Classifications

• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
  • A23L2/70—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter
  • A23L2/80—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by adsorption
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
  • A23L2/70—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter
  • A23L2/78—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by ion-exchange
• • 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
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W10/00—Technologies for wastewater treatment
  • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
  • Y02W10/33—Wastewater or sewage treatment systems using renewable energies using wind energy

Definitions

• the invention concerns a process for reducing the patulin concentration in fruit juices, apparatus suitable for such a purpose and to related methods and means.
• Patulin 4-Hydroxy-4H-furo[3,2-c]pyran-2(6H)-one (See Formula 1) is a mycotoxin produced by certain species of the genera Aspegillus and Penicillium. It is common in fruit that is rotting prior to processing for juice production. Penicillium expansum, is one such fungus and it is responsible for decomposition of apples and other fruit.
• Apples destined for processing into juice production frequently are pack house rejects, wind falls, weather damaged or from cold storage.
• the fruit is often stored in the open for extended periods before processing.
• the percentage of fruit with varying degrees of rot can be high and inevitably will contain patulin.
• Penicillium expansum which produces patulin is a common storage rot in a diverse range of product (e.g. apples, peaches, pears, bananas, pineapples, apricots, cherries and grapes). They indicate that for apple juices patulin levels are generally higher in cloudy juices than in clear juices (highest levels in their data showed as 434 ⁇ g/kg and 118 ⁇ g/kg respectively).
• Mycotoxins are undesirable in food because of their toxicity to animals and potential toxicity to human beings.
• the toxic activity of patulin, its teratogenicity, carcinogenicity and mutagenicity is known and is of concern.
• the Codex Alimentarius Commission as part of the United Nations joint FAO WHO Food Standards Programme in their 28th Session (June 1997) in respect of patulin indicates a PMTDI (Provisional Maximum Tolerable Intake) of 0.4 micrograms per kilogram body weight per day (i.e. 0.4 ⁇ g/kg.bw/day).
• Apple juice can occasionally be heavily contaminated) notwithstanding that apple juice generally (particularly single strength apple juice eg; 11.5° Brix) has patulin levels of below 50 ⁇ g/l (micrograms per litre).
• Patulin also degrades in time in stored juice. The gradual loss of patulin from juice on storage is not a practical solution to providing juice with acceptable patulin levels.
• Activated carbon can be used commercially to reduce patulin from fruit juice, but it is difficult to handle and is an expensive consumable item. Activated carbon is not viable to regenerate and reuse. It also adds to the solids loading of the factory effluent creating environmental problems.
• the present invention consists in a process for reducing the patulin content in a fruit juice which comprises or includes
• step (ii) harvesting the juice with a reduced patulin content from step (i).
• the adsorption of patulin onto the surface of the micropores of the resin is dependent upon the plurality of the surface matrix and orientation of the polar groups on the patulin molecule.
• the forces of chemisorption are likely provided by van der Waal and London dispersion interactions.
• the energy of chemisorption is very small and the patulin molecules are able to undergo lateral diffusion and conformational changes on surrounding surfaces. Therefore the chemisorption is best described as the physical attraction on to a chemically inert adsorption surface.
• the resin has weak base functionality although non-functionalised yet wettable resins may be used.
• said resin is substantially devoid of mesopores and macropores.
• Preferably said process uses a resin having very high internal surface areas yet a low mercury intrusion characteristic.
• said resin has a surface area of greater than 900 (eg; from 900 to 1500) m 2 /g (BET).
• said surface area is from 1000 to 1500 m 2 /g (BET).
• said resin has a mercury intrusion (d 50 ,A) of less than 100.
• said resin has micropores in abundance of less than 15 A (mpw).
• said resin is in the form of a bed of fibres, beads or granules.
• said beads granules or fibres have a section of from 300 to 1600 microns across.
• said resin is a styrene divinyl benzene network copolymer resin.
• said resin has been hypercrosslinked whilst in the swollen state.
• said resin has in abundance micropores of minimum pore width of from 5 to 20 ⁇ (mpw).
• the resin has been regenerated after a previous use in a similar patulin extraction process.
• Preferably said regeneration has involved the conversion of the resin held patulin to a more easily flushed out derivative using ammonia or a volatile base.
• said conversion has involved the at least substantially in situ generation of ammonia or a volatile base from a high pH solution in contact with the resin.
• said regeneration has subsequently involved after flushing out of the patulin derivative(s) the presentation of an acid to the resin.
• the juice is presented to the resin in the range of 20 or greater bed volumes prior to regeneration of the resin, the bed volume range being expressed in proportion to a real or notional single juice strength.
• the juice is presented to the resin at a rate of from about 4 to about 10 bed volumes/hour.
• the resin has been tertiary amine functionalised but is presented to the juice in an acid form as opposed to the free base form thereby reducing the uptake of juice acid during the presentation of the juice to the resin.
• the resin provides a bed of depth of from 0.5 to 2.0 metres.
• the present invention consists in apparatus for use in a process as previously defined, said apparatus having at least one vessel providing a bed of the resin and which is operable in at least two modes, the first mode being that which presents juice to and harvests juice from the resin and the second mode being that which regenerates the resin.
• the present invention consists in a method of regenerating a micropored resin which contains patulin in micropores which comprise or includes, in a high pH liquid environment containing the patulin fouled resin, generating a basic vapour (preferably ammonia) sufficient to convert the micropore held patulin to a more easily flushed out derivative or derivatives and thereafter flushing the derivative(s) from the micropores.
• a basic vapour preferably ammonia
• ammonia is generated.
• the high pH liquid environment is 10 or above.
• the resin after the flushing step is presented to an acid.
• the present invention consists in, in a patulin reducing process of a fruit juice, the use of a styrene divinyl benzene network co-polymer resin in the form of spherical beads or granules or fibres in sufficient quantities and with a sufficient proportion of micropores with a mpw of less than 20 ⁇ .
• said resin has a weak base functionality.
• beads or granules or fibres preferably beads or granules having a section of between 300 - 1600 microns across are used.
• the present invention consists in a process for reducing the patulin concentration in a fruit juice or fruit juices (hereafter juice) comprising or including the steps of presenting the juice to a styrene-divinyl benzene network co- polymer resin beads or granules (preferably spherical) in sufficient numbers for the volume of juice being present so that it achieves a desired patulin reduction over the contact.
• the present invention consists in a process for reducing the patulin content of a fruit juice which comprises
• the resin has been functionalised to facilitate wetting prior to its contact with the fruit juice.
• said functionalising has been weak base functionalised.
• said apparatus is apparatus of any of the kinds hereinafter described.
• the resin is regenerated using ammonia or a volatile base.
• the use of ammonia or volatile base follows resin contact with strong alkali.
• said strong alkali is sodium or potassium hydroxide.
• the regeneration involves the provision of an acid rinse following exposure of the resin to ammonia gas or the substitute volatile base.
• the present invention consists in apparatus for reducing the patulin concentration in a fruit juice or fruit juices which includes a vessel holding a quantity of styrene-divinyl benzene network co-polymer resin beads or granules in a manner such that a through-put of juice can be presented to the resin thereof and which allows between process runs of juice through the vessel the flushing of the resin with regenerative liquid(s) and/or gas(es).
• the present invention consists in a process for reducing patulin concentration in a fruit juice which comprises presenting the juice to beads or granules of a styrene-divinyl benzene network co-polymer resin having micropores of less than 20 A mpw.
• said beads, granules or fibres have a section of from 300 - 1600 microns across.
• said beads or granules or fibres are substantially devoid of mesopores and macropores.
• the present invention consists in a process for reducing patulin concentration in a fruit juice which comprises or includes presenting the juice to beads or granules of a styrene-divinyl benzene network co-polymer resin having pores which are almost exclusively micropores of less than 20 A mpw (ie; is low or substantially devoid of mesopores and macropores).
• said beads, granules or fibres have a section of from 300 to 1600 microns.
• said resin has a low mercury intrusion (e.g. ⁇ 100).
• said resin has been hypercrosslinked whilst in the swollen state.
• micropore - pores with a m.p.w. in the range of less than 20 A.
• pores - pores with a m.p.w. in the range of 20 to 500 A.
• macropores - pores with a m.p.w. in the range of greater than 500 A.
• BV bed volumes (i.e. the volume equal to the volume of resin contained in the processing vessel).
• juice includes within its ambit optionally pretreated fruit juices (eg; concentrated, ultrafiltrated, etc.) and/or blended and/or diluted fruit juices.
• pretreated fruit juices eg. concentrated, ultrafiltrated, etc.
• Figure 1 is a flow diagram of a conventional process for manufacturing apple juice save for the fact that it includes preferably after a preferred ultra filtration or other filtration (eg; diatomaceous earth) stage, a system for reducing patulin levels prior to the concentration of the juice,
• a preferred ultra filtration or other filtration eg. diatomaceous earth
• FIG. 2 is a diagram of preferred apparatus in accordance with the present invention
• Figure 3 shows in longitudinal cross section a typical underbed strainer (eg; of the kind indicated in Figure 2 as 28), such a strainer forming part of conventional type apparatus (such as discussed in "Commercialisation of Absorber Technology in the Fruit Juice Industry", Fruit Processing 4 - 96, R Lyndon, the full content of which are hereby here included by way of reference)
• Figure 4 is a juice and regenerant inlet distributor (referred to as 26 in Figure 2)
• 26 in Figure 2 is a juice and regenerant inlet distributor
• Figure 5 is a photograph (2500 x magnification) of the preferred resin (Alimentech P570) of the present invention showing the surface of the bead,
• Figure 6 is a similar photograph to Figure 5 but showing the surface of the bead magnified by 10,000 times
• Figure 7 is a similar photograph to that of Figure 5 but of a typical styrene-divinyl benzene adsorbent polymer with a high level of mesopores and macropores (the photo being shown at 2500 time magnification)
• Figure 8 is a surface of the same bead depicted in Figure 7 but at 10,000 times magnification, again showing the high level of mesopores and macropores in a typical styrene-divinyl benzene adsorbent polymer (for example as disclosed in US Patent 4,297,220 of Rohm and Hass Company and US Patent 4,439,458 of the Coca-Cola
• Figure 9 is a complex plot in respect of trials using a partial apple juice concentrate (25 °Brix) (SAMPLE A) and a preferred synthetic adsorbent resin media of the present invention (Alimentech P570) to demonstrate the regenerative nature of the media (for example, by plotting results for process cycles 23, 26 and 27 - each cycle being one presentation of the media to the juice for the purpose of patulin removal and thereafter one regeneration), the plot showing (i) concentration of patulin ( ⁇ g/1) against the volume of apple juice processed (BV), (ii) the absorbance at 325nm of Total Polyphenolics against volume of apple juice processed (BV), and (iii) the relationship of °Brix against bed volume,
• Figure 10 is a similar plot to that of Figure 9 but in respect of a similar partial concentrate (25 °Brix) (SAMPLE A) using a different media (Alimentech P700) showing as against the media (Alimentech P570) of Figure 9 (by plotting cycles 9, 12 and 13) the greater reduction in colour arising from the greater absorbance at 325 n.m of Total Polyphenolics of the juice,
• Figure 11 shows for a different source of apple juice partial concentrate (25 °Brix) (SAMPLE B) (again using the media of Figure 9, ie; Alimentech P570) and for process cycle 28 the relationship of (i) pH to volume of apple juice processed, (ii) the conductivity with respect to volume to apple juice processed, (iii) titratable acid against volume of apple juice processed, (iv) absorbance of total polyphenolics and absorbents against volume of apple juice processed, and (v) °Brix and patulin concentration against volume of apple juice processed,
• Figure 12 is a similar plot to that of Figure 11 (SAMPLE B also) but where Alimentech P700 has been used and in respect of an earlier process cycle (process cycle 14), and
• Figure 13 is a flow diagram of the preferred resin regeneration process.
• the present invention in its preferred form can commercially reduce patulin in fruit juice and concentrates made from fruit juice using equipment and engineering techniques used in existing applications of adsorbent polymers and ionic exchange resins in the food industry. See for example the machinery referred to by R Lyndon in the previously mentioned reference.
• the present invention in its preferred forms provides an economically viable method for reducing patulin by typically in the order of 90% from clarified apple juice with a synthetic adsorbent resin having clearly defined characteristics. Contained in a suitably designed and engineered system, the synthetic adsorbent resin can be repeatedly cycled between adsorbing patulin and rejuvenated by a unique regeneration process.
• patulin reduction in apple juice there is no reason to expect that patulin will not be reduced from other fruit juices (e.g. peaches, pears, bananas, pineapples, apricots, cherries and grapes) with the described process.
• the preferred synthetic adsorbent resins will preferably not remove colour from the apple juice to be processed. This is an important consideration, as colour reduction is often not required by juice processors. However if colour reduction of juice is required it can or may be achieved by inclusion of a suitable adsorbent into the processing vessels in addition to the patulin reducing resin.
• the apparatus depicted hereinafter in Figures 2, 3 and 4 are described as follows:
• Alkali inlet concentrated sodium or potassium hydroxide
• Ammonia inlet commercial ammonia solution diluted to 0.5% / v with dilution water.
• Adsorbent resin containment / Process vessel 25.
• FIG. 3 an under bed strainer to retain resin within the process vessel (such strainers being arrayed at the bottom of the vessel to provide containment of the resin and even distribution and collection of the treated juice and the regenerants
• FIG. 4 (Detail of inlet juice and regenerant distributors within the process vessel) the distributors being arranged to provide even distribution of juice and regenerant onto the top of the adsorbent resin bed.
• the most effective adsorbents were those with a high surface area characterised by a high percentage of micropores.
• the most preferred resins tested were those high in micropores and correspondingly very low in mesopores and macropores.
• the most preferred resins are the P570 and P700 Alimentech resins of our.
• the latter with its greater mercury intrusion characteristic than that of Alimentech P570 has more affect on colour of apple juice.
• Other resins are those of Purolite International Limited referred to below.
• Table 2 collects some relevant static characteristics of some resins of this kind available from Purolite International Ltd or sacred. Table 2.
• the chosen functionalities are those historically selected in ion-exchange applications:
• SB A - strong base anion, quaternary ammonium.
• Alimentech P570 is a very highly cross linked polystyrenic network produced by hypercrosslinking in the swollen state (small low pore diameters ( ⁇ 100 d 50 A)). This resin is characterised by having very few mesopores and macropores and a very high percentage of micropores (minimum pore width ⁇ 20 Angstroms).
• Alimentech P570 has virtually no mesopores or macropores. See Figures 5 and 6 and contrast them with Figures 7 and 8. The absence of these larger pores means that colour bodies in the juice are not adsorbed.
• Colour reduction is sometimes a requirement, but most often colour reduction is specifically not required by a processor.
• a further advantage of these synthetic adsorbent polymers is that they have a microporous structure. Molecules that would normally displace patulin are size excluded from being adsorbed.
• Standard styrene - DVB, polyester and acrylic resins can show a capacity to adsorb patulin but do not have such a "tight" porosity, and therefore have limited capacity. See Figures 7 and 8. However other resin types otherwise having the characteristics specified can be used.
• Non functionalised synthetic polymers of kind required with an abundance of micropores can sometimes be difficult to wet - amination with a tertiary amine (or any other means of providing a weak base functionality) ensures wetability of the micropores allowing passage of aqueous solution into them.
• Alimentech P570 is aminated with tertiary amine to provide the preferred weakly basic capacity. The weak base functionality assists the wetting of the resin.
• Patulin is desorbed from the resin at elevated pH. It was necessary to use a base that would migrate into the micropores of the resin. Trials were conducted with the use of ammonium hydroxide as a volatile base. This has proven to be very successful and unique.
• the process of reducing patulin from clarified fruit juice may be engineered to provide a commercial process.
• Practical plant may be constructed using conventional engineering techniques used in the application of ion exchange and other adsorbent polymers used in the water and food processing industries.
• Equipment may be constructed from stainless steel and designed to process at any flow rate encountered in practice. Typical flow rates will be 2,000 litres per hour to 30,000 litres per hour.
• Either fresh, single strength juice or reconstituted juice from concentrate may be used.
• Alimentech P570 (the preferred media) is contained in a suitably sized processing vessel and retained by a system of strainers located in the bottom of the vessel.
• the resin contained within the vessel can be contacted with juice during the resin exhaustion or juice process cycle, and various regenerants during the rejuvenation or regeneration cycle.
• a single processing vessel provides batch operation with the vessel alternating between juice processing for patulin reduction and regeneration or rejuvenation.
• a continuously processing machine may be installed in as part of the juice production facility so that all, part or none of the juice may be passed through the adsorbent resin bed.
• the process is completed in a number of steps carried out in a predetermined order.
• Step Description 1 Sweeten-on: Water from the previous cycle (final step of the regeneration) is displaced by juice, which is pumped into the vessel from the juice feed supply. The displaced water is diverted to drain or may be recycled to a water reuse system. Juice flow rate 5-10 bed volumes per hour.
• Completion of the sweeten-on step may be determined by either the volume of the influent juice or sensing the presence of juice at the outlet of the vessel with a suitable instrument, (conductivity, refractive index, mass flow etc).
• Juice into clear juice inlet (1) Juice flow controlled at flow control valve (14). Juice flows into process vessel through valve (16). Juice distributed onto adsorbent resin bed through juice inlet distributors (26). Water displaced from resin bed is collected in the under bed strainer/distributor system (28) and diverted to the drain (41) via Regenerant and rinse outlet to drain valve (32).
• Juice process Also known as exhaustion cycle. Juice is processed down flow through the resin bed at a flow rate in the range 5-10 bed volumes per hour. During this cycle patulin is adsorbed into the pores of the resin. The juice process step continues until the capacity of the resin to adsorb patulin is exceeded. This point is established by analysis of the juice for residual patulin, and retrospectively applied to subsequent processing cycles. Once the predetermined juice volume as measured with a suitable volume measuring device the next step begins Flow description: Juice into clear juice inlet (1). Juice flow controlled at flow control valve (14). Juice flows into process vessel through valve (16). Juice distributed onto adsorbent resin bed through juice inlet distributors (26). Having passed through the adsorbent bed the treated juice is collected by the under bed strainer/distributor system (28) and diverted via Treated juice outlet valve (31) to the treated juice outlet (35).
• Sweeten off At the completion of the exhaustion step the juice is displaced with water at 5-10 b.v. per hour to ensure that the maximum amount of juice is recovered to the product collection tank. The completion of sweeten off is determined by either the volume of the influent water or sensing the reduced juice concentration at the outlet of the vessel with a suitable instrument (conductivity, refractive index, mass flow etc).
• Raw potable water enters via valve (5) and isolation valve (7), is pumped (13) into the top of the resin containment/processing vessel via sweeten off valve (24). Juice contained in the vessel is displaced down-flow through the bed collected in the under bed strainer/distributor system (28) and diverted via valve (31) to the treated juice outlet (35).
• Backwash Water is passed up-flow through the resin bed at a flow rate of about 6 meters/hour .
• the resin bed is expanded and fluidised to remove any insoluble solids filtered on to the bed or channelling within the bed which may have occurred on the previous process cycle
• Flow description Soft water enters via valve (6) and isolation valve (8), is pumped ( 13) into the bottom of the resin containment/processing vessel at a preset flow rate via the upflow water control valve (23).
• the backwash water is distributed up-flow into the resin containment vessel. Water exits the vessel to drain via backwash out let valve (29).
• Settle Flow through the bed is stopped, allowing the resin to classify and settle.
• Alkali inject Resin bed is contacted, down-flow (or up-flow) with alkali solution. Acceptable performance is obtained using 2 b.v. of 2% w / v solution of either sodium or potassium hydroxide solution, passed down flow through the bed at a flow rate of about 4 b.v. per hour.
• Soft water from inlet (6) and isolation valve (8) is pumped (13) via flow control valve (22), and regenerant isolation valve (21) into the resin containment/processing vessel (25), distributed onto the resin bed via the regenerant chemical inlet distributors (26).
• Concentrated sodium or potassium hydroxide from inlet (2) is pumped ( 10) via injection valve ( 17) and "on-line” diluted to 2% w / v .
• the spent solution is collected by the under bed strainer/distributor system (28) and diverted via regenerant rinse outlet valve (33) to the effluent discharge (41).
• Resin bed is contacted, down flow or up flow with solution of caustic and ammonium hydroxide. 1 b.v. of solution containing
• 1% / v sodium or potassium hydroxide and 0.5% w / v ammonium hydroxide is passed through the bed at a suitable flow rate of about 4 b.v. per hour.
• Soft water from inlet (6) and isolation valve (8) is pumped (13) via flow control valve (22), and regenerant isolation valve (21) into the resin containment/processing vessel (25), distributed onto the resin bed via the regenerant chemical inlet distributors (26).
• Concentrated sodium or potassium hydroxide from inlet (2) is pumped (10) via injection valve (17) and "on-line” diluted to 1% / v .
• Ammonium hydroxide solution from inlet (3) is pumped (11) via injection valve ( 18) and "on-line " diluted to 0.5% w / v .
• the spent solution is collected by the under bed strainer/distributor system (28) and diverted via effluent outlet valve (33) to the effluent tank (34).
• aqueous caustic ammonia solution injection step flow through the vessel is stopped to allow a holding time of approximately 30 minutes enabling diffusion of gaseous ammonia into the matrix of the resin and for patulin to diffuse out from the resin matrix.
• Soft water from inlet (6) and isolation valve (8) is pumped (13) via flow control valve (22), and regenerant isolation valve (21) into the resin containment/processing vessel (25), distributed onto the resin bed via the regenerant chemical inlet distributors (26). Having passed down- flow through the process vessel, the spent solution is collected by the under bed strainer/distributor system (28) and diverted via effluent outlet valve (33) to the effluent tank (34).
• First Fast rinse The bed is rinsed from the top of the vessel with 1 b.v. of water at about 12 b.v. per hour to rinse the majority of the free aqueous caustic ammonia solution from the resin.
• the rinse effluent from this step is diverted to the effluent tank.
• Acid wash Necessary to convert the functional groups on the resin from the free base form into the acid form to avoid the removal of fruit acid from the subsequent juice process cycle. Either citric or phosphoric acid may be used to effect the conversion. The effluent from this step is diverted to the effluent tank.
• Additional acid is used to ensure that the ammonia in the effluent tank is neutralised and acidified to ensure that free ammonia is not liberated form the effluent solution when it is diverted to the effluent drain.
• 2 b.v. of citric acid as a 2% w / v solution is adequate to ensure effluent neutralisation.
• the flow rate that the acid solution is applied at may be at typical fat rinse rate of up to 12 bed volumes per hour.
• the partially depleted solution is collected by the under bed strainer/distributor system (28) and diverted via effluent outlet valve (33) to the effluent tank (34).
• Displacement Acid solution is displaced with 1 b.v. of raw potable water at a flow rate of 4 b.v. per hour. The effluent from this step is diverted to the effluent tank.
• Final Rinse Resin bed is rinsed with raw potable water at a suitable rate (approximately 12 b.v. per hour) to remove residues of acid. Completion of final rinse is sensed by the monitoring the conductance of the rinse water exiting the resin bed. Final rinse water is diverted to drain.
• the resin bed may be returned to service for the next juice processing cycle to begin.
• Raw water from inlet (6) and isolation valve (8) is pumped (13) via rinse inlet valve (24), into the processing vessel (25), Having passed down-flow through the resin containment /process vessel, the rinse solution is collected by the under bed strainer/distributor system (28) and diverted via the rinse outlet valve (32) to the drain (41).
• the resin bed may be returned to service for the next juice processing cycle to begin.
• the temperature at which the process is conducted will effect the performance, however all development trials have been conducted at ambient temperature with commercially acceptable results. Increasing the temperature will improve the kinetics of the process (possibly without leakage of patulin) but the capacity of the resin will not be increased.
• Effluent processing Effluent from this process does contain ammonia. Consideration has been given to minimising the egress of ammonia gas by collecting (bulking) the effluent which contains ammonia into a suitable tank.
• the effluent from the acid wash step is added to the ammonia containing effluent at a rate to ensure that the pH is less than 7 thus preventing the evolution of ammonia gas.
• the tank is mixed with a suitable mixer.
• the contents of the tank is discharged to the common drain.
• Adsorbent Resins are lightly functionalised with tertiary amine groups and thereby comply with FDA regulations. Both also have a preponderance of micropores eliminating the competition from the larger hydrophobic compounds in a juice which are size excluded from the large portion of the available adsorption surface. Evaluation of both of these adsorbent resins were progressed to laboratory scale column trials.
• SAMPLE A Apple juice reconstituted to 25 ° Brix from concentrate.
• the partial concentrate was moderately coloured with a higher than typical total polyphenol content.
• the detected level of patulin in the juice decreased from 98 ⁇ g/1 to 13 ⁇ g/1 corrected to 12
• SAMPLE B 25 °Brix apple juice reconstituted from concentrate. This partial concentrate was lower in colour and total polyphenolics than the SAMPLE A juice. During these trials patulin was reduced from 78 ⁇ g/T to 12 ⁇ g/1 corrected to 12 °Brix..
• the resin was stored layed-up in 2 % caustic solution and hence was conditioned by cycling once with phosphoric acid before initiating a standard patulin regeneration followed by five monitored, sequential processing cycles using SAMPLE A high patulin juice, and finally by one cycle with SAMPLE B juice.
• the adsorbent resin was preconditioned from new with eight cycles using apple partial concentrate prior to conducting five monitored, sequential processing cycles treating SAMPLE A high patulin juice, followed by one cycle using SAMPLE B juice.
• the selected concentrate was reconstituted to 25 ° Brix and thirty bed volumes pumped through the bed at 6 b.v./hr, at ambient temperature.
• the performance of the resins are predicted to be diffusion rate dependent so flow rates are important.
• Five samples were drawn through each of the service cycles and analysed to determine the patulin and polyphenol leakage profiles. The results are displayed in Figures 9 to 12.
• Tables 3 to 5 exhibit the typical feed juice analysis, plus the concentrations of indicative components in selected treated composite samples, after normalisation to 25 °Brix. The results were selected to demonstrate performance trends, the other results are available upon request.
• the World Health Organization guideline limit for patulin is 50 ppb, ⁇ 50 ⁇ g/1 at 12 °Brix.
• the total polyphenolics, absorbance and patulin results have been normalised to 25 °Brix for ease of comparison.
• the World Health Organisation guideline limit for patulin is 50 ppb, ⁇ 50 ⁇ g/1 at 12 °Brix.
• the total polyphenolics, absorbance and patulin results have been normalised to 25 °Brix for ease of comparison.
• the World Health Organisation guideline limit for patulin is 50 ppb, ⁇ 50 ⁇ g/1 at 12 °Brix.
• Figure 9 compares the patulin and total polyphenolic leakage profiles for selected process cycles through Alimentech P570, and Figure 10 displays the analogous data for the process runs through Alimentech P700.
• Figure 9 the concentration of Patulin
• Volume axis is pH.
• Conductivity is a measure of conductivity
• 59 is Bed Volume vs Conductivity ( ⁇ S/cm)
• 60 is Bed Volume vs Abs of Total Polyphenolics (AU)
• Figure 12 plots Soluble Solids (°Brix) and Patulin ( ⁇ g/1) against Volume of 25
• 64 is Bed Volume vs °Brix
• 65 is Bed Volume vs Patulin ( ⁇ g/1)
• Alimentech P700 has the effect of much greater colour reduction (ie; -42% at 420 nm as opposed to only -2% with Alimentech P570 for SAMPLE B).
• the patulin analyses were conducted using Reversed-phase High Performance Liquid Chromatography using standard methods.

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• 1998
  • 1998-03-27 JP JP54134398A patent/JP2002501372A/ja active Pending
  • 1998-03-27 CA CA002284868A patent/CA2284868C/en not_active Expired - Fee Related
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