SE1351272A1 - Ny produkt - Google Patents

Abstract

21 Sammandrag Foreliggande uppfinning hanfor sig till en ny reaktor for utforande, med hjalp av atminstone ett fast reaktionselementet, biologisk eller kemisk omvandling, eller fysisk eller kemisk adsorption fran, eller frisattning av amnen for att, en vatskefas, vilken reaktor innefattar ett reaktorkarl innefattande medel for att 6ka vatskeskjuvspanning, och en transformationsanordning som är operativt monterad i namnda reaktorkarl. Uppfinningen tillhandahaller aven en sats av delar innefattande ett reaktorkarl innefattande medel for att oka vatskeskjuvspanning och en transformationsanordning. Slutligen tillhandahaller uppfinningen en metod for anvandning av namnda reaktor och / eller namnda sats av delar for biologisk eller kemisk omvandling eller fysisk eller kemisk adsorption fran, eller frisattning av amnen till, en vatskefas, med hjalp av minst en fast reaktionsmedlem.

Description

bed, in transformation schemes where seouentiai addition of agents and/or removal of by-products or desired products are necessary, or where the physical or chemical conditions must otherwise be altered during the course of processing with the solid member. in those cases, a batch-wise processing 5 model is often preferred. Such batch-wise heterogeneous processing can either be done by suspending the solid member directly in the fluid medium as particulate material under agitation, a process that will norrnally call for a filtration or sedimentation step to separate the phases after the process has been brought to an end. Alternatively, the fluidlc medium can be circulated 10 from the batch reactcr through a packed reservoir containing the solid member by means of a specially designed flow system ccmprising pumps and/or valves or the like, in order to accomplish the convective mass transfer needed for the transformation to take place. Such reactors are often quite complicated and must regularly be built on-site and adapted for a specific 15 purpose.

The challenge of establishing efficient convective mass transfer between solid and fluid phases has been addressed in different ways. Some interesting alternatives are disclosed in WO 201 11098570, which relates to devices for performing biological or chemical transformation, or physical or 20 chemical trapping from, or release of agents to, a fluidic medium by means of a solid reaction member. These devices are cornprised of a flow distributor having a fluid medium inlet, a fluid medium outlet, at least one confinement where said transformation, trapping, or release of agents is performed, and a means for rotating, rocking, wagging, or osciiiating the flow distrlbutor, by 25 which action fluidic medium in which it is subrnerged is pumped through a bed of solid member contained within the flow distributor.

As a result of this pumping action, use of the devices disclosed in WO 2011/098570 leads to increased convective mass transfer, and accordingly improved performance of most heterogeneous transformation schemes. One 3G of the reasons for these enhanced convective mass transfer properties is the ability of the flow distributor to use a combination of centrifugal force and flow dynamics to draw fluid through the central inlet(s) and discharge it through the peripherai outiets, resulting in a pumping action that predominantiy draws fluid from the larger central intet iocated at the bottom of the device.

However, there is stiii a need for devices capabie of providing even rriore increased convective mass transfer and an increased ratio between soiid 5 reagent and fiuidic reaction medium, in order to improve the performance of biological and chemical transformation, physicai and chemicai trapping and reiease of agents by means of a solid reaction member even further. Factors that hamper the efficient use of fiovv distributor devices disciosed in WO 201 11098570 in a cyiindricai reactor are the formation of soiid body rotation 10 and piughoie vortices, accompanied by suction of gases, which can be difficuit to get rid of, into the fiow distributor. The conventionai way of soiving the probiem of solid body rotation and vortex formation for standard irnpelier- stirred batch reactors (Fig. t) is to disturb the rotationai fiow in the reactor by furnishing the vessei with a set of baffies 10 (H. A. Jakobsen, “Chemical 15 reactor modeling: ltilultiphase reactive fiows", Springer Veriag: Beriin/Heidelberg, 2008; pp. 579-684), which are normaily impiemented as several (typicaiiy four) verticai fiow-interrupting eiements that are placed at some distance from the inner wait of the reactor in order to avoid the formation of unstirred fiuid oockets. However, as is evident from Fig. 1, the 20 inclusion of a conventionai set of baffles results in a substantial increase in the totai fiuid voiume of the reactor. Such excess voiume is often detrimentai to the kinetics of the intended transformations, since it will prevent the use of a high volume ratio between the soiid reaction member and the fluidic phase.

For an equal charged amount of reactants in the fluid phase, the 25 concentration wili thereby become lower, which has a negative effect on reaction kinetics in most cases. Conventionai baffles are furthermore impractical to impiement in smail scale iaboratory reactors.

Summarv of the invention 30 lt has now turned out to be possible to produce a reactor which ieads to substantiai increase in the convective mass transfer of heterogeneous transformation schemes, while at the same time improving the reaction kinetics by reducing the voiume of the fiuidic medium, in comparison with prior art, and accordingly further improve the performance of biologicai and chemical transformations, and physical and chemical trapping from or, reiease of agents to, the fluidic media being processed by such schemes. ln a first aspect, the invention provides a reactor for performing, by 5 means of at least one solid reaction memheds), biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media, said reactor comprising a cylindricai reactor vessel having a first end part, a second end part, and an inner wall between these parts, in which reactor vessel a transformation device has been mounted, said 1G transformation device comprising a flow distributor having an essentially cylindrical shape, a first essentially flat surface, a second essentially flat surface, and a peripheral wall having an essentialiy Circular cross-section, at least one fluid medium inlet adapted for receiving fiuid medium, and optionally 15 adapted for receiving initiaily suspended solid reaction member(s), located in vicinity of the centre of said first and/or second surface, at least one fluid medium outlet permeable for said fluid medium but impermeable for solid reaction members, said outlet(s) being located on said peripheral wall, a driving shaft located on said first surface for 2G enabling rotation or oscillation of the flow distributor, and at least one confinement wherein said solid members can be trapped and said transformation is performed; and a means for rotating and/or osciilating the device; wherein said inner wall of the reactor vessel comprises means for enhancing 25 the fluidic shear stress in any of the two rotary directions along said inner wall between said first end part and said second end part. ln a second aspect, the invention provides a kit for performing a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media by means of a solid reaction member, 30 comprising: a) a cylindrical reactor vessel having a first end part, a second end part and an inner wall between these parts, wherein said inner wall comprises means for enhancing the fluidic shear stress in any of the two rotary directions along said inner wall between said first end part and said second end part; and b) a flow distributor having an essentially cylindrical shape, a first essentially flat surface, a second essentially flat surface, and a peripheral wall 5 having an essentially circular cross-section, at least one fluid medium inlet adapted for receiving fluid medium and optionally adapted for receivlng initially suspended solid members located at the centre of said first andlor second surface, at least one fluid medium outlet permeable for said fluid medium but impermeable for solid members, said outlet being located on said 10 peripheral wall, a driving shaft located on said first surface for enabiing rotation or oscillalion of the flow distributor, and at least one confinement wherein said solid members can be trapped and said transformation is performed. ln a third aspect, the invention provides a method of using a reactor 15 according to the first aspect for performing a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, in a fluidic media by means of a solid reaction member.

Brief description of the enclosed fioures 20 The present invention will now be further disclosed with reference to the enclosed figures, in which: Fig. t presents a side view of a conventional reaction set-up for performing a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media by means of a solid 25 reaction member; Flg. 2 shows a side view of an embodiment of a transformation device Fig. 3 outlines the second surface of an embodiment of the flow dlstributor; Fig. 4 discloses a view of the first surface of an embodirnent ofthe flow 30 distributor of the transformation device in Fig, 2; Fig. 5 shows a horizontal cross-sectionai view from below along the line A - B of the embodiment of a transformation device shown in Fig. 2.

Fig. 6 presents a horizontal cross-section of a reactor comprising a transformation device and semi-elliptically-shaped groves in the inner wall of the reactor; Fig. 7 discloses a horizontal cross-section of a reaotor comprising a 5 transformation device and tubes on the inner wall of the reactor; Flg. 8 describes a horizontal cross-section of a reactor cornprising a transformation device and rectangular channels on the inner wall of the reactor; Fig. 9 describes a horizontal cross-section of a reaotor oornprising a 10 transformation device and seml-elliptlcal Channels on the inner wall of the reaotor; Fig. 10 outlines a horizontal cross-section of a reaotor comprislng a transformation device and triangular Channels on the inner wall of the reactor; and 15 Fig. 11 shows a side view of a reactor corriprising a transformation device as well as means for enhancing the fluidic shear stress in any of the two directions along said inner wall between said first end part and said second end part. 20 Detailed description of preferred embodlments Acoordlngly, in a first aspect the invention provides a reactor for performing, by means of at least one solid reaction rnembeds), a biological or chemical transformation, or physical or chemical trapplng from, or release of 25 agents to, a fluidlc media, said reactor comprising a cylindrloal reactor vessel having a first end part, a second end part and an inner wall between these parts, in which reactor vessel a transformation device has been mounted, said transformation device comprising a flow distributor having an essentially cylindrical shape, a first 3G essentially flat surface, a second essentially flat surface, and a perlpheral Wall having an essentially Circular orosssection, at least one fluid medium lnlet adapted for receiving fluid medium and optionally adapted for recelving initially suspended solid reaction member(s)s iocated in vicinity of the centre of said first and/or second surface, at ieast one fluid medium outiet permeabie for said fiuid medium but impermeabie for said soiid reaction members, said outiet being iocated on said peripherai Wait, a driving shaft iocated on said first surface for 5 enabiing rotation or osciiiation of the fiow distributor, and at least one confinement wherein said solid reaction members can be trapbed and said transformation is performed; and a means for rotating andior osciiiating the device; wherein said inner wait of the reactor vessei cornprises means for enhancing 10 the fluidic shear stress in any of the tvvo rotary directions atong said inner wall between said first end part and said second end part.

Transformation devices comprising a fiow distributor and a means for rotating andíor osciiiating the device have been described in WO 2011/998570. 15 As disciosed herein, the term “means for enhancing the fiuidic shear stress" reiates to some different types of Structures capabie of causing perturbations in the fiuidio media fiow close to the inner wait of the reactor vessei that is caused by the rotationai movement of the fiow distributor. Such means typicaiiy has a smati voiuine, and the totai voiume of such means in a 20 reactor according to the invention typicaiiy arnounts to less than 10 % of the totai vciume of the reactor vessei. in some embodiments, the totai voiume of such means amounts to less than 8 °/@, 6 %, 5 %, 4 %, 3% or 2 %, respectivety, of the totai volume of the reactor vessei. Exampies of semi- eiiipticaiiy shaped groves are given in Fig. 6, and exampies of hemicyiindrical, 25 cyiindricai, rectangular, and trianguiar shapes are given in Figs. 7, 8, 9 and iO, but the invention is not iimited to these specificaiiy exempiified embodiments; instead numerous other shapes are conceivabie, with or without hoiiovv channeis, and in varying number and height, that Wouid cause sufficient perturbation of the shear iayer to induce a turbuient flow wiii fuifiii 30 the criteria of a working device according to the invention and a skiiied Worker shouid be abie to figure out aiternative perturbating gecmetries faiiing within the scope of the invention, based on the examples given in these disclosures. ln a preferred embodirnent, said means for enhancing the fluidic shear stress is at least one semi-ellipticaily-shaped grove in said inner wall extending in a direction from said first end part to said second end part. ln one embodiment, the inner wall of the reactor vessei comprises a plurality of 5 such semi~elliptically-shaped groves. ln one ernbodiment, said groves are arranged adjacent to each other. in one embodirnent, the depth of said groves amount to 10 - 50 % of the width of the groves, in a preferred ernbodirnent, said means for enhancing the fluidic shear stress is at least one hollovv structure in said wall, said hoilow structure 10 extending in a direction from said first end part to said second end part, said hoilovv structure having open ends above and below said flow distributor and a through~going channel there between, thereby facilitating communication between the fluidic medium above and below the flow distrihutor. in a preferred embodiment, the channel has a triangular, elliptical or 15 semi-elliptical cross-section. The cross~section of the internal channel of the hollow structure is sufficiently large in order to allow flow of fluidic medium therein. in one embodiment, the inner cross-section of the hoiiow structure has an internal area of at least 0.25 cmz. ln a preferred embodiment, the reactor comprises 2 - 30 of said means 20 for enhancing the fluidic shear stress. in other embodiments, the reactor comprises 3 -- 30, 4 - 30, 5 - St), 6 -- 30 or 8 -- 25 of said means. ln a second aspect, the invention provides a kit for performing, by means of a solid reaction member, a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media, 25 comprising: a) a cylindrical reactor vessel having a first end part, a second end part and an inner wall between these parts, wherein said inner wall comprises means for enhancing the fluidic shear stress in any of the two rotary directions aiong said inner Walt between said first end part and said second 30 end part; and b) a flow distrlbutor having an essentially cylindrical shape, a first essentially flat surface, a second essentially flat surface, and a peripheral wall having an essentially circular cross-section, at least one fiuid medium intet adapted for receiving fiuid medium and optionally adapted for receiving suspended solid reaction membeds) located in vicinity of the centre of said first and/or second surface, at least one fluid medium outiet permeable for said fluid medium but impermeable for solid reaction membeds), said outlet 5 being located on said peripheral wall, a driving shaft located on said first surface for enabling rotation or osciliation ofthe flow distributor, and at least one confinement wherein said solid reaction member(s) can be trapped and said transformation is performed. ln one embodiment said means for enhancing the fluidlc shear stress is 10 at least one semi-eilipticaily-shapecl grove in said inner wall extending in a direction from said first end part to said second end part. ln a further embodiment, said means for enhancing the fiuidic shear stress is at least one hollow structure in said wall, said hollow structure extending in a direction from said first end part to said second end part, said 15 holiow structure having open ends and a through-going channel therebetvveen, thereby facilitating communication of the fluidic medium in the upper and lower parts of the reactor vessel. ln a further embodiment, the channel has an trianguiar, ellipticai or semi-eliiptical cross-section. 20 ln a further embodiment, the reactor comprises 2 - 30 of said means for enhancing the fluidic shear stress. in a third aspect, the invention provides a method of using a reactor _ according to any the first aspect for performing, by means of a solid reaction member, a biological or chemical transformation, or physical or chemical 25 trapping from, or release of agents to, a fluidic media.

Turning now to the enciosed figures, Fig. 1 presents a side view of a conventional reaction set-up 10 according to the state of the art for performing a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media by means of a solid reaction member. 30 The set-up 10 is comprised of a reactor vessel 12 having two intet openings 14, with stoppers 1o fitted onto a tid 18 with closure means 20 as well as an Outlet opening 22 fitted with closure means 24. The reactor vessei 12 further comprises stirring means 26 powered by an electricaiiy, pneumatically, or 10 hydrauticalty driven motor 30 via a drive shaft 28. The reactor vessel 12 aiso comprises several voluminous baffles 32, 34, 36 joined by two ring-Shaped joining members 38, 40. Such a conventionat set-up is associated with the problems discussed above in the technicat background section. 5 Fig. 2 presents a side view of an embodimerit of a transformation device 100 that is a part of the present invention. The transformation device comprises a fiow distributor 102 and a rotation and/or oscillation means 116, typicaity an etectrioally, pneumaticaliy, or hydrauiicatiy driven motor, joined to the flow distributor 102 by a drive shaft 114. The flow distributor 102 has a 10 first surface 104, a second surface 106 and a oeriphera! wa!! 108. The flow distributor 102 has an essentially cyiindricai shape and the periphera! wall 108 has an essentially circular cross-section. There are ftuid medium inlets 110 on the first 104 or on the second 106 surface, or optionaiiy on both said surfaces. There are also ftuid medium outlets 112 on the peripheral wall 108. 15 The drive shaft 114 is rnounted centratty on top ofthe first surface 104.

Fig. 3 shows a view of the first surface 104 of the fiow distributor 102.

There is optionaity, or compulsory if there are no ftuid inlets on the second surface 106 in Fig. 4, at ieast one fiuid medium intet 110 on the first surface 104 in close proximity to the attachment iocation of the drive shaft 114, or in 20 other words adjacent to the intended axis of rotation of the second surface 104.

Fig. 4 shows a view of the second surface 106 of the flow distributor 102. There is optionaiiy, or compulsory if there are no fluid iniets on the first surface 104 in Fig. 3, at least one fluid medium intet 110 at, andlor adjacent 25 to, the intended axis of rotation ofthe second surface 106.

Fig. 5 discloses a cross-sections! view from the first surface of an embodiment of the fiow distributor 102 shown in Fig. 2 aiong the radie! plane from A to B. tn the shown embodirnent, there is a plurality of confinements 130 seoarated from each other by separating Waits 132. The confinements 30 130 may be futty or parttatiy separated from each other. tn the shown ernbodiment, there is a central ftuid medium intet 110 which is cornmon to all confinements. ln other embodiments comprising fuity separated confinements there is at least one ftuid medium intet for each confinement. As already 11 shown in Fig. 2, there are fluid medium outlets 112 arranged in the peripheral wall 108 in such a way that there is at least one such outlet 112 from each confinement 130. in the embodiment shown in Flg. 5 there is also a peripheral retaining mesh 134 along the inner surface of the perioheral wall 108. The 5 peripheral retaining mesh 134 is perrneable for the fluid reaction medium but not for the solid reaction members. in the shown embodiment, there is also, ootionaily and suspended on a rnesh retainer 136, an inner retaining mesh 138, which also is permeable for the fluid reaction medium but not for the solid reaction members. in situations where the solid reaction mernber(s) are 10 arranged in confinements 130 of the flow distrlbutor right from the start, such an inner retaining mesh could be included in order to prevent the solid reaction members from escaping through the fluid medium inlet 110.

However, in cases were solid reaction memherts) are added to and suspended in the fluld medium, such an inner retaining mesh should not be 15 included as the solid reaction member(s) will be effeotively drawn into the flow distributor 102 by its suction force and trapped thereln when rotating/oscillating the flow distributor 102.

Fig. 6 presents a horizontal cross~section of a reactor 120 comprising the flow distrlbutor 102 of a transformation device and semi-elliptically-shaped 20 groves 122 in the inner wall of the reactor. The distance V-V refers to the distance between the deepest points of two opposite grcves (or valleys) and V-V to the distance between two opposite ridges. Typically, the distance R-R is 70 - 95 % of the distance V-V. Typically, the amount of groves is 10 - 25.

Fig. 7 discioses a horizontal cross-section of the flow distributor 102 of 25 a transformation device encased in a reactor 120 comprising a set oftubes 124 adapted on the inner side of the peripheral wall 148 of the reaotor 120. in a manner similar to a set of conventional baffles, these tubes 124 will cause perturbations and enhanced fluidic shear stress in relation to the fiow distrlbutor 102 rotating inside reactor 120, while additionally providing flow 30 paths between the fluid volumes above and below the flow distributor 102 to enhance the mixing of these fluid volumes, which are otherwise effectively separated by a radial flow curtaln created by fluid exiting from the peripheral outlets of flow distributor 102. 12 Fig. 8 discloses a horizontal crosssection of the flow distributor 102 of a transformation device encased in a reactor 120 cornprising a set of hollow rectangular Channels 126 adapted on the inner side of the peripheral wall 148 of the reactor 120, channels 126 of which both ends are open and which 5 Iengths extend at least along the entire height of the flow distributor 102.

Similar to a set of conventional baffles, these Channels 126 will cause perturbations and enhanced fluidic shear stress in relation to the flow distributor 102 rotating inside reaotor 120, while additionally providing flow paths between the fluid volumes above and below the flow distributor 102 to 10 enhance the mixing of these fluid volumes, which are otherwise effectively separated by a radial flow curtain created by fluid exlting from the peripheral outlets of flow distributor 102.

Fig. 9 describes a horizontal cross-section of the flow distributor 102 of a transformation device encased in a reactor 120 comprising a set of semi- 15 elliptical tubes 128 forming channeis on the inner side ofthe peripheral wall 148 of the reactor 120, channels 128 ofwhioh both ends are open and which lengths extend at least along the entire height of the flow distributor 102.

Similar to a set of conventional baffles, these Channels 128 will cause perturbations and enhanced fluidic shear stress in relation to the flow 20 distributor 102 rotating inside reactor 120, while additionally providing flow paths between the fluid volurnes above and below the flow distributor 102 to enhance the rnixing of these fluid volurnes, which are otherwise effectively separated by a radial flow curtain created by fluid exiting from the peripheral outlets of flow distributor 102. 25 Fig. 10 outlines a horizontal cross-section of the flow distributor 102 of a transformation device encased in a reactor 120 comprising a set of triangular Channels 140 on the inner side of the oeripherai wall 148 of the reactor 120, Channels 140 of which both ends are open and which iengths extend at least along the entire height of the flow distributor 102. These 30 triangular Channels cause perturbations and enhanced fluidic shear stress in relation to the flow distributor 102 rotating inside reactor 120, while additionally providing flow paths between the fluid volumes above and below the flow distributor 102 to enhance the mixing of these fluid volumes, which 10 15 20 25 30 13 are otherwise effeotively separatecl by a radial flow curtain created by fluid exiting from the peripheral outlets of flow distributor 102.

Fig. 11 shows a side view of a reactor 230 according to the present inventlon comprising a first end part 250 and a second end part 260, and further comprising a transformation device including a flow distributor 212, an electricaliy, pneumatioally, or hydrauiically driven motor 214, a lid 228 with closure means and a drive shaft 226, inlet openings 234 with stoppers 236 as well as a multitude of means 232 for enhancing the fluidic shear stress in any of the two directions along said inner wall between said first end part and said second end part, constructed according to any of the principles illustrated in Fig. 6, 7, 8, 9, or 10. The reactor 230 also cornprises an outlet means 244 which can be used to empty the fluid content of the reactor after completion of the transformation, without having to filter the solution. lnterstitial fluid trapped by the solid member in the flow distributor 212 can then easily be emptied into the reactor by centrifugal force, simply by allowing the flow distributor 212 to continue its rotational movement during the emptying step.

Exgerimental section The present invention will now be further described in the following examples, which are provided for illustration purposes and are not intended to limit the scope of the present invention, Examgle 1, A flow distributor of the invention, constructed essentially according to Fig. 2, 3, 4, and 5, with outer diameter 45 mm and height 30 mm, was used in the experiment, in combination with an electric overhead stlrred with electronically controlled rotational speed. A standard 250 ml. glass beaker of 60 mm inner diameter was used as reactor vessel, without the use of any means of baffling to reduce the solid body rotation and vortex formation. The vessel was filled with 150 ml of water into which the flow distributor was placed, pre-filled with 27 ml of water-washed active carbon (12/40 mesh) in 14 the space between the with the options! inner retaining mesh and the perioheral retaining mesh. At this stage 0.435 ml of a 'i % (w/v) solution of disodium B-hydroxy-5-((2-methoxy-5-methyi-4-sulfophenyl)azo)-2-naphtha- ienesulfonate, a red foodstufi dye also known as Ailura Red, CJ. 16035, 5 FD&C Red 40, and 5129, was added to the water. The fiow distributor was immediately thereatter set to rotate at 509 RPM, and a decoiorization experiment was continued untii the solution was oornpieteiy coioriess. There was a strong solid body rotation aocompanied by formation of a weil developed vortex and the time required for oompiete decoiorization ot the 10 solution was 510 seconds.

Examgle 2 The same set-up and water volume as in Example 1 was used, with the difference that the conventional beaker was substituted for a reactor 15 vessei of the invention (60 mm outer diameter) with 18 radial unduiations as in Fig. 6, with ridge-ridge (R-R) diameter 49.5 mm and valley-valley (V-V) diameter 54.3 mm, according to notations shown in said Figure. Essentialiy no soiid body rotation was seen and an accompanying vortex was thus not formed. The time required for complete decoiorization was 360 seconds at a 20 rotational rate of 500 RPM, verifying a substantiai increase in mass transfer compared to Exarnple t.

Examgle 3 The same set-up as in Exarnpie t was used, with the difference that 25 oniy 60 ml water was used in combination with the flow distributor of the invention and the unbaffied beaker. There was a strong solid body rotation accompanied by the formation of a weil deveioped vortex extending essentially across the entire upper surface of the flow distrihutor. The time required for complete deoolorization of the soiution was 225 seconds at a 3G rotationai rate of 560 RPM.

Examgle 4 15 The same set-up and water voiume as in Exampie 3 was used, with the difference that the fiow distributor and reaotor vesset of the invention were used in combination. Ûniy very limited solid body rotation was observed and hardiy any vortex was formed. The time required for compiete decoiorized of 5 the soiution was 195 seconds at a rotational rate of 500 RPM. The reactor vessei of the invention acoompiished an praoticaiiy total prevention of vortex formation and a slight increase in mass transfer compared to Exampie 3.

Exampie 5 10 The same set-up as in Example 1 was used, With the difference that the fiow distributor of the invention was used in combination with an unbaffied 400 mL beaker With inner diameter 77 mm. A strong vortex was formed that extended down to the upper intets of the fiow distributor, with unwanted Suction of air as a resutt. The time required for compiete deooiorization was 15 600 seconds at a rotational rate of 500 RPM.

Example 6 The same set-up as in Exampie 5 was used, with the difference that the a 400 mL beaker (80 mm outer diameter) was now equipped with three 20 conventional baffles made from poiyitetrafiuoroethene), according to prior art.

No voitex was formed and the slanted level of the water surface shows the action of the conventionai baffles lead to pressure buiid-up between the baffies. The time required for complete decolorization was 420 seconds at a rotational rate of 500 RPM, which verifies that the oonventionai bafftes led to 25 increased mass transfer compared to the unbaffied beaker.

The same set-up as in Exampie 5 was used, with the difference that the beaker Was substituted for a reactor vessei of the ihvention (80 mm outer 30 diameter) with 18 radiai unduiations as in Fig. 6, with ridge-ridge (R-R) diameter 69.6 mm and vaiiey-vaitey (V-V) diameter 74.3 mm, according to notations shown in said Figure. No tendency of soiid body rotation 16 accompanied by voriex formation was seen. The time required for compiete decoiorization was 270 seconds at a rotationai rate of 500 RPM, which is evident of a substantiai increase in mass transfer, compared to the conventionai baffies used in Experiment 0.

Exampie 8 The same set-up as in Exarnpie 5 was used, with the difference that the flow distributor according to the invention was now larger, with diameter was 65 mm and height 30 mm, and the water voiume was increased to 300 10 mi. to which 0.645 mi of 1 % (wiv) Aiiura Red was added. A strong vortex was formed that extended down to the upper iniets of the fiow distributor, with unwanted suction of air as a result. The time required for compiete decoiorization was 450 seconds at a rotationai rate of 500 RPM. 15 Exampie 9 The same set-up as in Exampie 8 was used, with the difference that the beaker was substituted for a reactor vessel of the invention (80 mm outer diameter) with 18 radiai unduiations as in Fig. 0, with ridge-ridge (R-R) diameter 69.6 mm and vaiiey-vaiiey (V-V) diameter 74.3 mm, according to 20 notations shown in said Figure. No tendency of soiid body rotation accompanied by vortex formation was seen. The time required for cornpiete decoiorization was 3?5 seconds at a rotationai rate of 500 RPM, which is reveais a substantiai increase in mass transfer. 25 The person skilied in the art reaiizes that the present invention by no means is iimited to the preferred embodiments described above. On the contrary, many modifications and Variations are possible within the scope of the appended ciaims.

Additionaliy, Variations to the disciosed ernbodiments can be 30 understood and effectec! by the skiiied person in practicing the ciairneci invention, from a study of the figures, the disciosure, and the appended oiairns. in the ciaims, the word “comprising" does not exciude other eiements 17 or steps, and the ândefinite artšcše "a" or “an" does not excåude a piurality. The mere fact that certaän measures are recšted in mutuaiiy different dependent claims cioes not indicaíe that a combinatšons of these measures sannot be useci to acivantage.

Claims (11)

10 15 20 25 30 18 AMENDED CLAIMS:

1. A reactor for performing, by means of at least one solid reaction member(s), a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media, said reactor comprising a cylindrical reactor vessel (120, 230) having a first end part (250), a second end part (260), and an inner wall (148) between these parts, in which reactor vessel a transformation device (100) has been mounted, said transformation device comprising a flow distributor (102, 212) having an essentially cylindrical shape, a first essentially flat surface (104), a second essentially flat surface (106), and a peripheral wall (108) having an essentially circular cross-section, at least one fluid medium inlet (110) located in vicinity of the centre of said first and/or second surface, said inlet (110) being adapted for receiving fluid medium and optionally being adapted for receiving initially suspended solid reaction member(s), at least one fluid medium outlet (112) permeable for said fluid medium but impermeable for solid reaction member(s), said outlet(s) being located on said peripheral wall (108), a driving shaft (114, 226) located on said first surface (104) for enabling rotation or oscillation of the flow distributor (102, 212), and at least one confinement wherein said solid reaction member(s) can be trapped and said transformation is performed; and a means (116, 214) for rotating and/or oscillating the device; characterized in that said inner wall (148) of the reactor vessel comprises means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress in any of the two rotary directions along said inner wall (148) between said first end part (250) and said second end part (260).

2. A reactor according to claim 1, characterized in that said means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress is at least one semi- elliptically-shaped grove (122) in said inner wall (148) extending in a direction from said first end part (250) to said second end part (260). 10 15 20 25 30 19

3. A reactor according to claim 1, characterized in that said means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress is at least one hollow structure (124, 126, 128, 140) in said wall (148), said hollow structure(s) extending in a direction from said first end part (250) to said second end part (260), said hollow structure(s) (124, 126, 128, 140) having open ends above and below said flow distributor (102, 212) and a through- going channel therebetween, thereby facilitating communication between the fluidic medium above and below the flow distributor (102, 212).

4. A reactor according to claim 3, characterized in that the channel has a rectangular, triangular, elliptical, or semi-elliptical cross-section.

5. A reactor according to any of claims 1 - 4, characterized in that the reactor comprises 2 - 30 of said means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress.

6. A kit for performing, by means of at least one solid reaction member(s), a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media, comprising: a) a cylindrical reactor vessel (120, 230) having a first end part (250), a second end part (260) and an inner wall (148) between these parts, wherein said inner wall (148) comprises means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress in any of the two rotary directions along said inner wall (148) between said first end part (250) and said second end part (260); and b) a flow distributor (102, 212) having an essentially cylindrical shape, a first essentially flat surface (104), a second essentially flat surface (106), and a peripheral wall (108) having an essentially circular cross-section, at least one fluid medium inlet (110) being adapted for receiving fluid medium and optionally being adapted for receiving initially suspended solid reaction member(s), which inlet (110) is located at the centre of said first (104) and/or second (106) surface, at least one fluid medium outlet (112) permeable for 10 15 20 25 30 20 said fluid medium but impermeable for solid reaction member(s), said outiet(s) (112) being located on said peripheral wall (108), a driving shaft (114, 226) located on said first surface (104) for enabiing rotation or osciilation of the flow distributor (102, 212), and at least one confinement (130) wherein said solid reaction member(s) can be trapped and said transformation is performed.

7. A kit according to claim 6, characterized in that said means for enhancing the fluidic shear stress (122, 124, 126, 128, 140, 232) is at least one semi- elliptically-shaped grove (122) in said inner wall (148) extending in a direction from said first end part (250) to said second end part (260).

8. A kit according to claim 6, characterized in that said means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress is at least one hollow structure (124, 126, 128, 140) in said wall (148), said hollow structure extending in a direction from said first end part (250) to said second end part (260), said hollow structure having open ends and a through-going channel there between, thereby facilitating communication of the fluidic medium in the upper and lower parts of the reactor vessel.

9. A kit according to claim 8, characterized in that the channel has a rectangular, triangular, elliptical or semi-elliptical cross-section.

10. A kit according to any of claims 6 - 9, characterized in that the reactor comprises 2 - 30 of said means (122, 124, 126, 128, 140, 232) for enhancing the fluidic shear stress. 11 _ Use of a reactor according to any one of claims 1 - 5 for performing, by means of at least one solid reaction member(s), a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, in a fluidic media.