself, after desulphurization.
Par conséquent, la présente invention a pour objet un procédé pour l'épuration en continu d'eaux résiduaires à forte pollution organique contenant des sulfates à l'aide de bactéries anaérobies avec brassage de la masse en réaction, dans lequel on élimine les sulfures formés à partir des sulfates au cours du processus biologique à l'aide d'un gaz d'entraíhement que l'on introduit dans la masse en réaction, caractérisé en ce que l'on dérive en continu une fraction de la masse en réaction dans une installation séparée et en ce que l'élimination des sulfures est effectuée dans cette fraction dérivée. Consequently, the present invention relates to a process for the continuous purification of highly organic waste water containing sulfates using anaerobic bacteria with mixing of the reaction mass, in which the sulfides formed are eliminated. from sulfates during the biological process using a entrainment gas which is introduced into the reaction mass, characterized in that a fraction of the reaction mass is continuously derived in a separate installation and in that the removal of sulphides is carried out in this derived fraction.
Selon l'invention on isole donc en continu une partie de la masse réactionnelle par transfert dans un récipient ayant de préférence la forme d'une colonne, dans lequel on fait passer à contre-courant et de bas en haut un gaz de strippage pour éliminer les sulfures jusqu'à la teneur tolérable souhaitée, clest-à-dire égale ou inférieure à 10 mg/l. According to the invention, therefore, a portion of the reaction mass is continuously isolated by transfer to a container, preferably in the form of a column, in which a stripping gas is passed against the current and from bottom to top to eliminate sulphides up to the desired tolerable content, ie equal to or less than 10 mg / l.
Le volume de la masse soumise au strippage est habituellement choisi entre 0, 3 et 1, 0 % en volume de la masse réactionnelle dans le digues teur principal, tandis que le rapport entre le débit d'entrée de l'eau à épurer et le débit d'alimentation de la colonne de strippage est choisi entre 1/2 et 1/50. A la sortie de la colonne de strippage on recycle une quantité de masse réactionnelle dans le digesteur principal suffisante pour maintenir le volume de liquide dans celui-ci constant, le reste est évacué. Par recyclage du liquide traité et désulfuré dans le digesteur principal, on contrôle dans ce dernier la teneur en sulfures pour la maintenir égale ou inférieure à o, 1 g/l.La durée de séjour du liquide dans la colonne de strippage dépendant notamment du débit d'alimentation de celle-ci, est déterminée en fonction de la teneur en sulfates du liquide à épurer, de manière à la maintenir au-dessous de la valeur sus-indiquée.The volume of the mass subjected to stripping is usually chosen between 0.3 and 1.0% by volume of the reaction mass in the main dam, while the ratio between the inlet flow rate of the water to be purified and the feed rate of the stripping column is chosen between 1/2 and 1/50. At the outlet of the stripping column, a quantity of reaction mass is recycled in the main digester sufficient to keep the volume of liquid in it constant, the rest is discharged. By recycling the treated and desulphurized liquid in the main digester, the sulphide content is controlled in the latter to maintain it equal to or less than 0.1 g / l. The duration of stay of the liquid in the stripping column depends in particular on the flow rate supply thereof, is determined according to the sulphate content of the liquid to be purified, so as to keep it below the above-mentioned value.
Comme cela a déjà été indiqué dans le brevet principal, on peut utiliser comme gaz de strippage tout gaz inerte vis-à-vis du processus de digestion anaérobie, mais on choisit de préférence le gaz formé au cours de la digestion, après l'avoir soumis à un traitement de désulfuration, la teneur en ions S.= de ce gaz devant être inférieure à 1, 5 % en volume, la teneur minimale que l'on peut atteindre étant 0, 1 % en volume (respectivement 0, 021 et 0; 0014 g de s=/î gaz). As already indicated in the main patent, it is possible to use as stripping gas any inert gas with respect to the anaerobic digestion process, but the gas formed during the digestion is preferably chosen, after having subjected to a desulphurization treatment, the content of S. = ions of this gas must be less than 1.5% by volume, the minimum content which can be reached being 0.1% by volume (respectively 0.021 and 0.0014 g of s = / gas).
Dans la plupart des casla masse dans le digesteur principal est suffisamment brassée par le prélèvement et le recyclage de la fraction soumise à la désulfuration dans la colonne de strippage annexe. En cas de besoin on peut, bien entendu, conformément au procédé décrit dans le brevet principal, introduire du gaz de strippage dans le digesteur pour augmenter ainsi la vigueur du brassage. Dans la pratique on-a constaté que le rapport : débit de gaz de strippage/gaz formé dans le digesteur, est avantageusement compris entre 2/1 et 70/1. Le choix du débit à retenir sera fait par llhomme du métier qui fixera expérimentalement les paramètres de fonctionnement de la colonne de strippage en tenant compte des indications concernant la durée de séjour et la teneur en sulfure donnéesci-dessus et nécessaires pour la réalisation de l'invention. In most cases, the mass in the main digester is sufficiently stirred by the removal and recycling of the fraction subjected to desulphurization in the annex stripping column. If necessary, it is of course possible, in accordance with the process described in the main patent, to introduce stripping gas into the digester to thereby increase the vigor of the stirring. In practice, it has been found that the ratio: flow of stripping gas / gas formed in the digester, is advantageously between 2/1 and 70/1. The choice of the flow rate to be retained will be made by a person skilled in the art who will experimentally fix the operating parameters of the stripping column taking into account the indications concerning the residence time and the sulphide content given above and necessary for carrying out the invention.
L'installation pour la mise en oeuvre de la présente invention comporte un digesteur dans lequel se déroulent les r éactions d'acidification et de méthanisation au sein de la masse liquide en réaction et une colonne de strippage dans laquelle est amenée en continu une partie de cette masse liquide pour y être désulfurée par injection d'une partie des gaz évacués du digesteur et préalablement désulfurés dans une installation annexe de désulfuration conformément au procédé décrit dans le brevet principal; la masse liquide désulfurée dans la colonne de strippage étant recyclée en continu dans le digesteur. Les gaz évacués de la colonne de strippage sont amenés à l'installation de désulfuration si nécessaire, en fonction de la concentration en sulfures dans le digesteur, une partie des gaz désulfurés est éventuellement utilisée pour le brassage de la masse liquide en réaction. The installation for implementing the present invention comprises a digester in which the acidification and methanisation reactions take place within the liquid mass in reaction and a stripping column into which a portion of this liquid mass to be desulphurized therein by injection of a part of the gases evacuated from the digester and previously desulphurized in an additional desulphurization installation in accordance with the process described in the main patent; the desulphurized liquid mass in the stripping column being continuously recycled in the digester. The gases evacuated from the stripping column are brought to the desulphurization installation if necessary, depending on the concentration of sulphides in the digester, part of the desulphurized gases is optionally used for stirring the liquid mass in reaction.
Une telle installation est représentée schématiquement à titre non limitatif dans la figure unique du dessin annexé. Such an installation is shown schematically without limitation in the single figure of the accompanying drawing.
L'eau à traiter, fortement polluée par des matières organiques et contenant des sulfates, est introduite à raison de 9 m3/h par le conduit 1 dans le digesteur principal 2. Par le conduit 5 on achemine du liquide du haut du digesteur vers le haut de la# colonne de strippage 3 dans laquelle on introduit par le conduit 11 du gaz de brassage et de strippage qui, après avoir parcouru le liquide dans la colonne sort par le conduit 9. Ce dernier rejoint le conduit 6 conduisant les gaz développés par la masse réactionnelle dans le digesteur 1, l'ensemble des gaz étant conduit vers le désulfurateur 7. La majeure partie des gaz sortant de ce dispositif 7 est amenée par le conduit 10 à la pompe 8-qui alimente le conduit 11. U#e partie du liquide ayant traversé la colonne 3 est recyclée dans le digesteur 2, la partie restante est évacuée par la vidange 12. The water to be treated, heavily polluted by organic matter and containing sulphates, is introduced at a rate of 9 m3 / h through line 1 into the main digester 2. Through line 5, liquid is conveyed from the top of the digester top of the # stripping column 3 into which the stirring and stripping gas is introduced via the conduit 11 which, after having passed through the liquid in the column, leaves via the conduit 9. The latter joins the conduit 6 leading the gases developed by the reaction mass in the digester 1, all of the gases being led to the desulfurizer 7. The major part of the gases leaving this device 7 is brought by the conduit 10 to the pump 8-which feeds the conduit 11. U # e part of the liquid having passed through the column 3 is recycled in the digester 2, the remaining part is evacuated by the drain 12.
Les gaz désulfurés non recyclés sont stockés (sortie S).The non-recycled desulfurized gases are stored (outlet S).
L'invention sera décrite plus en détail dans la'exemple non limitatif ci-après. The invention will be described in more detail in the following non-limiting example.
Exemple
On traite par digestion anaérobie dans une installation du type - représenté dans la figure unique une eau résiduaire contenant 15 g/l de
DCO, 10 g/l de DBPS et 2, 5 g/l de 504 que l'on introduit à raison de 20 m3/;h dans un digesteur permettant de maintenir le volume de la masse réactionnelle à 2500 m3. Le sulfate transformé donne naissance à un débit de 70 m3/h de 1125. Example
Waste water containing 15 g / l of an anaerobic digestion is treated in an installation of the type represented in the single figure
COD, 10 g / l of DBPS and 2.5 g / l of 504 which are introduced at the rate of 20 m3 /; h into a digester allowing the volume of the reaction mass to be maintained at 2500 m3. The transformed sulphate gives rise to a flow rate of 70 m3 / h of 1125.
La colonne de strippage contenant 8 m3 de liquide réactionnel à traiter est alimentée à raison de 160 m3/h de liquide réactionnel en provenance du digesteur principal, tandis que le débit du gaz de strippage désulfuré est mantenu à 530 m3/h. Dans-la colonne de strippage se forme 8 m3/b de gaz, qui, additionnés au gaz de strippage, donnent à la sortie 538 m3/h de gaz. Le débit total des gaz conduits à la désulfuration est de 608 m3/h, donnant 600 m3/h de gaz désulfurés. Compte tenu des 530 m3/hrecyclés, on envoie au stockage 70 m3/h de gaz (C02 + CH# l'eau traitée contenant 7 g/l de DCO, 3 g/l de D305 et 0, 5 g/l de SO
4 The stripping column containing 8 m3 of reaction liquid to be treated is supplied at the rate of 160 m3 / h of reaction liquid coming from the main digester, while the flow rate of the desulfurized stripping gas is maintained at 530 m3 / h. In the stripping column 8 m3 / b of gas is formed, which, added to the stripping gas, give the outlet 538 m3 / h of gas. The total flow rate of the gases led to the desulfurization is 608 m3 / h, giving 600 m3 / h of desulfurized gases. Taking into account the 530 m3 / h recycled, 70 m3 / h of gas is sent to storage (C02 + CH # the treated water containing 7 g / l of COD, 3 g / l of D305 and 0.5 g / l of SO
4
Claims (4)
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8013514A FR2484990A2 (en) | 1979-07-23 | 1980-06-18 | Purification of effluent water contg. sulphate and organic material - by anaerobic bacterial treatment and continuous desulphurisation of partial side stream |
| BR8004557A BR8004557A (en) | 1979-07-23 | 1980-07-22 | PROCESS FOR THE CONTINUOUS PURIFICATION OF RESIDUAL WATERS WITH STRONG ORGANIC POLLUTION AND CONTAINING SULFATES |
| AR28187080A AR226433A1 (en) | 1979-07-23 | 1980-07-23 | PROCEDURE FOR ANAEROBIC BIOLOGICAL DEPURATION OF STRONG WASTEWATER ORGANIC CONTAMINATION CONTAINING SULPHATES |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR7918899A FR2461684A1 (en) | 1979-07-23 | 1979-07-23 | Purificn. of organically polluted water contg. sulphate(s) - using anaerobic bacteria with sulphide(s) removed by gas entrainment |
| FR8013514A FR2484990A2 (en) | 1979-07-23 | 1980-06-18 | Purification of effluent water contg. sulphate and organic material - by anaerobic bacterial treatment and continuous desulphurisation of partial side stream |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| FR2484990A2 true FR2484990A2 (en) | 1981-12-24 |
| FR2484990B2 FR2484990B2 (en) | 1985-04-19 |
Family
ID=26221277
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| FR8013514A Granted FR2484990A2 (en) | 1979-07-23 | 1980-06-18 | Purification of effluent water contg. sulphate and organic material - by anaerobic bacterial treatment and continuous desulphurisation of partial side stream |
Country Status (3)
| Country | Link |
|---|---|
| AR (1) | AR226433A1 (en) |
| BR (1) | BR8004557A (en) |
| FR (1) | FR2484990A2 (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0241602A1 (en) * | 1986-04-16 | 1987-10-21 | Gist-Brocades N.V. | Anaerobic purification of wastewater, containing sulphate and organic material |
| EP0331806A1 (en) * | 1988-03-09 | 1989-09-13 | Passavant-Werke Ag | Process for the anaerobic purification of waste and process water |
| US4966704A (en) * | 1986-09-24 | 1990-10-30 | Ac Biotechnics Ab | Anaerobic process for microbiological purification of sulphur-containing water |
| FR2651769A1 (en) * | 1989-09-14 | 1991-03-15 | Degremont | PROCESS OF TREATMENT, BY ANAEROBIC FERMENTATION, OF WASTEWATER FOR THE REMOVAL OF ORGANIC MATERIAL AND OF THE SULFATES CONTAINED THEREIN. |
| WO1991019558A1 (en) * | 1990-06-15 | 1991-12-26 | Paques B.V. | Process for the removal of hydrogensulphide (h2s) from biogas |
| WO1996000191A1 (en) * | 1994-06-23 | 1996-01-04 | Nederlandse Organisatie Voor Toegepast- Natuurwetenschappelijk Onderzoek Tno | Anaerobic removal of sulphur compounds from waste water |
| US5651890A (en) * | 1995-04-04 | 1997-07-29 | Trost; Paul B. | Use of propane as stripper gas in anaerobic digestion of wastewaters |
| US6361694B1 (en) | 2000-06-26 | 2002-03-26 | Paul B. Trost | Enhanced biomass digestion through intermittent injection of propane |
| ES2167222A1 (en) * | 2000-04-10 | 2002-05-01 | Meyme S A | Process and installation for treatment of purin in cattle-raising establishments involves purin deposited in pond or pit which is impermeable and tight, being sealed by cover and in which anaerobic fermentation is produced |
| WO2009050661A2 (en) * | 2007-10-16 | 2009-04-23 | Water Research Commission | Process for treating sulphate-containing effluent |
| US20130341269A1 (en) * | 2010-12-27 | 2013-12-26 | Degremont | Method for desulphuration of the digestate and the biogas of a digester, and biogas production facility implementing said method |
| WO2014104877A2 (en) * | 2012-12-24 | 2014-07-03 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3754376A (en) * | 1972-02-01 | 1973-08-28 | Texaco Inc | Inert gas stripping of contaminated water |
| US4040953A (en) * | 1976-03-10 | 1977-08-09 | Rectech, Inc. | Anaerobic digestion process |
-
1980
- 1980-06-18 FR FR8013514A patent/FR2484990A2/en active Granted
- 1980-07-22 BR BR8004557A patent/BR8004557A/en not_active IP Right Cessation
- 1980-07-23 AR AR28187080A patent/AR226433A1/en active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3754376A (en) * | 1972-02-01 | 1973-08-28 | Texaco Inc | Inert gas stripping of contaminated water |
| US4040953A (en) * | 1976-03-10 | 1977-08-09 | Rectech, Inc. | Anaerobic digestion process |
Cited By (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0241602A1 (en) * | 1986-04-16 | 1987-10-21 | Gist-Brocades N.V. | Anaerobic purification of wastewater, containing sulphate and organic material |
| EP0241999A1 (en) * | 1986-04-16 | 1987-10-21 | Biothane Systems International B.V. | Anaerobic purification of waste water containing sulphate and organic material |
| US4966704A (en) * | 1986-09-24 | 1990-10-30 | Ac Biotechnics Ab | Anaerobic process for microbiological purification of sulphur-containing water |
| EP0331806A1 (en) * | 1988-03-09 | 1989-09-13 | Passavant-Werke Ag | Process for the anaerobic purification of waste and process water |
| FR2651769A1 (en) * | 1989-09-14 | 1991-03-15 | Degremont | PROCESS OF TREATMENT, BY ANAEROBIC FERMENTATION, OF WASTEWATER FOR THE REMOVAL OF ORGANIC MATERIAL AND OF THE SULFATES CONTAINED THEREIN. |
| EP0418121A1 (en) * | 1989-09-14 | 1991-03-20 | Degremont S.A. | Process for elimination of organic substances and sulphates from waste waters by means of anaerobic fermentation |
| US5298163A (en) * | 1989-09-14 | 1994-03-29 | Degremont | Process for the treatment of effluents |
| WO1991019558A1 (en) * | 1990-06-15 | 1991-12-26 | Paques B.V. | Process for the removal of hydrogensulphide (h2s) from biogas |
| AU636505B2 (en) * | 1990-06-15 | 1993-04-29 | Paques B.V. | Process for the removal of hydrogensulphide (h2s) from biogas |
| NL9401036A (en) * | 1994-06-23 | 1996-02-01 | Tno | Anaerobic removal of sulfur compounds from wastewater. |
| WO1996000191A1 (en) * | 1994-06-23 | 1996-01-04 | Nederlandse Organisatie Voor Toegepast- Natuurwetenschappelijk Onderzoek Tno | Anaerobic removal of sulphur compounds from waste water |
| US5651890A (en) * | 1995-04-04 | 1997-07-29 | Trost; Paul B. | Use of propane as stripper gas in anaerobic digestion of wastewaters |
| ES2167222A1 (en) * | 2000-04-10 | 2002-05-01 | Meyme S A | Process and installation for treatment of purin in cattle-raising establishments involves purin deposited in pond or pit which is impermeable and tight, being sealed by cover and in which anaerobic fermentation is produced |
| US6361694B1 (en) | 2000-06-26 | 2002-03-26 | Paul B. Trost | Enhanced biomass digestion through intermittent injection of propane |
| AP2926A (en) * | 2007-10-16 | 2014-06-30 | Water Res Commission | Process for treating sulphate-containing effluent |
| WO2009050661A2 (en) * | 2007-10-16 | 2009-04-23 | Water Research Commission | Process for treating sulphate-containing effluent |
| WO2009050661A3 (en) * | 2007-10-16 | 2009-06-11 | Water Res Commission | Process for treating sulphate-containing effluent |
| US20130341269A1 (en) * | 2010-12-27 | 2013-12-26 | Degremont | Method for desulphuration of the digestate and the biogas of a digester, and biogas production facility implementing said method |
| US9359240B2 (en) * | 2010-12-27 | 2016-06-07 | Degremont | Method for desulphuration of the digestate and the biogas of a digester, and biogas production facility implementing said method |
| WO2014104877A2 (en) * | 2012-12-24 | 2014-07-03 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
| WO2014104877A3 (en) * | 2012-12-24 | 2014-10-02 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
| CN105073645A (en) * | 2012-12-24 | 2015-11-18 | 巴格知识产权有限公司 | Hydrogen sulfide removal from anaerobic treatment |
| US9764966B2 (en) | 2012-12-24 | 2017-09-19 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2484990B2 (en) | 1985-04-19 |
| BR8004557A (en) | 1981-02-03 |
| AR226433A1 (en) | 1982-07-15 |
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