WO2010117288A1 - Procede integre de filtration de dreche seche de brasserie - Google Patents

Procede integre de filtration de dreche seche de brasserie Download PDF

Info

Publication number
WO2010117288A1
WO2010117288A1 PCT/PT2010/000016 PT2010000016W WO2010117288A1 WO 2010117288 A1 WO2010117288 A1 WO 2010117288A1 PT 2010000016 W PT2010000016 W PT 2010000016W WO 2010117288 A1 WO2010117288 A1 WO 2010117288A1
Authority
WO
WIPO (PCT)
Prior art keywords
compression
filtration
filter
vacuum drying
vacuum
Prior art date
Application number
PCT/PT2010/000016
Other languages
English (en)
Other versions
WO2010117288A8 (fr
Inventor
Jorge Manuel Rodrigues De Carvalho
Remigio De Matos Machado
Ricardo Anndrlé Duarte RODRIGUES
Carlos Miguel Carvalho Henriques
Paulo Fernando Martins de Magalhâes CORREIA
Original Assignee
Instituto Superior Tecnico
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 Instituto Superior Tecnico filed Critical Instituto Superior Tecnico
Publication of WO2010117288A1 publication Critical patent/WO2010117288A1/fr
Publication of WO2010117288A8 publication Critical patent/WO2010117288A8/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12F—RECOVERY OF BY-PRODUCTS OF FERMENTED SOLUTIONS; DENATURED ALCOHOL; PREPARATION THEREOF
    • C12F3/00—Recovery of by-products
    • C12F3/06—Recovery of by-products from beer and wine
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K10/00—Animal feeding-stuffs
    • A23K10/30—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms
    • A23K10/37—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms from waste material
    • A23K10/38—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms from waste material from distillers' or brewers' waste
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K50/00—Feeding-stuffs specially adapted for particular animals
    • A23K50/10—Feeding-stuffs specially adapted for particular animals for ruminants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D25/00—Filters formed by clamping together several filtering elements or parts of such elements
    • B01D25/003—Filters formed by clamping together several filtering elements or parts of such elements integrally combined with devices for controlling the filtration
    • B01D25/007—Filters formed by clamping together several filtering elements or parts of such elements integrally combined with devices for controlling the filtration by pressure measuring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D25/00—Filters formed by clamping together several filtering elements or parts of such elements
    • B01D25/28—Leaching or washing filter cakes in the filter handling the filter cake for purposes other than regenerating
    • B01D25/282—Leaching or washing filter cakes in the filter handling the filter cake for purposes other than regenerating for drying
    • B01D25/284—Leaching or washing filter cakes in the filter handling the filter cake for purposes other than regenerating for drying by gases or by heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D25/00—Filters formed by clamping together several filtering elements or parts of such elements
    • B01D25/28—Leaching or washing filter cakes in the filter handling the filter cake for purposes other than regenerating
    • B01D25/282—Leaching or washing filter cakes in the filter handling the filter cake for purposes other than regenerating for drying
    • B01D25/285—Leaching or washing filter cakes in the filter handling the filter cake for purposes other than regenerating for drying by compression using inflatable membranes
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
    • Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
    • Y02P60/87—Re-use of by-products of food processing for fodder production

Definitions

  • the present invention was developed at 1ST, in the waste recovery field, with applicability in the brewing industry and in the use of membrane filter presses for waste dehydration.
  • This invention consists in the development of a dehydration process of BSG, as it proceeds from the beer production process, with moisture content between 72% and 85%, for a stabilized BSG, and with a moisture content of 15%, maintaining the protein, fibre and lipid content of the initial BSG.
  • the BSG a brewing industry by-product, is the solid fraction (72%- 85% moisture) obtained during the lautering (or mash separation) stage that occurs after the mashing.
  • This by-product is rich in proteins, fibres and lipids, besides several organic compounds as vitamins and antioxidants polyphenols.
  • the BSG due to its moisture content, is easily degraded at temperatures greater than 2 °C by microorganisms, and the process is accelerated by temperature increase.
  • the degradation process causes the destruction of proteins and other organic compounds, forming butyric acid and other compounds with intense bad odours , and the development of fungi .
  • the BSG is used, as it proceeds from the beer production process, in cattle feed, ensuring that its consumption occurs within 3 to 4 days after production.
  • this is a non stabilized product, with minimal commercial value.
  • BSG dehydration processes currently available are the following: a) BSG dehydration to levels of 10% - 15% with a fluidized bed or rotary dryer using hot air in countercurrent . This is an expensive process due to high energy demand, even using energy from co-generation units. b) BSG dehydration first using a screw conical press with sieve (worm extruder) or a travelling screen press for mechanical dewatering followed by thermal dehydration in a convection dryer or through the use of solar energy (U.S. Pat. No. 6,167,736).
  • the fraction rich in fiber is processed in a screw-press, increasing its dry matter content up to 40%, and then burned to produce vapour.
  • the filter press is a device used since the mid-nineteenth century which has undergone numerous developments until reaching the state of the modern membrane filter presses, but has never been applied to the dehydration of BSG, as it proceeds from the beer production process .
  • a filter press consists of a series of plates held in contact through the action of a fixed head plate and a mobile tail plate usually acted by one or more hydraulic cylinders.
  • the modern filters generally use recessed plates, in which a concavity allows the formation of an empty space (filtration chamber) between two consecutive plates.
  • plates have been developed, in which the surface area that forms the filtration chamber is not made of a rigid material, but of a flexible membrane (also called a diaphragm) .
  • a flexible membrane also called a diaphragm
  • a filter of this kind is described in the document U.S. Pat. No. 5,558,773, or a version with modified plates in the U.S. Pat. No. 6,180,002 and the US 2006/0032805.
  • the particular filter used here is based on filter presses with the latest technology but subjected to several changes to allow BSG dehydration. It consists of a membrane filter press and associated vacuum circuit that reduces the pressure inside the filtration chambers and thus promotes the water vaporization below 100 0 C while holding a driving force for the extraction of moisture. Modifications were made to allow the dehydration of BSG as it proceeds from the beer production process, including:
  • the use of a progressive cavity pump 2) Implementation of a modified proportional, integral and derivative control chain (PIDM) .
  • PIDM modified proportional, integral and derivative control chain
  • This control chain was specifically developed to enable the effective control of the pressure generated by the progressive cavity pump, inside the filter. Without such effective control it would not be possible to use the progressive cavity pump coupled to the filter press .
  • the control chain comprises a pressure sensor, two independent proportional-integral- derivative (PID) controllers, a temporizer and a frequency variator, the latter being the actuator that determines the rotational speed of the progressive pump motor and therefore limits the pressure inside the filter.
  • PID proportional-integral- derivative
  • temporizer a temporizer
  • a frequency variator the latter being the actuator that determines the rotational speed of the progressive pump motor and therefore limits the pressure inside the filter.
  • This chain is distinguished from a usual closed loop control chain by using two PID controllers with independent parameterization.
  • PID controllers The need for two independent PID controllers arises from the fact that during the filtration operation there are two distinct sequential stages which can be designated by cake formation and cake consolidation and each of these stages requires a controller (PID) with specific parameterization.
  • PID controller
  • the choice of the controller actuating in a given moment of the process is made via a timer properly parameterized.
  • Figure 1 shows an integrated unit of filtration, compression and vacuum, using an electrical resistance as the heat source for the compression fluid.
  • 9 Lower distributor of the compression and heating cycle, which allows the supply of the hot compression fluid to the filter plates.
  • 10 Centrifugal pump for feeding the compression fluid to the filter plates.
  • FIG. 11 Heater for compression water. Item 11 relates only to figure 1. In Figure 2, it is replaced by items 18 and 19.
  • Figure 1 shows a unit characterized by the use of water heated by an electrical resistance for the heating and compression of the cakes .
  • Figure 2 presents the case for the use of process hot water or low pressure steam produced in a boiler for the same purpose .
  • 12 Upper distributor of the compression and heating cycle. A valve to produce suitable pressure loss, and thereby increase the pressure inside the compression plates, is embodied in it.
  • the pump used is an oil ring vacuum pump. However, other types of pumps can be used, such as aqueous liquid ring pumps. These pumps allow pressure reduction in the filtration chambers (space between two consecutive filter plates) to values of around 50 mbar. Thus in these conditions the water boiling temperature drops to about 40°C.
  • Figure 2 is identical to Figure 1 except differences in the compression fluid heating system, represented in the figure under items 18 and 19.
  • the solids deposit in the filtration chambers originating what is known as the filter cake.
  • the filter cloths preferably from polypropylene fabric, mono-mono filament, with the air porosity of 500 L/dm2.min, cover the plates, coating the membranes and allowing the passage of fluid as the solids are retained at their surface.
  • the fluid with a low solid content, a high polyphenol content and consequently high antioxidant power, is collected through small holes on the edge of the membranes and directed by consecutive channels in the 4 corners of each plate to an external piping system and collected in (8) .
  • the progressive cavity pump (3) feeds the filter (5) , keeping a constant value of the filtration pressure of 3-6 bar preferably 4 bar, until the flow rate of fluid collected in (8) is very low. At this time completion of the filtration step is achieved.
  • the filtration step lasts about 10 minutes. After turning the feed pump (3) off, the isolating valve of the feed channel (4) is closed.
  • the second step of the mechanical dehydration starts: cake compression.
  • a thermal fluid preferably water (up to 120°C) or low pressure steam circulates through the lower distributor (9) , passes through the inner part of the plates (5) and exits through the top, where the upper distributor (12) and their piping lead it back to the heat source (11 and 18) , preferably a heat exchanger (19) or a steam production boiler (18) .
  • a valve at the outlet of the upper distributor (12) creates a pressure drop, increasing the pressure upstream in the circuit, causing membranes' dilatation and consequent cake compression.
  • heat is transferred from the thermal fluid to the solids. This compression step takes place at a pressure of 4-8 bar.
  • the compression pressure must be at least 1 bar higher than the filtration pressure, preferably 3 bar, i.e., at a 4 bar filtration pressure, the compression must take place at 7 bar.
  • the compression fluid is again collected in (8) and added to the filtrate. When the compression fluid flow rate decreases significantly, the compression is completed.
  • the pressure inside the membranes is reduced to 2-3 bar in order to ensure good contact between the heated membranes and the cake surface without compressing it too much.
  • the central filter channel - "core-blow"- is then unblocked.
  • the filtrate exits are closed, the center channel purge valve is opened and compressed air is injected in the chambers through one of the corner channels that communicate with the filtration chambers through the filtrate collecting eyelets .
  • the pressure increases within the chambers due to the compressed air injection and causes the expulsion of the wettest and less consolidated brewer' s spent grain accumulated in the central channel.
  • the required pressure of the compressed air can be between 1 and 3 bar.
  • the duration of this step is usually about 1 minute.
  • the central channel purge valve is closed.
  • the next step is cake blowing.
  • the plate sets that allow for on-line blowing have the filtrate collection eyelets asymmetrically placed in each consecutive plate.
  • the filtrate collection is achieved in the top and bottom right corners and on the other side in the top and bottom left corners. Therefore, by closing the valves of the upper right and lower left filtrate collecting channels, air can be injected under pressure through the upper-left channel, across the cake and exits the system through the bottom right channel .
  • This step lasts for about 5 minutes and allows the removal of some moisture from both the piping and the cake. It also increases cake porosity.
  • air injection valves are closed and the vacuum drying stage starts.
  • the four filtrate output channels are opened; the exit (8) is closed.
  • the collection of air / steam / water starts to be carried out by the vacuum circuit (7).
  • Heating is kept between 60-120 0 C, preferably between 80 0 C and 90 0 C when polypropylene membrane plates are used. If higher temperatures are required (up to 12O 0 C) Ethylene Propylene Diene Monomer (EPDM) membranes and low pressure steam may be used.
  • the condenser (13) cooling fluid is circulated and the vacuum pump, preferably an oil ring vacuum pump (15) is turned on.
  • a reduced pressure of around 15 to 100 mbar (absolute) preferably between 15-50 mbar is applied inside the filtration chambers through the filtrate exits while maintaining the membranes compression pressure at 2-3 bar. With this arrangement, it is possible to vaporize water at temperatures of around 40 0 C.
  • the drying operation is prolonged until the cake reaches the desired moisture values, usually around 15%.
  • the vacuum pump (15) is stopped and the system is vented (8) to restore pressure in the pipes.
  • the compression circuit upper distributor valve is opened, reducing the compression pressure to zero.
  • the thermal fluid circulation is stopped.
  • the filter is opened and the dry cakes are discharged.
  • the membrane plates used in the proposed process have the main body made of polypropylene.
  • the membranes, which can be detachable or welded to the plate, can be made of polypropylene or EPDM according to the required working temperatures.
  • the thickness of the cakes produced should not exceed 2.0 cm, being preferably 1.5 cm.
  • Two membrane plate combinations were developed to be used with BSG: i) In a first combination, all membrane plates are recessed
  • recessed membrane plates have advantages due to the fact that they are easier to handle and provide a better seal for creating vacuum in the filtration chambers .
  • the recessed membrane plates alternate with recessed rigid plates. These rigid recessed plates have several extraction holes evenly distributed on the surface area of the plate (figure 3) . This combination allows the use of higher compression pressures and necessarily involves the use of higher temperatures for the thermal fluid in order to compensate the fact that the heating is carried out only on one side of the cake. Since the rigid plates have a greater number of extraction points spread over the entire surface of the cake, a more effective drying is achieved.
  • Process 2 (alternative process)
  • the alternative process for using the filter press with membrane plates for the dehydration of BSG is to use the filter press only for mechanical dewatering.
  • the mechanical dewatering is carried out through filtration and compression, as previously described in case 1, but with the possibility of operating at higher pressures (up to 50-70 bar) .
  • This procedure requires the strengthening of the structure of the filter and the use of suitable filter plates.
  • the BSG results from low pressure filtration of must (lautering) , resulting in a filtrate (which will lead to beer) and a solid that accumulates in the filter chambers (the BSG) .
  • the filtration cycle is extended by increasing the pressure on the cake up to 50-70 bar, using for example, membrane plates that operate on compressed air, a large amount of exudate, rich in polyphenols, is extracted.
  • this extract cannot be mixed with the filtrate obtained in the low pressure filtration stage, since that would be detrimental to the taste of the beer. This process would save time of filtration and would have a low investment cost for the filtration equipment.
  • the filter for mash separation could also be used for process 1.
  • modifications and upgrades required by the filter equipment stressening of the structure, new membrane plates, installing a vacuum line, installing a pressurized thermal fluid line, etc
  • the process of beer manufacturing would be impaired.
  • the BSG resulting from this mechanical dewatering may then be thermally dried in conventional thermal dryers.
  • This alternative process reduces the humidity of BSG, without spending any thermal energy and the BSG obtained has a moisture content that allows its preservation for a few days, and thus, has added value in the market.
  • the process is not self- sufficient, since it failed to stabilize the BSG for a long period, and thermal drying is still required.
  • This innovative and alternative process described herein produces a stabilized and dried BSG (15% humidity) that maintains all its nutritional characteristics.
  • This process is technically and economically feasible, with a production cost of 50 €/ton of dry BSG, which is considered very competitive as raw material for animal feed.
  • the BSG resulting from this process can be used either in feed for ruminants and non-ruminants, as well as for human consumption, and as a stable raw material for other industries .
  • Studies conducted with BSG obtained from the unit described in this invention suggest that a diet with BSG is beneficial to the animals. For example, it was found that the inclusion of BSG in the diet of young animals being weaned prevent them from suffering from diarrhea.
  • the BSG can also be used by the bakery industry or for biotechnological processes.
  • the dried BSG produced as described herein is chemically and microbiologically stable, it can be stored for a long period of time (several years) before being marketed or used in is multiple applications and therefore there is a clear economic recovery from this process .
  • Exudates The exudate collected in the steps of filtering and compression is a fluid rich in polyphenols, which, depending on the pressures used and the type of grain used in the manufacture of beer, may have a polyphenol content of between 20 and 300 ppm.
  • This by-product, obtained in this invention, from the process of dehydration of BSG, may be applicable to the pharmaceutical and cosmetic industries, since polyphenols are well-known antioxidants .

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Polymers & Plastics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Zoology (AREA)
  • Animal Husbandry (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Food Science & Technology (AREA)
  • Botany (AREA)
  • General Engineering & Computer Science (AREA)
  • Mycology (AREA)
  • Molecular Biology (AREA)
  • Birds (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Physiology (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Biotechnology (AREA)
  • Wood Science & Technology (AREA)
  • Filtration Of Liquid (AREA)
  • Medicines Containing Plant Substances (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne un procédé et le matériel correspondant, capable de déshydrater la drêche de brasserie, depuis entre 72 et 85% jusqu'à 15% d'humidité, permettant d'obtenir un produit stabilisé avec la même teneur en protéines, fibres et lipides. Le procédé de déshydratation comprend plusieurs étapes, dont deux sont mécaniques (filtration et expression membranaire) et au moins une étape finale qui consiste en un séchage sous vide au moyen d'eau chaude ou de vapeur basse pression en tant que source de chaleur. L'énergie pour le procédé est disponible à coût nul dans l'industrie brassicole, grâce à l'utilisation de l'eau chaude de fabrication, ou de la vapeur basse pression provenant des unités de cogénération. La drêche de brasserie déshydratée est un produit stabilisé et peut être utilisée comme aliments pour humains et pour animaux, ruminants et non ruminants, comme matière première pour des applications biotechnologiques et pharmaceutiques.
PCT/PT2010/000016 2009-04-06 2010-04-05 Procede integre de filtration de dreche seche de brasserie WO2010117288A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
PT104494 2009-04-06
PT104494A PT104494B (pt) 2009-04-06 2009-04-06 Unidade integrada de filtração, compressão e vácuo para processo integrado de filtracção, compressão e secagem sob vácuo do drêche da indústria cervejeira, e respectiva aplicação dos produtos finais

Publications (2)

Publication Number Publication Date
WO2010117288A1 true WO2010117288A1 (fr) 2010-10-14
WO2010117288A8 WO2010117288A8 (fr) 2014-10-16

Family

ID=42026531

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/PT2010/000016 WO2010117288A1 (fr) 2009-04-06 2010-04-05 Procede integre de filtration de dreche seche de brasserie

Country Status (2)

Country Link
PT (1) PT104494B (fr)
WO (1) WO2010117288A1 (fr)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130055622A1 (en) * 2011-09-01 2013-03-07 Akbev, Llc Spent grain fuel product and process
CN104048495A (zh) * 2014-06-16 2014-09-17 无锡全邦能源科技有限公司 粮油压榨过程中的余热回收系统
US20150114914A1 (en) * 2012-04-19 2015-04-30 Outotec (Finland) Oy Method for filtering a suspension and recess plate
US20170121619A1 (en) * 2011-09-01 2017-05-04 Akbev Group, Llc Spent grain fuel product and process
US20170190994A1 (en) * 2011-09-01 2017-07-06 Akbev Group, Llc High Protein Organic Materials as Fuel and Processes for Making the Same
BE1024957B1 (nl) * 2017-08-14 2018-08-23 Anheuser-Busch Inbev S.A. Proces voor microbiële stabilisatie van bierbostel, microbiologisch gestabiliseerd bierbostel en toepassing daarvan
WO2019009741A1 (fr) * 2017-07-03 2019-01-10 Instituto Superior Técnico Procédé de valorisation de marc de tomate
WO2019034567A1 (fr) * 2017-08-14 2019-02-21 Anheuser-Busch Inbev S.A. Procédé de stabilisation microbienne de drêches de brasserie, drêches de brasserie stabilisées microbiologiquement et leur utilisation
EP3459359A1 (fr) * 2017-09-25 2019-03-27 Cordeiro & Peça Lda. Procédé de déshydratation et de granulation de céréales de brasserie
EP3617301A1 (fr) * 2018-08-29 2020-03-04 Heineken Supply Chain B.V. Membrane de filtre à maische
US10982162B2 (en) 2011-09-01 2021-04-20 Akbev Group, Llc High protein organic materials as fuel and processes for making the same
WO2021080450A1 (fr) 2019-10-21 2021-04-29 БиоБо ГмбХ Suspension de protéines issue de drêche de brasserie, procédé et installation de production
WO2021201711A1 (fr) 2020-04-02 2021-10-07 "Биобо Гмбх" Produit protéiné issus de drêche de brasserie et procédé de production
US11441090B2 (en) 2011-09-01 2022-09-13 Akbev Group, Llc High protein organic materials as fuel and processes for making the same
US11866669B2 (en) 2011-09-01 2024-01-09 Akbev Group, Llc High protein organic materials as fuel and processes for making the same

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107126738A (zh) * 2017-07-17 2017-09-05 景津环保股份有限公司 隔膜滤板压榨空气再用于反吹滤饼装置及方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5558773A (en) * 1992-12-04 1996-09-24 Bertrams Dehydrat Ag Method for producing and drying a filter cake, while avoiding entering of the filter cake into a thermoplastic phase
EP0978304A2 (fr) * 1998-08-03 2000-02-09 United States Filter Corporation Filtre-presse avec une alternance de plaques pour chambre à membrane et de plaques pour chambre de filtration
US20060032805A1 (en) * 2002-09-13 2006-02-16 Hildebrant Mark W Heating plate for vacuum filter press
DE202006007248U1 (de) * 2006-05-04 2007-09-13 Klinkau Besitzgesellschaft Mbh Antistatische Kammerfilterplatte

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5558773A (en) * 1992-12-04 1996-09-24 Bertrams Dehydrat Ag Method for producing and drying a filter cake, while avoiding entering of the filter cake into a thermoplastic phase
EP0978304A2 (fr) * 1998-08-03 2000-02-09 United States Filter Corporation Filtre-presse avec une alternance de plaques pour chambre à membrane et de plaques pour chambre de filtration
US20060032805A1 (en) * 2002-09-13 2006-02-16 Hildebrant Mark W Heating plate for vacuum filter press
DE202006007248U1 (de) * 2006-05-04 2007-09-13 Klinkau Besitzgesellschaft Mbh Antistatische Kammerfilterplatte

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
EL-SHAFEY ET AL: "Dewatering of brewer's spent grain using a membrane filter press: A pilot plant study", SEPARATION SCIENCE AND TECHNOLOGY, DEKKER, NEW YORK, NY, US LNKD- DOI:10.1081/SS-200028775, vol. 39, no. 14, 1 January 2004 (2004-01-01), pages 3237 - 3261, XP009137801, ISSN: 0149-6395 *
EL-SHAFEY, E.I.; GAMEIRO, M.; CORREIA, P.; DE CARVALHO, J.: "Dewatering of brewer's spent grain using a membrane filter press: a pilot plant study", SEPARATION SCIENCE AND TECHNOLOGY, 2004

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130055622A1 (en) * 2011-09-01 2013-03-07 Akbev, Llc Spent grain fuel product and process
US11441090B2 (en) 2011-09-01 2022-09-13 Akbev Group, Llc High protein organic materials as fuel and processes for making the same
US9447354B2 (en) * 2011-09-01 2016-09-20 Akbev Llc Spent grain fuel product and process
US10982162B2 (en) 2011-09-01 2021-04-20 Akbev Group, Llc High protein organic materials as fuel and processes for making the same
US20170190994A1 (en) * 2011-09-01 2017-07-06 Akbev Group, Llc High Protein Organic Materials as Fuel and Processes for Making the Same
US20170121619A1 (en) * 2011-09-01 2017-05-04 Akbev Group, Llc Spent grain fuel product and process
US10781388B2 (en) 2011-09-01 2020-09-22 Akbev Group, Llc High protein organic materials as fuel and processes for making the same
US11866669B2 (en) 2011-09-01 2024-01-09 Akbev Group, Llc High protein organic materials as fuel and processes for making the same
US10364400B2 (en) 2011-09-01 2019-07-30 Akbev Group, Llc Spent grain fuel product and process
US20150114914A1 (en) * 2012-04-19 2015-04-30 Outotec (Finland) Oy Method for filtering a suspension and recess plate
US9776109B2 (en) * 2012-04-19 2017-10-03 Outotec (Finland) Oy Method for filtering a suspension and recess plate
CN104048495A (zh) * 2014-06-16 2014-09-17 无锡全邦能源科技有限公司 粮油压榨过程中的余热回收系统
WO2019009741A1 (fr) * 2017-07-03 2019-01-10 Instituto Superior Técnico Procédé de valorisation de marc de tomate
WO2019034567A1 (fr) * 2017-08-14 2019-02-21 Anheuser-Busch Inbev S.A. Procédé de stabilisation microbienne de drêches de brasserie, drêches de brasserie stabilisées microbiologiquement et leur utilisation
BE1024957B1 (nl) * 2017-08-14 2018-08-23 Anheuser-Busch Inbev S.A. Proces voor microbiële stabilisatie van bierbostel, microbiologisch gestabiliseerd bierbostel en toepassing daarvan
EP3459359A1 (fr) * 2017-09-25 2019-03-27 Cordeiro & Peça Lda. Procédé de déshydratation et de granulation de céréales de brasserie
EP3617301A1 (fr) * 2018-08-29 2020-03-04 Heineken Supply Chain B.V. Membrane de filtre à maische
WO2020046122A1 (fr) * 2018-08-29 2020-03-05 Heineken Supply Chain B.V. Membrane de filtre à maische
DE112019007829T5 (de) 2019-10-21 2022-07-07 BioBo GmbH Proteinsuspension aus Biertreiber, Verfahren und Vorrichtung zu deren Erzeugung
WO2021080450A1 (fr) 2019-10-21 2021-04-29 БиоБо ГмбХ Suspension de protéines issue de drêche de brasserie, procédé et installation de production
US11576401B2 (en) 2019-10-21 2023-02-14 BioBo GmbH Protein suspension from brewer's grains, method and apparatus for obtaining same
WO2021201711A1 (fr) 2020-04-02 2021-10-07 "Биобо Гмбх" Produit protéiné issus de drêche de brasserie et procédé de production
DE112020006997T5 (de) 2020-04-02 2023-01-12 BioBo GmbH Proteinöses erzeugnis aus biertreber und verfahren zu dessen erzeugung
US11712048B2 (en) 2020-04-02 2023-08-01 BioBo GmbH Protein product obtained from brewer's grains and its production method

Also Published As

Publication number Publication date
PT104494B (pt) 2010-03-25
PT104494A (pt) 2009-08-14
WO2010117288A8 (fr) 2014-10-16

Similar Documents

Publication Publication Date Title
WO2010117288A1 (fr) Procede integre de filtration de dreche seche de brasserie
US5558773A (en) Method for producing and drying a filter cake, while avoiding entering of the filter cake into a thermoplastic phase
CN103822454B (zh) 基于机械式蒸汽再压缩的湿粕干燥系统及干燥工艺
EP1800077A1 (fr) Appareil de sechage et procede d'utilisation et de fabrication associe
FI72256C (fi) En foerbaettrad metod foer behandling av boskapsfoderprodukter och en anlaeggning foer genomfoerande av metoden.
El-Shafey et al. Dewatering of brewer’s spent grain using a membrane filter press: a pilot plant study
AU2014261043B2 (en) Method for ultra-dehydrating thickened or pasty biomass products, and equipment for implementing the method
US20120005916A1 (en) Process for drying brewer's spent grains
CN102080922A (zh) 一种固体物料干燥方法及系统
WO1984001884A1 (fr) Procede de production de fourrage et de graisse a partir de matieres brutes animals
CN107594547A (zh) 一种以大豆分离蛋白湿豆渣为原料生产大豆纤维粉的装置
EA006013B1 (ru) Способ и установка для переработки зерна
RU2595152C1 (ru) Линия производства растительного масла
CN1078866A (zh) 啤酒糟粕蛋白饲料加工工艺及设备
CN109836028A (zh) 一种畜禽粪便两级连续深度脱水处理的一体化系统
CN107289770A (zh) 一种用于生产有机废水处理催化剂的干燥工艺及设备
Hutchins Continuous solvent extraction of soybeans and cottonseed
RU198439U1 (ru) Экструдер с вакуумной камерой
CN105423732A (zh) 聚酯再生瓶片连续干燥系统
RU2120962C1 (ru) Способ получения растительного масла из высокомасличного сырья и технологическая линия для осуществления способа
CN110089636A (zh) 一种鲜酒糟制饲料的烘干工艺
CN219518276U (zh) 一种大豆纤维粉的节能生产装置
RU2693046C1 (ru) Способ управления процессом переработки масличных семян в биодизельное топливо
RU2773436C1 (ru) Способ управления линией производства растительного масла
CN219836228U (zh) 一种提取液加工装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10720047

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 10720047

Country of ref document: EP

Kind code of ref document: A1