DK176496B1 - Plant for enzymatic hydrolysis of a batch of animal or vegetable constituents and process for using the plant - Google Patents
Plant for enzymatic hydrolysis of a batch of animal or vegetable constituents and process for using the plant Download PDFInfo
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- DK176496B1 DK176496B1 DK200301878A DKPA200301878A DK176496B1 DK 176496 B1 DK176496 B1 DK 176496B1 DK 200301878 A DK200301878 A DK 200301878A DK PA200301878 A DKPA200301878 A DK PA200301878A DK 176496 B1 DK176496 B1 DK 176496B1
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- 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
- A23J3/00—Working-up of proteins for foodstuffs
- A23J3/30—Working-up of proteins for foodstuffs by hydrolysis
- A23J3/32—Working-up of proteins for foodstuffs by hydrolysis using chemical agents
- A23J3/34—Working-up of proteins for foodstuffs by hydrolysis using chemical agents using enzymes
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Description
DK 176496 B1DK 176496 B1
Opfindelsen angår et anlæg til enzymatisk hydrolysering af en reaktionsblanding omfattende en batch i hvert fald delvist hydrolyserbare animalske eller vegetabilske bestanddele eller en blanding af disse bestanddele, og af den art, der omfatter 5 en reaktor, der har en øvre sektion med en fødeåbning, en midtersektion , og en bundsektion med en bundåbning, et røreværk til at bestryge reaktionsblandingen i reaktoren 2's midtersektion og bundsektion, og en pumpe til at lede et delvolumen af reaktionsblandingen ud gennem reaktorens 10 bundåbning, når pumpen er i drift,The invention relates to a plant for enzymatically hydrolyzing a reaction mixture comprising at least a batch of at least partially hydrolyzable animal or vegetable components or a mixture of these components, and of the kind comprising a reactor having an upper section having a feed opening, a a bottom section, and a bottom section with a bottom opening, a stirrer for coating the reaction mixture in the middle section and bottom section of the reactor 2, and a pump for passing a partial volume of the reaction mixture through the bottom opening of the reactor 10 when the pump is in operation;
Opfindelsen angår også en fremgangsmåde til anvendelse af anlægget.The invention also relates to a method of using the plant.
15 Store dele af levnedsmiddelindustrien, såsom slagterier og færdigvareindustrien, producerer store mængder affaldsprodukter ved oparbejdning af f.eks. kød, fisk og fjerkræ. Sådanne affaldsprodukter afskaffes ved forbrænding eller kan i et vist omfang forarbejdes og genanvendes til f.eks. benmel eller 20 dyrefoder.15 Large parts of the food industry, such as slaughterhouses and the finished goods industry, produce large quantities of waste products by processing e.g. meat, fish and poultry. Such waste products are disposed of by incineration or can to some extent be processed and reused for e.g. bone meal or 20 animal feed.
Den hydrolyserbare del af affaldsprodukterne kan imidlertid hydrolyseres og udnyttes til fremstilling af f.eks. aromater, fonds og supper.However, the hydrolyzable portion of the waste products can be hydrolyzed and utilized to produce e.g. aromatics, fondants and soups.
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En kontinuerlig hydrolyse kræver store pladskrævende procesanlæg, store investeringer og store råvaremængder for at kunne udnyttes rentabelt.Continuous hydrolysis requires large space-intensive processing plants, large investments and large quantities of raw materials in order to be utilized profitably.
30 Fra US 4,379,083 kendes et mindre kontinuerligt anlæg til fremstilling af blodplasmafraktioner, hvor blodplasma, buffer og udfældningsmiddel reageres under pH og temperaturkontrol i en reaktor under kraftig omrøring i reaktorens midterzone. Et delvolumen af reageret reaktionsblanding udtages løbende til 35 særskilt fraktionering i f.eks. proteinfraktioner. Dette udtagne volumen erstattes simultant med nye reaktanter, der DK 176496 B1 tilføres ved reaktorens top, for at sikre bedst mulig tilblanding og opblanding af den til enhver tid eksisterende samlede reaktionsblanding over hele reaktorens volumen.From US 4,379,083, a smaller continuous plant for producing blood plasma fractions is known in which blood plasma, buffer and precipitant are reacted under pH and temperature control in a reactor under vigorous stirring in the center zone of the reactor. A partial volume of reacted reaction mixture is taken continuously for 35 separate fractionation in e.g. protein fractions. This withdrawn volume is simultaneously replaced with new reactants, which are added at the top of the reactor to ensure the best possible mixing and mixing of the total reaction mixture existing at all times of the entire reactor volume.
5 Ved mindre eller små råvaremængder kan mindre batchanlæg fordelagtigt benyttes.5 For smaller or small quantities of raw materials, smaller batch plants can advantageously be used.
Kendte små batchanlæg består af en lodret reaktor med en varmekappe og en omrører, der holder reaktionsblandingen 10 opblandet. Reaktoren har typisk en konisk bund med et bundudtag, gennem hvilket den færdighydrolyserede masse, dvs. blandingen af hydrolysat, fedt og ben udtages på en gang til efterfølgende separation i f.eks. en dekanter. En af ulemperne ved disse kendte anlæg er, at bundudtaget nemt stopper til, da 15 benene pakker sig sammen i bundudtaget, mens reaktoren tømmes.Known small batch plants consist of a vertical reactor with a heating jacket and a stirrer which keeps the reaction mixture 10 mixed. The reactor typically has a tapered bottom with a bottom outlet through which the finished hydrolyzed mass, i.e. the mixture of hydrolyzate, fat and bone is taken out at once for subsequent separation in e.g. a decanter. One of the drawbacks of these known plants is that the bottom outlet easily stops as the 15 legs compress into the bottom outlet while the reactor is emptied.
I nogle batchreaktorer er dette problem søgt løst ved hjælp af en snegl, der roterer over bundudtaget. Sneglen løfter i et vist omfang benene væk fra bundudtaget, men nedsætter kun 20 delvist risikoen for tilstopning af bundudtaget, da sneglen roterer forholdsvis langsomt.In some batch reactors, this problem has been solved by means of a auger rotating over the bottom outlet. To a certain extent, the auger lifts its legs away from the bottom outlet, but only partially reduces the risk of clogging the bottom outlet as the auger rotates relatively slowly.
Som følge af batchanlæggets driftproblemer genanvendes de hydrolyserbare affaldsprodukter kun i beskedent omfang.Due to the operating problems of the batch plant, the hydrolysable waste products are only recycled to a limited extent.
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Affaldsprodukterne fra kødforarbejdning er en umiddelbar tilgængelig råvare, som endda kan være bekostelig at slippe af med. Udnyttelse af dette affald til fremstilling af et hydrolysat, der kan anvendes som f.eks. suppe, fond og 30 aromakoncentrat, kan derfor udgøre en fordelagtig indtægtskilde, såfremt driften af batchanlægget kan optimeres.The waste products from meat processing are an immediately available raw material that can even be expensive to get rid of. Utilization of this waste to produce a hydrolyzate which can be used, e.g. Soup, foundation and 30 aroma concentrate can therefore constitute an advantageous source of revenue if the operation of the batch plant can be optimized.
I et første aspekt ifølge den foreliggende opfindelse anvises et batchanlæg til enzymatisk fremstilling af et hydrolysat, 35 hvor batchanlægget har en simpel, driftsikker konstruktion, og er nemmere at vedligeholde og anvende end hidtil kendt.In a first aspect of the present invention there is provided a batch plant for the enzymatic preparation of a hydrolyzate, wherein the batch plant has a simple, reliable construction and is easier to maintain and use than heretofore known.
DK 176496 B1 I et andet aspekt ifølge den foreliggende opfindelse anvises et batchanlæg til udnyttelse af enzymatisk hydrolyserbare biprodukter fra levnedsmidler og levnedmiddeloparbejdning.In another aspect of the present invention there is provided a batch plant utilizing enzymatically hydrolysable food by-products and food processing.
5 Det nye og særegne hvorved dette opnås ifølge opfindelsen består i, at anlægget yderligere omfatter en i eller tæt ved bundåbningen tilvejebragt omrører.The new and unique feature of this invention is that the system further comprises a stirrer provided in or near the bottom opening.
SS
I kendte batchreaktorer til tilsvarende formål har partikulært 10 materiale med stor massefylde en tendens til at lejre sig i og omkring reaktorers bundåbning, som derfor kan være vanskelig at holde åben under f.eks. reaktortømningen. Denne ulempe afhjælpes på simpel måde ved med pumpen at tilvejebringe det fornødne sug til at opretholde et kontinuerligt flow ud gennem 15 bundåbningen. Det dynamiske tryk, som pumpen skal yde, varierer afhængig af reaktorens dimensioner og reaktionsblandingens sammensætning og kan fastlægges empirisk.In known batch reactors for similar purposes, particulate matter of high density tends to settle in and around the bottom opening of the reactors, which can therefore be difficult to keep open during e.g. reactor emptying. This drawback is simply remedied by providing the pump with the suction required to maintain a continuous flow through the bottom opening. The dynamic pressure to be applied by the pump varies depending on the dimensions of the reactor and the composition of the reaction mixture and can be determined empirically.
Når omrøreren holder partikulært materiale i 20 reaktionsblandingen i kontinuerlig dispersion i området omkring bundåbningen, vanskeliggøres pumpens arbejde ikke af ophobninger af partikulært materiale i og omkring bundåbningen.When the stirrer holds particulate material in the reaction mixture in continuous dispersion in the area around the bottom opening, the work of the pump is not hampered by accumulations of particulate matter in and around the bottom opening.
Under hydrolysen spaltes proteinholdige bestanddele i mindre 25 peptider og aminosyrer. Når reaktionsblandingen opvarmes udskilles fedt og lipider, som lejrer sig ovenpå vandfasen, som en fedtfase øverst i reaktoren. Fedtfasens omfang vokser under den varme enzymatiske reaktion efterhånden som fedtet smelter og olier og lipider fraskilles.During the hydrolysis, proteinaceous components are cleaved into smaller peptides and amino acids. When the reaction mixture is heated, grease and lipids that settle on top of the aqueous phase are separated as a fat phase at the top of the reactor. The extent of the fat phase grows during the hot enzymatic reaction as the fat melts and oils and lipids are separated.
3030
Typen af omrører og dennes rotationshastighed vælges således, at fedtfasen i videst muligt omfang bevares intakt under omrørerens rotation og pumpens sugning.The type of agitator and its rotational speed are chosen such that the fat phase is kept intact as far as possible during the rotation of the agitator and the suction of the pump.
35 I en foretrukken udførelsesform for anlægget ifølge den foreliggende opfindelse er omrøreren en blandepropel, der kan DK 176496 B1 holde i hvert fald det delvolumen reaktionsblanding, der er beliggende i området nær bundåbningen kontinuerligt opblandet. Hydrolyserbart materiale vil naturligt som følge af gravitation kontinuerligt søge mod bundsektionen og indgå i dette 5 delvolumen.In a preferred embodiment of the system of the present invention, the stirrer is a mixing propeller capable of continuously mixing at least the partial volume of reaction mixture located in the region near the bottom opening. Hydrolyzable material will naturally, as a result of gravity, continuously search towards the bottom section and be included in this 5 part volume.
Alternativt kan omrøreren være udformet som en roterende kniv, for således også at kunne neddele større partikler i reaktionsblandingen ved bundåbningen.Alternatively, the stirrer may be designed as a rotating knife, so as to be able to also divide larger particles into the reaction mixture at the bottom opening.
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Andre former for omrørere, såsom f.eks. en skiveomrører med vinger eller en bladomrører, er omfattet indenfor opfindelsens ramme.Other types of agitators such as e.g. a blade stirrer with wings or a blade stirrer is included within the scope of the invention.
15 En meget hurtigtgående omrører vil være tilbøjelig til at sætte hele reaktionsblandingen i rotation omkring sin akse. Hvis reaktionsblandingen rejser sig langs reaktorens indervæg vil dette sammen med omrørerens sugevirkning i aksialretningen kunne føre til dannelse af en sugetragt. En sådan sugetragt vil 20 emulgere fedtfase og vandfase, hvilket er uønsket. Omrørerens rotationshastighed kalibreres derfor til at holde et delvolumen reaktionsblanding mellem bundåbningen og fedtfasen i dispergeret opblanding, uden at fedtfasen opblandes i vandfasen.A very fast stirrer will tend to rotate the entire reaction mixture around its axis. If the reaction mixture rises along the inner wall of the reactor, this, together with the suction action of the stirrer in the axial direction, can lead to the formation of a suction funnel. Such a suction funnel will emulsify fat phase and water phase, which is undesirable. The rotational speed of the agitator is therefore calibrated to maintain a partial volume of reaction mixture between the bottom opening and the fat phase in dispersed mixture without mixing the fat phase into the aqueous phase.
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En god kontakt mellem substrat, i form af hydrolyserbare bestanddele, såsom kødben fra kødaffald, og enzym vil bevirke at reaktionen kan forløbe under optimale reaktionsbetingelser.A good contact between substrate, in the form of hydrolyzable constituents such as meat offal, and enzyme will allow the reaction to proceed under optimal reaction conditions.
30 I dette øjemed omfatter anlægget ifølge den foreliggende opfindelse en recirkulationsledning med en første ende, der strækker sig i hvert fald et stykke op gennem reaktorens bundsektion mellem omrøreren og reaktorens indervæg. Gennem denne recirkulationsledning kan pumpen pumpe reaktionsblanding 35 fra reaktorens bundåbning og tilbage til reaktoren, og DK 176496 B1 omroreren og pumpen kan holde reaktionsblandingen i konstant bevægelse.To this end, the system of the present invention comprises a first-end recirculation line extending at least some distance through the bottom section of the reactor between the stirrer and the inner wall of the reactor. Through this recirculation line, the pump can pump reaction mixture 35 from the bottom opening of the reactor and back to the reactor, and the stirrer and pump can keep the reaction mixture in constant motion.
Herved opnås en bedre omrøringsintensitet, opblandingshastighed 5 og varmetransmission end i kendte batchreaktorer. Den ønskede gode kontakt mellem enzym og substrat giver optimal reaktionshastighed. Desuden hindres reaktorens bundåbning i at tilstoppe.This results in a better stirring intensity, mixing speed 5 and heat transmission than in known batch reactors. The desired good contact between enzyme and substrate provides optimal reaction rate. In addition, the bottom opening of the reactor is prevented from clogging.
10 Væskestrømningerne i recirkulationsledningen kan fordelagtigt styres ved hjælp af en første ventil i recirkulationsledningens første ende og en anden ventil i recirkulationsledningens anden ende.Advantageously, the fluid flows in the recirculation line can be controlled by a first valve at the first end of the recirculation line and a second valve at the second end of the recirculation line.
15 Recirkuleret reaktionsblånding passerer gennem den første åbne ventil i et første tidsinterval, f.eks. svarende til den ønskede hydrolysetid. Når dette første tidsinterval er forløbet, lukkes den første ventil.Recycled reaction mixing passes through the first open valve for a first time interval, e.g. corresponding to the desired hydrolysis time. When this first time interval has elapsed, the first valve is closed.
20 Den anden ventil holdes lukket i hele det første tidsinterval og i en efterfølgende faseadskillelsesperioden, hvor en faseadskillelse i fedtfase, vandig fase og fast fase kan finde sted i reaktionsblandingen.The second valve is kept closed throughout the first time interval and during a subsequent phase separation period where a phase separation in fat phase, aqueous phase and solid phase can take place in the reaction mixture.
25 Den anden ventil åbnes dernæst og faserne aftappes successivt via reaktorens bundåbning ud gennem recirkulationsledningens anden ende. Først aftappes den vandige fase, dernæst aftappes fedtfasen, og sluttelige aftappes en fast fase, der i hovedsagen .består af ben, benpartikler og andet ikke 30 hydrolyserbart partikulært materiale og restbestanddele.The second valve is then opened and the phases are successively discharged via the bottom opening of the reactor through the other end of the recirculation line. First, the aqueous phase is then drained, then the fat phase is drained, and finally a solid phase which consists essentially of bones, bone particles and other non-hydrolysable particulate matter and residual components is drained.
Den faste fase fungerer under aftapningen af de ovenstående flydende faser som et filter og tilbageholder de urenheder, der måtte være i de flydende faser. Den aftappede vandige fase kan 35 have et lille indhold af fedt og lipider, og kan derfor passeres videre gennem en fedtskilletank.The solid phase acts during the bottling of the above liquid phases as a filter and retains any impurities that may be in the liquid phases. The bottled aqueous phase can have a low content of fat and lipids and can therefore be passed on through a fat separation tank.
DK 176496 B1DK 176496 B1
En lille del af fedtet vil under aftapningen af fedtfasen lægge sig som restfedt på ben og partikulært materiale i den faste fase. Dette restfedt kan udvaskes fra den faste fase, såfremt restfedtet ønsket genanvendt.A small portion of the fat, during the bottling phase, will settle as residual fat on bone and particulate matter in the solid phase. This residual fat can be leached from the solid phase if the residual fat is desired to be recycled.
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Fedtfasen kan med anlægget ifølge den foreliggende opfindelse fordelagtigt holdes intakt udenfor omrørerens aktionsfelt, når recirkulationsledningens første ende er udformet med en afskærmning, der strækker sig i et plan vinkelret på omrørerens 10 rotationsakse, således at den recirkulerede reaktionsblanding kan tvangsstyres ind mod reaktorens midte til fornyet kontakt med omrøreren.The grease phase can advantageously be kept intact outside the agitator's field of action with the apparatus of the present invention when the first end of the recirculation line is formed with a shield extending perpendicular to the axis of rotation of the agitator 10 so that the recycled reaction mixture can be forced into the reactor center again. contact with the stirrer.
Når afskærmningens har en længde, der er større end eller lig 15 med recirkulationsledningens diameter, kan den recirkulerede reaktionsblanding på simpel måde hindres i, som følge af pumpetrykket, at presses opad i reaktoren. Fedtfasen kan derfor bevares intakt i hele den første tidsperiode.When the shielding has a length greater than or equal to the diameter of the recirculation line, the recycled reaction mixture can simply be prevented from being forced upwards in the reactor due to the pump pressure. The fat phase can therefore be kept intact throughout the first period of time.
20 I en alternativt udførelsesform for den foreliggende opfindelse kan recirkulationsledningens første ende være bøjet i en vinkel på mellem 70° og 110°, foretrukket mellem 75° og 105° men især mellem 80° og 100°, for således at sende den recirkulerede reaktionsblanding tangentielt ind i reaktoren.In an alternative embodiment of the present invention, the first end of the recirculation line may be bent at an angle of between 70 ° and 110 °, preferably between 75 ° and 105 ° but especially between 80 ° and 100 °, so as to send the recycled reaction mixture tangentially into the reactor.
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Reaktoren kan yderligere omfatte et over omrøreren lokaliseret røreværk til at holde en yderligere del af reaktionsblandingen i opblanding. Et sådant røreværk skal anbringes i reaktoren på en sådan måde, at fedtfasen på reaktionsblandingens overflade 30 ikke berøres. Desuden må røreværket ikke danne en sugetragt eller medvirke til at øge omrørerens sugetragt.The reactor may further comprise a stirrer located above the stirrer to keep an additional portion of the reaction mixture in admixture. Such a stirrer must be placed in the reactor in such a way that the fat phase on the surface of the reaction mixture is not touched. In addition, the agitator must not form a suction funnel or assist in increasing the suction funnel.
Anlægget og fremgangsmåden vil blive mere detaljeret beskrevet i det følgende under henvisning til den ledsagende tegning og 35 eksemplet, hvor DK 176496 B1 fig. 1 viser et langsgående snit gennem et tomt anlæg ifølge den foreliggende opfindelse, fig. 2 viser samme i et indledende hydrolysetrin, hvor 5 reaktoren er fyldt med en batch reaktionsblanding, og fig. 3 viser samme, hvor den hydrolyserede reaktionsblanding ses efter faseseparation og under aftapning af vandigt hydrolysat.The plant and method will be described in more detail in the following with reference to the accompanying drawing and the example in which DK 176496 B1 FIG. 1 is a longitudinal section through an empty plant according to the present invention; FIG. Figure 2 shows the same in an initial hydrolysis step where the reactor is filled with a batch reaction mixture; Figure 3 shows the same where the hydrolyzed reaction mixture is seen after phase separation and during draining of aqueous hydrolyzate.
10 I det følgende antages, at det i fig. 1, 2og 3 viste batchanlæg 1 anvendes til proteolytisk hydrolyse af en blanding af vand og neddelte kødben.10 In the following, it is assumed that in FIG. 1, 2 and 3, batch plant 1 is used for proteolytic hydrolysis of a mixture of water and divided meat bones.
15 Anlægget 1 består af en cylindrisk reaktor 2 med et dæksel 3. Reaktoren 2, der typisk vil være en tank 2 af syrefast rustfrit stål, er indkapslet i en varmekappe 4, om hvilken en varmeisolerende kappe 5 er anbragt. Dækslet 3 er her vist at være et simpelt dæksel 3 med et isolerende dække 6. Når 20 reaktoren 2 skal fyldes gennem fødeåbningen 7, løftes dækslet af, og reaktoren fyldes med en batch reaktionsblanding bestående af vand og kødben. Enzymet tilsættes enten med det samme eller efter at reaktionsblandingen er opvarmet til hydrolysetemperaturen.The plant 1 consists of a cylindrical reactor 2 with a cover 3. The reactor 2, which will typically be an acid-resistant stainless steel tank 2, is encapsulated in a heat jacket 4, about which a heat insulating jacket 5 is arranged. The cover 3 is shown here to be a simple cover 3 with an insulating cover 6. When the reactor 2 is to be filled through the feed opening 7, the cover is lifted off and the reactor filled with a batch reaction mixture of water and meat bone. The enzyme is added either immediately or after the reaction mixture is heated to the hydrolysis temperature.
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Reaktoren 2 har en konisk bundsektion 8 med en bundåbning 9, der med et udløbsrør 10 er forbundet til en pumpe 11, her som eksempel en centrifugalpumpe.The reactor 2 has a tapered bottom section 8 with a bottom opening 9 connected to a pump 11 by an outlet pipe 10, here for example a centrifugal pump.
30 Umiddelbart over bundåbningen 9 er anbragt en omrører 12, i form af en blandepropel 12 til at holde reaktionsblandingen i rotation over bundåbningen 9. Reaktoren 2 har desuden et røreværk 13. Røreværket 13 er i fig. 1 som eksempel vist at være en stakit omrører, der drives af en ekstern motor 14 og 35 bestryger et stort delvolumen reaktionsblanding i reaktoren 2's midtersektion 15 og bundsektion 8.Immediately above the bottom opening 9 is arranged a stirrer 12, in the form of a mixing propeller 12, to keep the reaction mixture in rotation over the bottom opening 9. The reactor 2 further has a stirrer 13. The stirrer 13 is shown in FIG. 1, as an example, shown to be a picket stirrer driven by an external motor 14 and 35 coating a large volume of reaction mixture in the center section 15 and bottom section 8 of the reactor 2.
DK 176496 B1DK 176496 B1
Pumpen 11 pumper reaktionsblanding 23 fra reaktoren 2's bundåbning 9 ud gennem udløbsrøret 10 og videre ud i recirkulationsledningen 16, der har en første ende 17 med en første ventil 18, og en anden ende 19 med en anden ventil 20, 5 der har en udløbsåbning 27. Recirkulationsledningen 16's første ende har en øvre åbning 21, der skærmes med en afskærmning 22 til at dirigere strømmen af recirkuleret reaktionsblanding ind over omrøreren 12.The pump 11 pumps reaction mixture 23 from the bottom opening 9 of the reactor 2 through the outlet pipe 10 and further out into the recirculation line 16 having a first end 17 with a first valve 18 and a second end 19 with a second valve 20, 5 having an outlet opening 27 The first end of the recirculation line 16 has an upper opening 21 which is shielded by a shield 22 to direct the flow of recycled reaction mixture over the stirrer 12.
10 i fig. 2 ses et anlæg 1 ifølge opfindelsen fyldt med reaktionsblanding 23 og enzym. Reaktionsblandingen 23 er opvarmet og en fedtfase 2 4 har udskilt sig på overfladen af reaktionsblandingen 23's vandfase 25, i hvilken benstykker 26 ses dispergeret ved hjælp af henholdsvis røreværket 13 og 15 omrøreren 12. Den første ventil 18 er åben og den anden ventil 20 er lukket.10 in FIG. 2 shows a plant 1 according to the invention filled with reaction mixture 23 and enzyme. The reaction mixture 23 is heated and a fat phase 24 has separated on the surface of the aqueous phase 25 of the reaction mixture 23, in which leg pieces 26 are dispersed by the agitator 13 and stirrer 12. The first valve 18 is open and the second valve 20 is closed. .
Omrøreren 12 holder reaktionsblandingen 23 tilstrækkelig opblandet til, at benstykkerne 26 ikke obstruerer bundåbningen 20 9 og udløbsrøret 10, når reaktionsblandingen ved hjælp af pumpen 11, som vist med pilene, kontinuerligt recirkuleres tilbage til reaktoren 2's bundsektion 8 gennem recirkulationsledningen 16. Pumpen 11 presser den recirkulerede reaktionsblanding gennem den åbne ventil 18 ud gennem 25 recirkulationsledningen 16's åbning 21. Den med pilene viste recirkulerede reaktionsblanding under tryk preller af mod afskærmningen 22. Recirkulationen foregår i bundsektionen 8 således, at fedtfasen 24 kan bevares intakt under hele reaktionsforløbet. En intakt fedtfase 24 kan fraskilles eller 30 skummes af som selvstændig fraktion uden at reaktionsblandingen behøver efterbehandling med f.eks. centrifugering. Den vedvarende recirkulation sikrer den bedst mulige kontakt mellem enzym og substrat og varmetransmission.The agitator 12 keeps the reaction mixture 23 sufficiently mixed so that the leg pieces 26 do not obstruct the bottom opening 20 9 and the outlet tube 10 as the reaction mixture is continuously recycled back to the bottom section 8 of the reactor 2 through the recycle line 16 by means of the pump 11. The recycled reaction mixture through the open valve 18 out through the opening 21 of the recirculation line 16. The pressurized recirculated reaction mixture bears off against the shield 22. The recirculation takes place in the bottom section 8 so that the fat phase 24 can be kept intact during the entire course of the reaction. An intact fat phase 24 can be separated or foamed off as an independent fraction without the reaction mixture needing post-treatment with e.g. centrifugation. Continuous recycling ensures the best possible contact between enzyme and substrate and heat transmission.
35 Når hydrolysen er afsluttet, stoppes røreværket 13, omrøreren 12 og pumpen 11. Den hydrolyserede reaktionsblanding 23 henstår DK 176496 B1 indtil den, som vist i fig. 3, har delt sig i tre faser: en fedtfase 24 øverst i reaktoren 2, en fast fase 26 i reaktoren 2's bundsektion 8, og en vandig fase 25 mellem fedtfasen 24 og den faste fase 26, 5When the hydrolysis is complete, the agitator 13, the agitator 12 and the pump 11 are stopped. The hydrolyzed reaction mixture 23 leaves DK 176496 B1 until, as shown in FIG. 3 has divided into three phases: a fat phase 24 at the top of the reactor 2, a solid phase 26 in the bottom section 8 of the reactor 2, and an aqueous phase 25 between the fat phase 24 and the solid phase 26, 5
Fig. 3 viser anlægget 1 efter faseadskillelse og med delvist tømt reaktor 2.FIG. 3 shows the plant 1 after phase separation and with partially emptied reactor 2.
Den faste fase 26 virker under aftapningen af de flydende faser 10 24,25 som et filter. Partikulært materiale i de flydende faser vil under aftapningen fanges og tilbageholdes i filterets porevolumen, og de flydende faser kan aftappes som rene, klare og faser.The solid phase 26 acts as a filter during the draining of the liquid phases 10.25. Particulate material in the liquid phases will during trapping be trapped and retained in the pore volume of the filter, and the liquid phases can be drained as clean, clear and phases.
15 Reaktoren tømmes, som vist i fig. 3, ved at lukke den første ventil 18 og åbne den anden ventil 20. Først aftappes de flydende faser 24,25. Pumpen 11 startes og flydende fase i form af vandigt hydrolysat 25 pumpes, som vist med pilene, via den anden åbne ventil 2 0 ud gennem recirkulationsledningen 16's 20 anden ende 19's udløbsåbning 27 og opsamles. Efter aftapningen af hydrolysatet 25 aftappes fedtfasen 24 på tilsvarende måde og opsamles.The reactor is emptied as shown in FIG. 3, by closing the first valve 18 and opening the second valve 20. First, the liquid phases 24,25 are drained. The pump 11 is started and liquid phase in the form of aqueous hydrolyzate 25 is pumped out, as shown by the arrows, via the second open valve 20 through the outlet opening 27 of the recirculation line 16 20 and collected. After draining of the hydrolyzate 25, the fat phase 24 is similarly drained and collected.
De flydende faser kan indenfor opfindelsens ramme også tappes 25 af reaktoren som følge af trykket fra væskesøjlen i reaktoren.The liquid phases can also be tapped within the scope of the invention by the reactor due to the pressure from the liquid column in the reactor.
Dernæst lukkes den anden ventil 20, reaktoren 2 fyldes med vand, omrøreren 12, røreværket 13 og pumpen 11 startes, og den faste fase og reaktoren vaskes med recirkulation, som beskrevet 30 ovenfor, i et ønsket tidsinterval. Dernæst åbnes den anden ventil 20 igen, og opslemningen af fast fase og vand pumpes ud af reaktoren.Next, the second valve 20 is closed, the reactor 2 is filled with water, the agitator 12, the agitator 13 and the pump 11 are started, and the solid phase and the reactor are washed with recirculation, as described above, for a desired time interval. Next, the second valve 20 is reopened and the solid phase and water slurry is pumped out of the reactor.
ILLUSTRATIONSEKSEHPELILLUSTRATIONSEKSEHPEL
35 En ca. 4 m3 isoleret cylindrisk reaktor, der er udstyret med varmekappe, har en diameter på 1,4 m, har en konisk bund med en DK 176496 B1 bundåbning med en diameter på 0,10 m. Recirkulationsledningens ventiler er lukkede. Reaktoren fyldes med en batch råvarereaktionsblanding af 1.800 kg okseben fra slagteriaffald (neddelt til stykker på ca. 2,5 cm's længde) og 1.200 kg vand.35 An approx. 4 m3 insulated cylindrical reactor, equipped with heating jacket, has a diameter of 1.4 m, has a conical bottom with a DK 176496 B1 bottom opening with a diameter of 0.10 m. The valves of the recirculation pipe are closed. The reactor is filled with a batch of raw material reaction mixture of 1,800 kg of bones from slaughterhouse waste (divided into pieces about 2.5 cm in length) and 1,200 kg of water.
5 Røreværk og omrører startes, og ved hjælp af varmekappen, der indeholder varm damp ved 2 bar, opvarmes blandingen til en gennemsnitstemperatur på 55°C. Pumpen startes, omrøreren startes og den første ventil åbnes, og recirkulation påbegyndes. Der tilsættes 1.800 g Novozyme 2,4 Alcalase 10 {protease), og omrøringen opretholdes i en hydrolyseringsperiode på 60 minutter. Alcalasen inaktiveres ved varmedenaturering idet reaktionsblandingens temperatur hæves til 95°C i 30 min ved hjælp af varme fra varmekappen. Omrøringen og pumpningen standses. Den første ventil lukkes.5 Stir and agitator is started, and by means of the heating sheath containing hot steam at 2 bar, the mixture is heated to an average temperature of 55 ° C. The pump is started, the stirrer is started and the first valve is opened and recirculation is started. 1.800 g of Novozyme 2.4 Alcalase 10 (protease) is added and stirring is maintained for a hydrolyzing period of 60 minutes. The alkalase is inactivated by heat denaturation, raising the temperature of the reaction mixture to 95 ° C for 30 minutes by heat from the heat jacket. Stirring and pumping are stopped. The first valve closes.
15 Reaktionsblandingen henstår i 10 min.. Benfraktionen synker til bunds i reaktorens bundsektion. Den anden ventil åbnes, og der aftappes først ca. 3.000 1 klar væske med et proteinindhold på 6w% beregnet på basis af massen af okseben. Dernæst aftappes 12 w% klart flydende fedt beregnet på basis af massen af okseben.The reaction mixture is allowed to stand for 10 minutes. The bone fraction sinks to the bottom of the reactor's bottom section. The second valve opens, and approx. 3,000 l of clear liquid with a protein content of 6w% calculated on the basis of the mass of beef bones. Next, 12 w% of clear liquid fat calculated on the basis of the mass of beef bones is drained.
2020
Den anden ventil lukkes, 1.000 1 vand påfyldes, den første ventil åbnes og røreværket, omrøreren og pumpen startes og vandet og den faste fase opblandes til en vaskeblanding. Efter 5 minutter lukkes den første ventil og den anden ventil åbnes.The second valve is closed, 1,000 l of water is filled, the first valve is opened and the agitator, the stirrer and pump are started and the water and solid phase are mixed into a wash mixture. After 5 minutes, the first valve closes and the second valve opens.
25 Vaskeblandingen pumpes ud.25 The wash mixture is pumped out.
Indholdet af proteiner, peptider og aminosyrer kan udvindes af den vandige fase. Alternativt anvendes den velsmagende vandige fase uden videre til f.eks. suppe eller kødekstrakt.The content of proteins, peptides and amino acids can be recovered from the aqueous phase. Alternatively, the tasty aqueous phase is readily used for e.g. soup or meat extract.
3030
Fedtstoffer, olier, lipider og ben kan udnyttes på kendt vis.Fats, oils, lipids and bones can be utilized in known manner.
3535
Claims (9)
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DK200301878A DK176496B1 (en) | 2003-12-18 | 2003-12-18 | Plant for enzymatic hydrolysis of a batch of animal or vegetable constituents and process for using the plant |
| PCT/DK2004/000870 WO2005058060A1 (en) | 2003-12-18 | 2004-12-16 | A plant for enzymatic hydrolysis of a batch of animal or vegetable components and method for using the plant |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DK200301878 | 2003-12-18 | ||
| DK200301878A DK176496B1 (en) | 2003-12-18 | 2003-12-18 | Plant for enzymatic hydrolysis of a batch of animal or vegetable constituents and process for using the plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| DK200301878A DK200301878A (en) | 2005-06-19 |
| DK176496B1 true DK176496B1 (en) | 2008-05-26 |
Family
ID=34684448
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DK200301878A DK176496B1 (en) | 2003-12-18 | 2003-12-18 | Plant for enzymatic hydrolysis of a batch of animal or vegetable constituents and process for using the plant |
Country Status (2)
| Country | Link |
|---|---|
| DK (1) | DK176496B1 (en) |
| WO (1) | WO2005058060A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DK200600920A (en) * | 2006-07-04 | 2008-01-05 | Danflavour Aps | Plant and method for hydrolyzing a reaction mixture of hydrolysable feedstock |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3018669A1 (en) * | 1980-05-16 | 1981-11-26 | Hoechst Ag, 6000 Frankfurt | METHOD FOR PRODUCING PLASMA FRACTIONS |
| US5113755A (en) * | 1984-04-30 | 1992-05-19 | Advanced Hydrolyzing Systems, Inc. | Apparatuses for producing a proteinaceous product by digestion of raw animal parts |
| US5248484A (en) * | 1991-08-05 | 1993-09-28 | Martin Marietta Energy Systems, Inc. | Attrition reactor system |
| US5744555A (en) * | 1994-11-25 | 1998-04-28 | Eastman Chemical Company | Process for the synthesis of elastomeric polypropylene |
| SE526999C2 (en) * | 2001-02-26 | 2005-12-06 | Biovelop Internat Bv | Process for extracting cell wall components and less accessible cereal clay proteins substantially free of soluble compounds |
-
2003
- 2003-12-18 DK DK200301878A patent/DK176496B1/en not_active IP Right Cessation
-
2004
- 2004-12-16 WO PCT/DK2004/000870 patent/WO2005058060A1/en active Application Filing
Also Published As
| Publication number | Publication date |
|---|---|
| WO2005058060A1 (en) | 2005-06-30 |
| DK200301878A (en) | 2005-06-19 |
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