FI60505B - OVER ANCHORING FOR BEHANDLING AV ETT FLYTANDE AEMNE - Google Patents

Description

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Patent and Registration Office .... , - . (44) Date of publication of the notice and of the publication. - "

Patent- oeh registerstyrelsen 'Anattkan utlagd och utukrifte »pubiicerad 30.10.81 (32) (33) (31) Pyydetty etuoikeus — Begird prloritet 17 · 0U. 75

Republic of South Africa - South Africa (ZA) 75 / 2UU2 (71) Atomic Energy Board, Pelindaba, Pretoria, Transvaal, Republic of South Africa - South Africa (ZA) (72) Pierre Cloete Haarhoff, Hartebeespoort, Transvaal, Werner Adolf Schumann, Brooklyn, Pretoria, South Africa-South Africa (ZA) (7U) Forssen & Salomaa Oy (5U) Method and apparatus for handling fluid - Förfarande och anordning för behandling av ett flytande ämne

The present invention is directed to a method of treating a fluid. The invention also relates to a device for treating a fluid.

The method according to the invention is mainly characterized in that a flow of material containing only one phase is fed into the channel, the composition of which varies in a known manner in a known cross-section of the flow perpendicular to the direction of flow. located in the channel downstream of the feed point, without eliminating the variation in flow composition and that before and after the fluid has passed through the impeller or propeller, at least some parts of the flow having different compositions are separated and removed from the channel .

Said particular property may be physical or chemical. Flow components with different compositions differ in this property. By "single phase" is meant that the fluid is a gas or that it is a liquid composed of completely mixed components with no interfaces.

When fed into a channel, the composition of the flow can vary from a minimum to a maximum with respect to a given property. The variation in composition may be substantially continuous or may be substantially stepwise.

2 60505

The channel may be circular in cross-section or preferably annular with the composition of the flow varying circumferentially from said minimum to said maximum with the minimum and maximum target on opposite sides.

The method may include one or more process steps for the flow prior to separating portions of said flows. The method may thus include changing the pressure of the fluid as a process step. The movement of the fluid along the channel can thus take place using an axial flow impeller or a propeller as the impeller increases the pressure of the fluid. The method may also include changing the temperature of the fluid as a process step.

This can be done with a porous heat exchanger element extending across the duct. The method may also include removing and adding the fluid to the stream as a process step. The fluid can be removed from the flow by an isotope separator that changes the isotopic composition of the flow, and the fluid can also be removed from the flow or added to the flow through channels opening from the channel.

In the method, partitions running parallel to the flow in a part of the channel can be used to separate the parts of the flows from each other, thus preventing the variation in the composition of the flow from disappearing.

The channel may form an endless ring or a portion thereof along which the flow passes as at least a portion of the flow circulates around the ring more than once. The fluid can thus pass around the ring as it follows different helical paths. When the channel has an annular cross-section with the composition varying circumferentially from minimum to maximum as described above, there may be two helical tracks, each running circumferentially from minimum to maximum and each passing around the ring more than once. The method may also include at least deflecting the flow from the flow of the ocean adjacent to the point where the fluid is fed into the channel to countercurrent flow of material to said helical paths.

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The ring may also be formed by an inner cylindrical housing 12 extending within the outer cylindrical housing 14 as the opposite ends of the inner housing open at opposite ends of the outer housing, the helical tracks having axes running circumferentially in opposite directions relative to the housings from minimum to maximum.

When the method is applied to isotope separation and the channel forms an endless ring or portion thereof along which the flow travels, the fluid to be fed or added to the flow is preferably added to the portion of the flow having the isotopic composition closest to the composition of the fluid to be added.

When the flow is circulated along the channel by an impeller or propeller that provides axial flow, the flow of material circulates as a whole as it passes through the impeller or propeller at a given angle. The method may thus include deflecting the flow in the circumferential direction to compensate for the flow rotation caused by the compressor with respect to the channel.

The device according to the invention, in turn, is mainly characterized in that it has means forming a ring comprising a channel, at least one feed point to the ring and at least one outlet point of the ring, an impeller or a propeller for causing a single phase flow of material along the ring and recirculation of at least one part of the flow more than once around the ring, said feed and discharge point and said impeller or propeller being arranged such that said part or parts each follow a helical path around the ring, the axis of each helical path being perpendicular to the direction of flow along the channel and each helical path being completely looped over the entire length of the tire.

The device may include deflection means for deflecting the fluid flowing along the ring to cause said portion or portions to travel along said path or paths.

The device may include one or more downstream partitions in a portion of the channel, and the flow generating member may be an axial flow impeller or propeller.

The device may include a porous heat exchanger element extending across said channel to change the temperature of the material flow as it flows along the ring.

The channel may be annular, with one sector of the channel having a main feed point and the opposite sector of the channel having a main outlet to divide the fluid entering the main feed point * i ...... '4 60505 into two sections following different helical paths around the ring main outlet -towards. The ring may be formed by an inner cylindrical housing that extends within the outer cylindrical housing as the opposite ends of the inner housing open to opposite ends of the outer housing.

The device may include an isotope separator in the ring to prevent the isotopes of the material flow from flowing along the ring.

In the device, a number of spaced apart feed points may be introduced into the ring and a plurality of spaced apart outlet points may leave the ring.

In the following detailed description of the invention, the invention is presented for reasons of convenience mainly related to the isotope separation process with a split ratio of 1/5, i.e. a fraction of the feed stream leaving the separation elements as enriched flow 1/5 and the enriched flow The example refers to the case where the enriched and impoverished flow leaving the elements are at the same pressure. The example is applicable to either a process that deals with a flow of material that consists only of

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from a process gas (such as UF 2, which must be enriched for U "" "sn) or a process for treating a substance stream consisting of a mixture of a process gas or a carrier gas, e.g. H 2 O or helium. However, in the following, all references to isotope composition and mass flow of a gas stream refer to the isotopic composition and mass flow background of the process gas in the stream.

The invention will now be described by way of example with reference to the accompanying drawings.

In the drawings: Fig. 1A schematically shows a flow diagram of a part of a cascade arrangement suitable for a split ratio of 1/5, Fig. 1 shows in axial section a side view of a fluid handling device according to the invention, Fig. 2 shows a flow diagram of the device of Fig. 1, Figs. 3A-3H Figures 4 show a flow diagram for a device similar to the device of Figure 1 but adapted to a lower recycling rate, Figures 5A-5D show a representation corresponding to Figures 3A-3H for the flow diagram of Figure 4, Figure 6 shows a flow diagram for a device similar to similar to the device of Fig. 1, but adapted to a higher recycling rate, Figs. 7A-7P show a representation corresponding to Figs. 3A-3H to the flow chart of Fig. 6, Fig. 8 shows a side view partially sectioned along the line VIII-VIII in Fig. 9 show a picture is a plan view of the device 8 partially sectioned along the line IX-IX in Fig. 8 and Fig. 10 shows a detail of the device according to Figs. 8 and 9 seen from the direction of the line X-X in Fig. 9.

In Fig. 1A, reference numeral 1 generally refers to a part of a block forming part of a cascade arrangement, the cascade arrangement consisting of a plurality of blocks connected in series. Each block has a number of substantially similar stages 2, each of which in turn comprises an isotope separator 3f, a heat exchanger 4 and a compressor 5 * adapted to circulate the gas flow in succession through the heat exchanger 4 and the separator 3. The stages 2 are interconnected by means forming feed streams 6, enriched streams 7 and depleted streams 8. Each feed stream 6 entering stage 2 consists of two other streams 7 and 8 coming from stage 2 and passes through the respective compressor 3 and heat exchanger 4 to the respective separator 3 » where it is divided into two new flows 7 and 8. These new flows in turn pass to the other two stages 2. In Fig. 1A a part of the block is shown to consist of three groups of four stages 2. Each group is fed by four enriched flows 7 from the previous group and a depleted flow from the next group 9. 8. The stages can be considered to be connected in series as the enriched streams 7 flow against the flow direction of the depleted streams 8 along a cascade. Thus, each stage is shown to receive as part of its feed an impoverished flow 8 from the next stage and as part of its feed an enriched flow coming from a stage in fourth order in series, the series being considered to advance along the cascade in the direction of increasing flow enrichment, each flow 7 is 1/4 from the same stage outflow 8 as mass flows and the flows 7 and 8 joining to form the flows 6 are approximately similar in isotopic composition. The cascade arrangement has an incoming feed flow, a final outgoing enriched flow, and a final outgoing depleted flow (not shown), and the flow rate at which fluids are fed and taken out of the cascade through these flows is adjusted to achieve desired mass flow rates and isotope compositions within the cascade arrangement. The interconnections of the stages 2 described above belong to internal stages which are within the block far from its edges. At the edges of a block, i.e. at the interfaces of that block and adjacent blocks, the block has edge stages whose connections to other blocks may be different depending on the structure of the cascade compared to the interconnections of the stages 2 shown.

In Fig. 1, reference numeral 10 generally denotes an apparatus according to the invention for separating isotopes of gases. The device 10 has an inner housing 12 and an outer housing 14 around it. · The housing 12 is a hollow cylinder open at its ends and has a narrow part 12.1 and a wide part 12.2 connected by a conical part 12.3 * The outer housing 14 is also hollow-cylinder-like and has the narrow part 14-a and the wide part 14 * 2, which are connected by a conical part 14 ·? · The outer housing is closed at its ends. Narrow section 12.1. is inside the narrow part 14 * 1, the wide part 12.2 inside the wide part 14 · 2 and the conical part 12.? conical section 14 ·? indoors.

The housing 12 forms a channel 16 with a narrow part 16.1 opening into the narrow part 14 * 1 of the housing 14 and a wide part 16.2 opening into the wide part 14 * 2 of the housing 14. The housings 12 and 14 are coaxial and the open ends of the housing 12 are spaced axially inwardly from the closed ends of the housing 14. The housings 12 and 14 form an annular channel 18 between them, with a channel 16 in the narrow part 16.1. the narrow part 18.1 connected to it and the wide part 18.2 connected to the wide part 16.2 of the channel 16. The channels 16 and 18 thus together form an endless channel or ring having an inner tubular portion formed by the channel 16 and an outer annular portion formed by the channel 18 750505, within which the inner portion is located.

The duct 16 has an axial compressor 20 formed by an axial flow impeller with a shaft 20.1 and a plurality of vanes 20.2. The shaft 20.1 is coaxial with the channels 16, 18 and extends from the outside of the housing 14 inwards into the narrow part 16.1 of the channel 16. Wings 20.2. located in the narrow part of channel 16 16.1.

The duct 16 has a heat exchanger with a porous heat exchanger element 22. The heat exchanger 22 extends over a wide part 16.2 of the duct 16. across the conical portion 12.3 of the housing 12.

The wide portion 16.2 of the channel 16 has a separator 24 with a plurality of gas isotope separating elements 26 with the heat exchanger 22 between the separator 24 and the impeller 20. Each element 26 has a feed point 26.1 communicating with the narrow portion 16.1 of the channel 16, a main outlet 26.2 communicating with the ring and directed towards the closed wide end 14 · 2 of the housing 14, and at least one side outlet between said main outlet and the feed point. The elements for use in Figures 1-7 are of the type having a split ratio of 1/5, i.e., split the feed flow into the enriched flow and the depleted flow with the enriched flow being 1/4 of the depleted flow as mass flows. Two partitions 28,30 located between the heat exchanger 22 and the separator 24 and at the free end of the wide part 16.2 of the duct 16, respectively, insulate the compartment 32 in the duct 16 from the rest of the ring. The feed points 26.1 and main discharge points 26.2 of the elements 26 come from the ring, lead to the ring outside the compartment 32 and the side discharge points lead to the compartment 32. The compartment 32 has an axial outlet passage 34 »extending axially outwards from the compartment 32 and through the end of the wide housing part 14.2. It should be noted that the side discharge points of each element 26 may be formed from the permeable surface of the element instead of a separate discharge point, depending on the isotope separation process intended to be used.

The wide part 18.2 of the channel 18 has a main feed point 36 formed by a tube, which is directed into the channel 18 in the axial direction towards the narrow part 18.1 of the channel.

From the wide part of the duct 18.2 leaves the main outlet formed by the pipe, which is directed into the duct 18 in the opposite axial direction to the feed 36 · 60505

The inlet 36 and the outlet 38 are located on opposite sides of the channel 18.

The second feed point formed by the channel 40 with four subchannels 40.1, 40.2, 4Ο.3 and 40.4 runs circumferentially around the housing 14.

The channel 40 has from its subchannels 40.1-40.4 into the annular channel 18 several flow connection points located on the circumference of the annular channel 18. The location of these flow junctions, two of which are shown in Figure 1 indicated by reference numeral 42, is explained in more detail below.

The inside of the channel 34 is similarly divided by partitions into four Osaka hubs 34.1, 34 * 2, 34 * 3 and 34 * 4 »which open via flow interfaces to the compartment 32. This arrangement of flow interfaces will also be explained in more detail later.

The annular channel 18 is provided with deflection members adapted to deflect the material flow of the channel 18. The operation of the exemption bodies is explained in more detail below. The deflection support members comprise a plurality of deflection elements in the channel 18, which most preferably consist of curved deflection plates (not shown). The plates are between the housings 14 and 12 and, viewed from the edge, form a radially inward angle with the longitudinal direction of the device 10, i.e. the polar axis. The plates are located on a circumferential ring 44 immediately upstream of the main feed point 36.

The operation of the device is shown below with further reference to Fig. 2, in which reference numeral 46 generally indicates a flow chart of the device of Fig. 1, and Figs. 3A to 3H, in which reference numeral 48 generally indicates various cross-sections of the device of Fig. 1. Unless otherwise indicated, the same parts are denoted by the same reference numerals.

The device 10 forms a module adapted to include a group of stages that form part of a block of a cascade arrangement in a process of isotope separation of gases, with several similar modules connected in series. A mixture of gas isotopes having a first component and a second component that differs in isotope from the first component runs in series. In each module, isotope separation takes place, whereby the gas mixture is divided into two streams, i.e. a stream enriched for the desired e.g. first component and a stream depleted for said desired component. Each module receives an enriched flow from the previous module in the series and an impoverished flow from the next module. The enriched flow from the preceding module is generally denoted by reference numeral 50 and runs along channel 40. Said flow 50 is divided into four sub-flows 50.1, 50.2, 50.5 and 50.4 * The isotopic composition of these sub-flows is different i.e. their concentrations or degrees of enrichment as determined by the desired component ) component and the other component have different mass ratios. They run along subchannels 40.1, 40.2, 40.3 and 40.4, respectively. · The depleted flow from the next module is indicated by reference numeral 52.

The depleted flow 52 enters the channel 18 of the device 10 through the main supply point 36. The subchannel 40.1 has one flow connection point 42 to the channel 18, which connection point is located immediately downstream and axially aligned with the supply point 36. The partial flow 50.1 has substantially the same isotopic composition as the flow 52. The interface 42 may, if desired, be provided with mixing means such as, for example, a nozzle plate or the like to promote mixing of the flows 52 and 50.1. Such a mixing member may be present at each of the interfaces 42 below.

The combined flow formed by the partial flow 50.1 and the flow 52 flows along the channel 18 towards the narrow end 14 of the housing 14. This flow flows substantially along the sector of the channel 18 and, after entering the compressor 20 in the channel 16, denoted by reference numeral 54 in Figures 2 and 3A. Said flow 50.1, 52 flows along said sectors of duct 18 and duct 16 through compressor 20 so that the flow mixes only slightly with adjacent flows. Said flow 50.1,52 thus forms a sector channel 18 of the total annular flow and a sector channel 16 of the total annular or circular flow. As the combined flow 50.1,52 passes through the compressor 20, the sector of the total flow passing through the channel 16 in which said combined flow passes moves in the circumferential direction in the direction of rotation of the blades 20.2 of the compressor 20. Sector 54 of compressor 20 thus follows a helical path at the compressor. However, this flow is not substantially mixed with flows in adjacent sectors. The flow 50.1.52 in its sector 54 flows along the duct 16 and enters the sector of the heat exchanger 22. As it passes through the heat exchanger 22, the temperature of said flow is changed by the desired amount, after which it enters the elements 26 of the corresponding sector of the compartment 32 through the supply points 26.1 of the separator elements 26. The sectors in the heat exchanger 22 and in the compartment J> 2 (i.e. in the separator 24) are indicated in Figures 2 and 3E by reference numeral 54 * 1 »These sectors 54 * 1 do not necessarily have to be axially aligned with sector 34 as this leaves the compressor 20, as it is conceivable that the total flow in the duct 16 may circulate in the circumferential direction between the compressor 20 and the heat exchanger 22.

The combined flow 50.1,52 undergoes an isotope separation process in the elements 26 which form the sector 24.1 of the separator 24.

In the sector 54.1 of the separator 24, the combined flow 50.1,52 is divided into an enriched flow 56.1 and a depleted flow 58.1 with a process gas ratio of 1/5 of the elements 26 of 1 · The depleted flow 58.1 leaves the main outlets of the elements 26 forming said sector 54 · 1. The enriched flow leaves the side outlets of said elements 26 to compartment 32. In compartment 32, the enriched flow 56.1 passes to sub-channel 34 · 1 of channel 34 and from there to the next module in the series.

The depleted flow 58 · 1 flows into the channel 18 and flows axially along the sector of the channel 18 to the ring of deflection plates at 44 "It impinges on one or more of said deflection plates and is divided into two partial flows 58.1 running axially along the channel 18 on opposite sides of the feed point 36. The subchannel 40.2 has two flow interfaces 42 to the channel 18 at points where the flow currents 58.1 run along the channel 18. The subflows 58.1 are associated with the subflow 50.2 from the subchannel 40.2 through these interfaces 42. The partial flows 50.2 and 58.1 are substantially similar in isotope composition. The combined partial flows 50.2,58.1 run axially along the channel 18 on opposite sides of the combined flow 50.1,52 in the narrow part 14.1 of the housing 14. Said combined partial flows 50.2, 58.1 enter the two sectors 60 of the channel 16 at the compressor 20 on opposite sides of the sector 54. It should be noted that for ease of presentation, sectors 60 are shown in Figure 2 as a single sector.

The combined partial flows 50.2, 58.1 pass, as described in connection with the combined flow 50.1, 52, along the duct 16 from the narrow part 16.1 through the heat exchanger 22 to the separator 24 «The sectors of the heat exchanger 22 and the separator through or to which these combined flows pass are marked. with reference number 60.1. This pair of sectors is again shown in Figure 2 as one sector in the heat exchanger 22 and the separator 24. · Each combined sub-flow 50.2, 58.1 enters the elements 26 of the second sector 60.1 of the separator 24 through these inlets 26.1.

In said sectors 60.1 of the separator 24, the combined partial flows 50.2, 58 * 1 are each divided into an enriched partial flow 56.2 and a depleted partial flow 58.2. The enriched partial flows 56.2 pass through the side outlets of the elements 26 in said sectors 60.1 to the compartment 52, from there through the flow junctions to the subchannel 54 * 2 of the outlet channel 54 to form an enriched flow 56.2 and from there to the next module in series.

The depleted partial flows 58.2 pass through the outlets 26.2 of the elements 26 in said sectors 60.1 to the channel 18 on opposite sides of the flow 58.1.

The partial flows 58.2 run along the channel 18 on opposite sides of the flow 58.1 and are deflected by the deflection plates at 44 so as to continue along the channel 18 on the sides of the combined partial flows 58.1, 5Q2 »farther from the combined flow 50.1,52. At the point where the partial flows 58.2 run radially inward from the channel 40, they are joined by an enriched flow 50-5 from the subchannel 40.5 through two flow junctions 42. The isotope composition of the enriched stream 50.5 is substantially the same as that of the partial flows 58.2.

The combined partial flows 50.5, 58.2 run axially along the channel 18 away from the deflection plates towards the narrow part 18.1 of said channel. Said combined sub-flows 50.5, 58.2 are on those sides of the combined sub-flows 50.2, 58.1 which are further from the combined flow 50.1, 52. The combined partial flows 50.5, 58.2 at the compressor 20 enter the two sectors 62 of the channel 16, which are on the sides of the sector 60 further away from the sector 54. Again, the sector 62 is shown in Figure 2 as one sector.

The combined partial flows 50.5, 58.2 pass, as described in connection with the combined flow 50.1, 52, along the duct 16 from its narrow part 16.1 through the heat exchanger 22 to the separator 24 » 62.1. Again, this pair of sectors in the heat exchanger 22 and the separator 24 is shown in Figure 2 as one sector. Each of the 12 60505 combined partial flows 50 * 3 »58 * 2 enters the elements 26 of one of said sectors 62.1 of the separator 24 through their supply points 26.1.

The combined partial flows 50 * 3 »58.2 are each divided in said sectors of separator 24 62.1 into enriched partial flow 56.5 and depleted partial flow 58.3 * Enriched partial flows 56.5 pass through the module.

The depleted partial flows 58.3 pass through the outlets 26.2 of the elements 26 of said sector 62.1 to the channel 18 with respect to the partial flows 58.2 on the sides farther from the flow 58.1.

The partial flows 58.3 run along the channel 18 with respect to the partial flows 58.2 on the sides farther from the flow 58.1. At 44, the deflection plates turn the sub-flows 58.3 so that they continue along the channel 18 with respect to the combined sub-flows 58.2, 5Q3 on the sides farther from the combined sub-flows 58.1, 50.2. After passing the deflection plates, the sub-flows 58.3 mentioned in 44 flow side by side to form a single flow 58.3 * At the point where the flow 58.3 runs radially inwards with respect to the channel 40, flow 58.3 *

The combined flow 50.4, 58.3 flows, as described in connection with the combined flow 50.1, 52, in the axial direction along the channel 18 towards the narrow end 14 * 1 of the housing 14. The combined flow 50.4, 58.3 enters the compressor 20, where it flows in sector 64 between sectors 62. Said combined flow 5Ο.4, 58.3 then passes along the channel 16 away from its narrow o-section 16.1 through the heat exchanger 22 to the separator 24. The sectors of the heat exchanger 22 and the separator through or to which the combined flow 50.4, 58.3 pass are indicated by reference numeral 64.1.

In said sector 64.1 of the separator 24, the combined flow 50.4, 58.3 is divided into an enriched partial flow 56.4 and a depleted partial flow 58.4.

15 60505 The depleted flow 59 * 4 passes through the outlet points 26.2 of the elements 26 of said sector 64 · 1 into the channel between the partial flows 58.3. The flow 58.4 travels a short distance in the wide part of the duct 18, after which it flows along the main outlet duct 38 to the previous module in the series.

It should be noted that the flow 58.4 in the outlet duct 38 functionally corresponds to the flow 52 in the previous module of the series through the supply channel 36. Similarly, flows 56.1-56.4 flowing as partial flows in the channel 34 subchannels 34 · 1-34 · 4 are treated in the next module in the series at the same time. and have the same function as the subcharges 5O.I-5O.4 entering the device 10 via the channel 40.1-40 * 4 of the channel 40.

The combined flow 50.1,52, the combined partial flows 50.2, 58.1, the combined partial flows 50.3 »5 & 2 and the combined flow 50.4» 58.3 run axially along the channels 16,18 next to each other substantially apart, except for a slight diffusion at the interfaces. Said mixing also does not take place as said flows and partial flows pass through the compressor 20. It is thus observed that in the device 10 different flows and partial flows are fed to the channel 18 in the zone of said channel with the feed point 36, the channel 40 and the deflection plates at 44, so that the composition of the total flow along the channel 18 varies as desired in the cross section against the direction of movement of the total flow. In fact, the composition changes as it travels in opposite directions along the circumference from the main feed point 36 to the main discharge point 38. Said composition change means the isotopic composition of the gas expressed as the concentration of the first or desired component. The total flow flowing in the channels 18 and 16 is caused to flow by means of the compressor 20, the variation of the composition remaining substantially unchanged in its cross section. As the total flow passes through the heat exchanger 22, heat is removed therefrom and as it passes through the separator 24 and below the duct 40, it is removed and, accordingly, more substance enters. The concentration of the desired component continuously increases along the circumference as it passes from the minimum at the main discharge point 38 to the maximum at the main feed point 36. The composition of the total flow of channels 16,18 with respect to the isotopic gas composition thus varies in the circumferential direction.

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It should be noted that the change in the total flow composition of the channel 18 immediately downstream of the deflection plate paths and flow junctions 42 at 44 will be somewhat stepwise because between the combined flow 50.1.52 and the combined sub-flows 50.2, 58.1, the combined sub-flows 50.2, 58 * 1 and the combined .3, 58.2 and between the combined partial flows 50 * 5 »58.2 and the combined flow 50 * 4» 58.3 there are stepwise differences in composition. The step nature of this change decreases as the flows and sub-flows mix due to diffusion at their interfaces as they pass through channel 18 and channel 16. The step size is clear between flow 52 and sub-flows 58.1 and decreases between adjacent flows in the circumferential direction so that the step difference in compositions * Between 5. Increasing the flows 50.1-50.4 through the channel 40 tends to slow down the disappearance of the step differences. Thus, as said flows and partial flows flow through the ring from the feed point 36 to the outlet 38, the step size of the change decreases towards a continuous change from minimum to maximum. As the total flow passes through the compressor 20, it rotates in the direction of rotation of the compressor blades 20.2, but the minimum and sweetness remain on opposite sides and the variation in the composition of the flow remains substantially unchanged.

As the total flow passes through the compressor 20, it compresses, as it passes through the heat exchanger 22 its temperature changes, and as it passes through the elements 26, the elements remove fluid from it to form enriched flows 56.1-56.4. The isotope-pilot compositions of the depleted streams and sub-streams 58.1-58.4 leaving the different sectors of the separator 24 thus differ from the compositions of the different combined streams and sub-streams from the channel 16 to the same sectors of the separator 24. The composition of the total flow through the separator to the channel 18 can thus be considered to be varied with respect to the concentration of the desired component by removing the fluid flowing therefrom as it passes through the separator 24. In addition, it should be noted that fluid is added to the total flow in channel 18 through feed point 36 and channel 40, and fluid is removed from channel 18 through main outlet 38.

The deflection plates at 44 deflect the flow of material through the channel 16. As the total flow passes the deflection plates at 44, the variation in the isotopic composition of its cross-section remains unchanged at 60505 miles when the fluid is removed, and the channels 38 and} 6 are added * The total flow in the channels changes its flow direction at both ends of the device 10 from channel 16 to channel 18 16 to channel 18. The flow thus flows in a closed ring.

The flow of the ring can be considered to originate from the flow through the main feed point 36, to which the flow from the subchannel 40.1 is added via the flow connection point 42. The combined flow 50.1.52 moves along the ring to the separator, where it is depleted by the elements 26. The remaining part of said flow, i.e. the impoverished flow 58.1, continues to flow along the ring until it reaches the deflection plates at 44 *. In this case it is divided into two experts, i.e. partial flows 58.1, which continue to flow around the ring. They are added from the channel 40.2 through the connection points at 42 and the combined sub-flows 58.1, 50.2 flow again along the ring to the separator 24, where they continue to impoverish. The depleted substreams 58.2 follow a similar cycle around the ring, adding the flow 50.3 from subchannel 4 & 3 at the flow junctions 42. The condensed substreams 50 * 3, 58.2 then flow to separator 24 where they further deplete to form a depleted flow 58 * 3 · Flow 58.3 enters flow junction in addition, the flow from the subchannel 40.4 50.4 * The combined flow 50-4, 58.3 makes the device the last turn for the separator 24, where it becomes impoverished for the last time. The depleted flow 58.4 then exits the main discharge point 58. It can be seen from the above that the flow 52 coming through the main supply point 36 circulates through the ring sectors 54, 54 * 1 of the device 10, after which it is divided into two flows. These currents run along the ring of channels formed by the channels 18,16, the paths moving circumferentially in opposite directions and passing in turn through the sector pairs 60, 60.1 and the sector pairs 62, 62.1.

This is most evident in Figure 3 · The distresses move away from each other until they finally converge and form a single track in sectors 64, 64.1 before being led out of the main outlet 38. The tracks are in said circumferential direction such that their helix axes run opposite two semicircles AND (65). ) from entry point 36 to exit point 38.

It is found that at the inlet of the duct 16 at the compressor 20, the total flow into the duct 16 can be considered as several different material flows into the duct 16, which are different in composition. The compressor 16 60505 ri 20 keeps them moving along the channel and they are physically separated in the separator 24 · When they leave the impoverished 24 in the channel 18, they can be considered to have been returned to the ring. Finally, flow 58.4 is physically separated from other flows (58.1, 58.2 and 58.5) at the point where it is removed from the ring via outlet 38.

Returning to Figure 1A again and comparing it to Figures 2 and 3, the following equivalents are observed:

The module, exemplified by the device 10 of Figure 1, may correspond, inter alia, to the four stages 2 of Figure 1A, i.e. one of the groups 9, the stages 2 of group 9 of Figure 1A are shown in Figures 2 and 3 by sector groups 54, 54 * 1; 60, 60.1; 62, 62.1 and 64, 64.1, the enriched flows 7 of Fig. 1A can be considered to correspond to the enriched partial flows 56.1-56.4 of Figs. 2 and 3, the depleted flows 8 of Fig. 1A can be considered to correspond to the depleted partial flows 58.1-58.4 of Figures 2 and 3 and 5 (Fig. 1A) and compressor 20 (Figs. 1-3) and heat exchangers 4 (Fig. 1A) and heat exchanger 22 (Figs. 1-3). The module 10 of Figures 1-3 thus corresponds to the group 2 of stages 2 as used in Figures 2 and 3 (Figure 1A). Thus, instead of the four compressors 5 and four heat exchangers 4 of the group 9 in Fig. 1Δ, one compressor 20 and one heat exchanger 22 are used (Fig. 1). Further, instead of the four separate separators 3 of Fig. 1A, one set of elements 26 formed by the separator 24 is used. In this case, it should be noted that in order to achieve the correspondence between Fig. 1A and Figs. 1, 2 and 3, all cascade arrangement modules 10 are intended to use elements 26 having a split ratio of 1/5 · with respect to the process gas.

In the representation of Figures 1, 2 and 3, the flow 52 with its various additions and removals can be seen circulating through the device four times in turn through sectors 54, 54.1, sectors 60. 60.1, sectors 62, 62.1 and sectors 64, 64.1.

In Fig. 4, reference numeral 66 generally indicates a flow diagram similar to that shown in Fig. 1 but adapted to a smaller number of revolutions. In Fig. 5, reference numerals 68 generally denote representations corresponding to Figs. 3A-3H for a device having the flow chart of Fig. 4.

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The enriched flow 70 from the second reverse module in series enters the device corresponding to Fig. 4 in two partial flows 70.1, 70.2 along a channel 40 with two subchannels 40.1, 40.2. At 42, there are thus two flow interfaces to duct 18, one for duct 40.1 downstream of feed point 36 and the other for duct 40.2 on the opposite side of the diameter from outlet 38 downstream. The depleted flow of the next module in the series comes through the supply point 36 in the form of a flow 72. The flow 72 circulates through the device twice instead of the four shown in Figure 2. The first cycle is made through sector 74 of compressor 20 and sectors 74 * 1 of heat exchanger 22 and separator 24. Before passing through the sector 74 »74 * 1, the flow 72 coincides with the partial flow 70.1 from the subchannel 40.1. After the combined flow 70.1, 72 has passed through the separator 24 and, as will be explained below, converted to a depleted flow 78.1, the deflection plates turn it at 44 to the opposite side of the channel 18.

The combined flow 70.1, 72 is divided in the sector 74 * 1 of the separator 24 into an enriched flow 76.1, which passes second in series to the next module through the subchannel 34 * 1 of the discharge channel 34, and to the depleted flow 78.1. The partition ratio of the elements 26 of sector 74.1 (and sector 80.1 below) with respect to the process gas is 1/5 * Channel 34 has two subchannels 34 · 1 »34 * 2, which lead to the next next module in series. The depleted flow 78.1 is reversed as shown above as it passes the deflection plates at 44 in the opposite position in the duct 18. Said flow 78.1 is combined with a partial flow 70.2 from the subchannel 40.2 and circulates the ring a second time through the compressor 20, heat exchanger 22 and separator 24. It passes through sector 80 of compressor 20 and sector 80.1 of heat exchanger 22 and separator 24. In sector 80.1 of separator 24, isotopic separation takes place in enriched flow 76.2, which exits along subchannel 34 * 2, and in depleted flow 78.2. The depleted flow 78.2 passes through outlet 38 to the next module in the series, and the enriched flow 76.2 continues to the next module in the series. Sectors 74 »74 · 1 and 80, 80.1 are thus substantially 180 ° sectors, while in the case of Figures 2 and 3, sectors 54 * 54 · 1 and 64, 64.1 are 90 ° sectors with sectors 60, 60.1 and 62, 62.1 being 45 ° sectors. .

In Fig. 6, reference numeral 82 generally denotes a flow diagram with a device 1a similar to that shown in Fig. 1 but adapted to a larger number of turns. In Fig. 7, reference numeral 84 shows representations generally corresponding to Figs. 3A-3H for the flow chart of Fig. 6.

The structure and operation of the device 10 represented by the flow charts of Figure 6 and Figure 7 are substantially similar to the device of Figures 1, 2 and 3. The main difference is that the deflection plates at 44 are arranged so that the depleted flow from the previous module in the series passes eight times through the compressor 20, the heat exchanger 22 and the separator 24 before leaving through the main outlet 38. Channel 40 has eight subchannels 40.1-40.8 and channel 34 has eight subchannels 34 · 1- 34.8. Channel 40 subchannels 40.1-40.4 carry four streams 88.1-88.4 from the previous module in the series and channel 34 subchannels 34.1-34.4 carry four enriched flows to the next module in the series. The subchannels 34 · 5-34 · 8 of channel 34 are connected directly to the subchannels 40.5-40.8 of channel 40. This combination is shown schematically in Figure 1 by dashed lines 89.

The sequential flow order is as follows: (a) Flow 86 enters channel 18 through inlet 36. The flow 86 is joined by the flow 90.1 from the subchannel 40.5 of the channel 40. The isotopic composition of flow 90.1 is substantially the same as that of flow 86. The combined flow 86, 90.1 circulates along the ring formed by channels 18,16 in the direction shown in Figures 1, 2 and 3 and enters compressor 20. It passes 45 ° to sector 92 of compressor 20 and heat exchanger. 22 and separator 24 via a 45 ° sector 92.1. The combined flow 90.1, 86 is divided into an enriched flow 94 * 1 in the elements of the separator sector 92.1 from said elements 26 to a compartment 32 and then from said sectors 92.1 of a compartment 32 through a flow junction to a subchannel 34 * 1 »and a depleted flow from said elements 26 26.2 to channel 18.

(b) The deflection plates divide the depleted flow into two partial flows at 44 which flow along the channel 18 towards the narrow part 18.1 on opposite sides of the feed point 36 and the flow 86. Said sub-flows 96.1 pass under the channel 40, whereby they are joined by parts of the flow 90.2 coming from the sub-channel 40.6 through the flow connection points 42. The combined partial flows 90.2, 96.1 circulate on the opposite sides of the combined flow 90.1, 86 in the ring and pass through a pair of sectors 9β of 22 l / 2 ° to the compressor 20 and pairs of sectors 98.1 of 22 1/2 ° of the heat exchanger 22 and separator 24. Sectors 98 are on opposite sides of sector 92 and sectors 98.1 are on opposite sides of sector 92.1 in heat exchanger 22 and separator 24. Elements of sectors 98.1 of separator 24 are separated by isotopes and said combined sub-flows 90.2, 96.1 are divided into enriched sub-flows 94 * 2 through the side discharge points to the compartment 32 and then through the flow connection points from the compartment sectors 98.1 to the subchannel 34 * 2 of the channel 34, and to the depleted partial flows 96.2 passing from the main discharge points 26.2 of the elements 26 to the channel 18.

(c) The depleted partial flows 96.2 run along the channel 18 on opposite sides of the depleted flow 96.1 until they reach the deflection plates at 44 »where they are deflected so as to continue along the channel 18 towards its narrow part 18.1 on the sides of the partial flows 96.1 farther from flow 86. As the beam currents 96.2 pass under the channel 40, they are joined by portions of a substantially similar flow 90.3 from the subchannel 40.7 through the flow connection points 42. The combined partial flows 90.3 »96.2 run on those sides of the combined partial flows 90.2, 96.1 which are further away from the combined flow 90.1, 86. Said combined partial flows 90.3» 96.2 enter the new 22 1/2 ° compressor 20 sectors 100 on the sides of the sector 98 which are further away from sector 92. The combined partial flows 96.2, 90.3 then pass through pairs of sectors 100.1 of the heat exchanger 22 and the separator 24 of 22 l / 2 °. Heat exchanger and separator sectors 100.1 are on those sides of sector 98.1 that are further away from sector 92.1. Isotopes are separated in the elements 26 of the sector 100.1 of the separator 24 and said combined partial flows 90.3 »96.2 are divided into enriched partial flows 94 · 3 from the side outlets of the elements 26 to the section 32 and then through the flow junctions from the sectors 32 to the section 96.3 »passing from the main outlets 26.2 of the elements 26 to the channel 18 on those sides of the partial flows 96.2 which are further away from the flow 96.1.

(d) The depleted sub-streams 96.3 run along channel 18 towards the Ben narrow section 18.1 on those sides of sub-streams 96.2 that are farther from the depleted stream 96.1. The deflection plates turn the depleted partial currents 96.3 at 44 so that they continue to pass along the channel 18 next to the depleted partial flows 96.2. As it passes under channel 40, the sub-flows 96.3 merge through the flow junctions 42 with portions of a substantially similar flow 90.4 from sub-channel 40.8. The combined sub-flows 90.4 »96.3 circulate along the ring on the sides of the combined sub-flows 96.2, 90.3 farther from the combined sub-flows 96.1, 90.2 and pass through a pair of 22 l / 2 ° compressor 20 sectors 102 and two 22 l / 2 ° heat exchangers 22 and separators. Through 24 sectors 102.1. Isotopes are separated in the elements 26 of the sector 102.1 of the separator 24 and said partial flows 90.4 »96.3 are divided into enriched partial flows 94 · 4 and depleted partial flows 96.4 · Enriched partial flows 94 * 4 pass through the side outlets of said elements 34 to the section · 4 · The depleted partial flows 96.4 pass through the main discharge points 26.2 of the elements 26 to the channel 18 on those sides of the depleted partial flows 96.3 which are further away from the depleted partial flows 96.2. The depleted sub-flows 96.4 flow along the channel 18 to the deflection plates at 44 »where they are deflected to continue their passage in the channel 18 on those sides of the depleted sub-flows 96.3» which are further away from the depleted sub-flows 96.2.

(e) At the point where the depleted sub-streams 96.4 fall below channel 40, they are joined by flow junctions 42 along sub-channel 40 of channel 40 along portions of a stream 88.1 of substantially similar isotopic composition from the previous module of the series. The combined sub-flows 96.4 »88.1 circulate along the ring on the sides of the combined sub-flows 96.3 * 9Ck4 farther from the combined sub-flows 96.2, 90.3 · The combined sub-flows 96.4 * 88.1 pass through a pair of sectors 104 of a compressor 20 of 22 1/2 adjacent to sectors 102. They then pass through a pair of 22 1/2 ° heat exchanger 22 sectors 104.1 to two 22 1/20 separator 24 sectors 104.1. Isotopes are separated in the elements 26 of the sector 104.1 of the separator 24 and said combined substreams 96.4, 88.1 are divided into enriched substreams 90.1 and depleted substreams 96.5 · Enriched substreams 90.1 pass through the side outlets of the elements 26 · The depleted substreams 96.5 pass from the main outlet points of the elements 26 to the channel 18 next to the depleted substreams 96.4 on those sides farther from the depleted substreams 96.3 * The depleted substreams 96.5 then pass along the channel 18 from partial flows 96.3 »for deflection plates to 44 * Sub-flows 96.5 depleted by deflection plates are deflected so that they continue to pass along channel 18 next to the depleted partial flows 96.4.

(f) At the point where the depleted partial flows 96.5 fall below the channel 40, they are joined by portions 40.2 along the sub-channel 40.2 of the flow from the previous module of the series of substantially similar isotopic composition 88.2. The combined partial flows 96.5 »88.2 pass through a pair of sectors 106 of a compressor 20 of 22 1/2 ° adjacent to sectors 104. The combined sub-flows 96.5 »88.2 then pass along duct 16 through two sectors 106.1 of the 22 l / 2 ° heat exchanger 22 adjacent to sector 104.1 to two 22 1/2 ° separator 24 sectors 106.1 adjacent to sectors 104-1. In the elements 26 of the sector 106.1 of the separator 24, isotope separation takes place and said combined partial flows 96.5 »88.2 are divided into two enriched partial flows 90.2 and two depleted partial flows 96.6. The enriched partial flows 90.2 pass through the side outlets of the elements 26 to the compartment 32 and then from the sectors 106.1 of the compartment 32 through the flow connection points to the subchannel 34 * 6 of the channel 34. The depleted sub-streams 96.6 run into the channel 18 and along the channel 18 adjacent to the depleted sub-streams 96.5 and on the sides farther from the depleted sub-streams 96.4.

(g) At the point where the entrained partial flows 96.6 fall below the channel 40, they are joined by portions 40.3 of the flow from the previous module of the series through the flow junctions 42 along the subchannel 40.3 with a substantially similar isotope composition. The combined partial flows 96.6, 88.3 pass along the channel 18 to the compressor 20. Said combined partial flows 96.6, 88.4 pass through a pair of sectors 108 of the 22 1/2 impeller 20 adjacent to the sectors 106. The combined sub-flows 96.6, 88.3 then pass through two sectors 22.1 of the 22 1/2 ° heat exchanger 22 adjacent to its sector 106.1 to the two 22 1/2 ° separator 24 sectors 108.1 adjacent to this sector 106.1. Isotopes are separated in the elements 26 of the sector 108.1 of the separator 24 and said combined substreams 96.6, 88.3 are divided into two enriched substreams 22 60505 90.3 and two depleted substreams 96 · 7 * The enriched substreams 90.3 pass from the flow through the junctions of the channel 34 to the subchannel 34 · 7- The depleted partial flows 96.7 pass into the channel 18 and flow along it next to the depleted partial flows 96.6 on the sides farther from the depleted subflows 96.5 to the deflection plates so as to divert its flow along channel 18 adjacent to the depleted partial flows 96.6.

(h) At the point where the partial flows 96.7 fall below the channel 40, they are joined by parts of a flow 88.4 of substantially similar isotopic composition from the previous module of the series through the flow connection points 42 along the sub-channels 40.4. The combined partial flows 88.4, 96.7 then flow along the channel 18 to the compressor 20. It is observed that after the depleted partial flows 96.7 have passed the deflection plates at 44, they merge into one depleted flow flowing along the channel 18 adjacent to the depleted partial flows 96.6 between them. The combined flow 88.4, 96.7 passes through sector 110 of a 45 ° compressor 20. Thereafter, said combined partial flow 96.7, 88.4 passes through a sector 110.1 of a 45 ° heat exchanger 22 and enters a sector 110.1 of a 45 ° separator 24. Sector 110 is between sectors 108 and sectors 110.1 are between a pair of sectors 108.1 of a heat exchanger 22 and a pair of sectors 108.1 of a separator 24, respectively. In the elements 26 of the sector 110.1 of the separator 24, isotope separation takes place and said combined flow 96.7, 88.4 is divided into an enriched flow 90.4 and a depleted flow 96.8. The enriched flow 90.4 passes through the side outlets of the elements 26 to the compartment 32 and then from the sectors 110.1 of the compartments 32 through the flow junction to the subchannel 34 · 8 of the channel 34. The depleted partial flow 96.8 passes from the main outlets 26.2 of the elements 26 of the sector 110.1 of the separator 24 to the channel 18 between the depleted partial flows 96.7. Said depleted partial flow 96.8 runs along one sector of the channel 18 between the depleted partial flows 96.7 and leaves the main discharge point 38.

It should be noted that, as in Figures 2 and 4, sector pairs 98,100,102, 104,106,108 and sector pairs 98.1, 100.1, 102.1, 104 * 1, 106.1 and 108.1 are shown in Figure 6 as a single sector for clarity. The isotopic compositions of the various streams flowing through the device corresponding to flow diagram 82 are arranged so that the isotopic compositions of enriched streams 90.1 to 90.4 correspond to the isotopic compositions of stream 86 and depleted ocean streams 96.1 to 96.3, respectively. The flow of flows 90.1-90.4 from subchannels 34 · 5-34 * 8 to subchannels 40.5-40.8 means an internal multiplier with respect to hardware 82. The enriched flows 94 * 1-94.4 correspond to flows 88.1-88.4 and pass to the next module in the series. The depleted flow 96.8 corresponds to flow 86 and flows to the previous module in the series.

As with Figures 2 and 3, the elements 26 of Figure 1 described in connection with Figures 4-7 have a split ratio of 1/5 with respect to the process gas.

Figures 4 and 5 and Figure 1A correspond to each other as follows:

The module 10 of Fig. 1 corresponding to Figs. 4 and 5 includes kakei stage 2 (Fig. 1A), i.e. a group of half (or half of such a group 9) of each group 9 of Fig. 1A »the group of Figs. 4 and 5 form two stages 2 (Figs. 1A ) are shown in Figures 4 and 5 as sector groups 74 »74 * 1 resp. 80, 80.1, the feed streams 6 of Fig. 1A can be considered the flows 70.1, 72 and 70.2, 78.1 of Figs. 4, 5 the enriched flows 7 of Figs. 4 and 5 can be considered the enriched flows 76.1, 76.2 and sub-flows 78.1 78.2.

Examining Fig. 1A, it is also observed that the supply flows 70 * 1, 70.2 of the module 10 corresponding to Figs.

Figures 6 and 7 and Figure 1A correspond to each other as follows:

The module 10 of Figure 1 corresponding to Figures 6 and 7 includes eight stages 2 of Figure 1A, i.e. it includes a group with twice as many stages as in group 9 (or two such groups 9) of Figure 1A, the group of figures 6 and 7 forming eight stages 2 is shown in Figures 24 60 5 0 5 sa 6 and 7 as sector groups 92, 92.1; 98, 98.1; 100, 10Q1; 102, 102.1; 104, 104.1; 106, 106.1; 108, 108.1 and 110, 110.1, the flows 86, 90.1 of Figs. 6 and 7 can be considered as the feed flows 6 of Fig. 1A; 96.1, 90.2; 96.2, 90.3; 96.3, 90.4; 96.4, 88.1; 96.5, 88.2; 96.6, 88.3 and 96.7, 88.4, the enriched partial flows 94-1-94 * 4 and 90.1-90.4 of Figs. 6 and 7 can be considered as the enriched flows 7 of Fig. 1A and the depleted partial flows 96.1-96.8 of Fig. 6 can be considered as the depleted flows 8 of Fig. 1A.

As with Figures 2 and 3, in Figures 1 and 4-7, in stages 2, compressors 5 (Figure 1A) correspond to compressor 20 (Figures 1 and 4-7) and heat exchangers 4 (Figure 1A) correspond to heat exchanger 22 (Figures 1 and 4-). 7) · Thus, the module 10 of Figure 1, when used as shown in Figures 4 and 5, includes half of the group 2 of degrees 2 (or a group half the size of said group 9) (Figure 1A). Instead of two compressors 5 and two heat exchangers 4 (Fig. 1A), one compressor 20 and one heat exchanger 22 (Fig. 1) are thus required. Similarly, module 10, when used as shown in Figures 6 and 7, includes two groups 9 of degrees 2 (or a group that is twice the size of group 9) (Figure 1A). One compressor 20 and one heat exchanger 22 thus replace the eight compressors 5 of Figure 1A and the heat exchanger 4-

In addition, it can be seen from Figures 4 and 5 and 6 and 7 that instead of several separators 3 in Figure 1A, one separator 24 can be used.

The invention has been described with particular reference to a gas isotope separation device. Device 10 forms a cascade-type series module of such devices. Figure 1 shows one device 10 and the idea is that the modules 10 are substantially similar throughout the cascade arrangement. Thus, the overall dimensions and relative positions of the housings 12,14, the compressor 20, the heat exchanger 22, the separator 24 and the compartment 32, the inlet 36 and the outlet 38, and the channels 34,40 are substantially similar in each module. However, as the cascade of modules progresses from the feed stream to the cascade toward either the final outgoing enriched flow or the final outgoing depleted flow along the cascade, the forward and reverse mass flows decrease. Thus, to handle the total mass flows of the four-stage group 9, several modules 10 may be needed in a block close to the cascade feed flow.

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In the middle of the cascade, perhaps one module 10 may handle the total mass flow of the four degree group 9 and near the final outlet of the enriched or impoverished flow of the cascade, one module 10 may process more than the total mass flow of the four degree group 9.

As shown in Figures 2 and 3, the module 10 may include a four-stage array 9 of the cascade array 1, which includes four enriched flows (50.1-50.4) from the previous module or group and one depleted flow 52 from the next module or group in the series. This may represent the module in the middle of the cascade arrangement.

On the other hand, Figures 4 and 5 show flow diagrams with module 10, which receives two enriched flows 70.1 and 70.2 from the module, one backwards, respectively, and one depleted flow 72 from the next module. Figures 4 and 5 may thus represent a module near the beginning of the cascade arrangement, in which the device 10 can process about half of the four-stage group 9 colonial mass flow. Thus, two devices 10 forming a group of stages 9 can be used to handle the total mass flow (Figure 1A). The enriched flows (four) from the previous group of stages flow to said two modules 10 and the depleted flow (one) from the next group of stages 9 flows from one of said two modules 10. The module 10 of Figure 1 in connection with Figures 1A, 4 and 5 thus includes a group 9 half.

Figures 6 and 7 show flow diagrams for a location near the end of the cascade arrangement. At this point, the device 10 of Figure 1 can handle twice the total mass flow. In connection with Figures 6 and 7, the device 10 thus includes two groups 9 of the cascade arrangement (Figure 1A). In fact, sectors 92.99 * 100 and 102 together with sectors 92.1, 98.1, 100.1 and 102.1 include the higher group 9 of module 10 and sectors 104, 106, 108 and 110 together with sectors 104 · 1, 106.1, 108.1 and 110.1 include the lower group 10 group 9. Thus, said enriched flow (88.1-88.4) from the previous stage group of the cascade arrangement (in different module 10) enters said lower group and the depleted flow 96 * 4 in the form of two partial flows from said higher group and its enriched effluent flows (90.1-90.4) go to said higher group with the depleted effluent 96.8 passing to said previous group. Correspondingly, said higher group becomes the enriched flows (90.1-90.4) from said lower group and the depleted flow (86) from the next group in the series (in the second module) and its enriched effluents flow into said next group of the series. as its depleted effluent (96.4) passes into said lower group.

Thus, as it travels along the cascade arrangement from the incoming feed stream toward the final enriched or depleted effluent stream (a) (Figures 4 and 5) · (u) As the cascade arrangement progresses per group of stages, the number of modules required decreases until one module is needed to handle the total mass flow (Figures 2 and 3) and (c) as the end of the cascade progresses, one module 10 may contain two or more groups ( Figures 6 and 7) ·

Figures 8 and 9 show another device for treating a fluid according to the invention. Unless otherwise shown in the figures, the same reference numerals as in Figure 1 have been used.

Thus, reference numeral 10 generally indicates a device having an inner housing 12 and an outer housing 14 around the inner housing 12. Inside the inner housing 12 there is a substantially cylindrical central member 112 and the outer housing 14 is inside a cylindrical vessel or container 114.

The housing 12 and the central member 112 are coaxial and form an annular channel 16 therebetween. The housings 12,14 in turn form an intermediate channel 18, which is also annular. The opposite ends of the channel 16 open radially to the opposite ends of the channel 18. The channels 16, 18 thus form an endless channel or ring having an inner annular portion formed by the channel 16 and an outer annular portion formed by the channel 18 within which the inner portion is located.

The duct 16 has an axial compressor 20 at one end 114 »1 of the tank 114. The compressor 20 has a shaft 20.1 and vanes 20.2. The shaft 20.1 is coaxial with the channels 16,1Θ and protrudes from the outside of the container 114 inwards at said end 114 · 1 ·

The duct 18 has a porous heat exchanger element 22 at the opposite end 114.2 of the container 114, where the duct 16 extends radially into the duct 16.

The heat exchanger 22 is annular.

27 60505

The separator 24 is likewise annular and is located in the duct 18 and extends from the heat exchanger 22 towards the end of the tank 114 * 1, being in the shape of a truncated cone tapering towards the heat exchanger 22. The gas isotope separation elements 26 corresponding to the elements 26 of Figure 1 are located in the separator 24 *

The portion of the duct 18 between the heat exchanger 22 and the separator 24, indicated by reference numeral 18.1, is located radially outward from the separator 24 to the separator and between the housing 14. The part of the duct 18, indicated by reference numeral 18.2, as seen from the heat exchanger 22 on the other side of the separator 24 is located radially inwards from the separator 24 between the separator 24 and the housing 12.

The feed points 26.1 of the elements 26 of the separator 24 communicate with the duct 18 through the partition 28 directed towards the part 18.1 of the duct 18. The main discharge points 26.2 of the separating elements 26 communicate with the part 18 18 of the channel 18 between the separator 24 and the housing 12 through the partition wall 30. The compartment 32, inside which the separator 24 is located, has an outlet channel 34 »formed by an annular compartment running around the housing 14 at the end 114 * 1 of the container 114. The side discharge points of the gas separator elements open into the channel 34 * The channel 34 has twelve circumferentially outwardly projecting discharge points 116 at regular intervals on the circumference.

The main feed point 36 enters the channel 18 at the end of the container 114 in the axial direction 114 * 1 outwards from the ring of the outlet points 116. On the opposite side of the supply point 36 there is a main outlet point 36 »which is also connected to the channel 18.

The auxiliary supply passage 40 is annular and extends around the shaft 20.1 of the compressor 20 in the axial direction outwards from the compressor 20. The passage 40 is bounded by a cam formation 118 projecting coaxially from the end 114.1 of the container 114. The cam formation 118 is bolted to the end of said container 114 and has an end plate 118.1 from which the shaft 20.1 projects outwards in the axial direction, said end plate 118.1 being provided with sealing members 118.2.

28 60505

The cam assembly 118 and the mounting member 122 at the compressor 20 end of the central member 112 have bearings 120 for the shaft 20.1.

The duct 40 has an axial compressor 124 with vanes 124.1 mounted on the shaft 20.1. The channel 40 has 12 feed points 126 which are circumferentially spaced apart and are associated with channels 126 in the cam formation 118 which open radially outward. The channel 40 opens axially to the channel 16 at a point where the channel 18 communicates radially with the channel 16 at the end of the container 114 114 * 1 ·

The end of the central member 112 is connected to the end 114-2 of the container 114 by a bellows member 130 of the access opening cover 128, which can expand and collapse. Compressor 20 has a diffuser 131 at the outlet *

As shown in particular in Figure 9, the duct 16, heat exchanger 22, separator 24 and duct 18 are divided into axial compartments by a plurality of spaced axially circumferentially spaced partitions 132. The figure shows 48 with the number 48 of partitions 132 typically suitable for use with separator 24, with a division ratio of approximately l / 20.

The partitions are provided with deflection means adapted to deflect the flow of material flowing along the ring formed by the channels 16, 18 in the circumferential direction with respect to said channels. The deflection members are in the channel 18 at 134 · The schematic representation of Fig. 10 shows by way of deflection means as breaks in the partitions 132 at 138, the deflection plates 140 forming parts of said partitions 132 forming a circumferential angle with the rest of said partitions 132, thus allowing flow between the two partitions 132 from one compartment to another compartment between a different pair of partitions.

The operation of the module 10 of Figures 8 and 9 is substantially similar to that of the module of Figure 1. The enriched flow from the previous module or modules of the series and / or the recirculating gas from the outlet 116 passes through the channel 40 in the form of a partial flow of 12 through the supply points 126 to the channel 40. Said enriched flow passes through a compressor 124 and enters a duct 16 located upstream of the compressor 20.

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The depleted flow from the next module 10 in the series comes through the main supply point 36 of the channel 18. This depleted flow flows radially inwards into the duct 18 and thence into the duct 16 and the compressor 20. Said impoverished flow from the following modules travels axially along the duct 16 to the end 114 * 2 of the duct housing 114 using its own duct 16 sector. It passes through the heat exchanger 22 to the duct 18 part 18.1, from there to the separator 24 and from there its depleted part passes in the direction of the arrows shown in the duct 18 part 18.2 and its enriched part passes into the duct 34 ·

It should be noted that the sector used by the depleted flow from the next module through the main supply point 36 may consist of several compartments between the partitions 132. In the deflection plates 140, the impoverished flow mentioned at point 134 of the channel 18 is divided into two parts which continue to flow along the ring in their respective sectors on opposite sides of the sector used by the impoverished flow coming through the main feed point 36. In this regard, it should be noted that the entire length of the partitions 132 is not parallel to the polar axis of the module 10. They are shaped to form an angle with said axis so that the compartments formed between the partitions discharge into the relevant sectors or sectors of the compressor 20. The purpose of this partition arrangement is to compensate for the rotation of the gas flow around said axis caused by the compressor as the flow passes through the compressor. Said two depleted flow sections continue to flow along their helical paths in opposite directions in the circumferential direction around the module 10, as described in connection with Figure 1, until they finally reunite and come out of the main outlet 28 as a depleted flow of the module 10 to the previous module in the series.

Comparing FIGS. 8 and FIG. which enter the channel 40 via the feed points 126 are arranged so that the compressor 124 feeds them to the compressor 20 feed point at positions where their isotopic composition is similar to that of the compressor 20 feed point from the flow from the channel 18.

30 60505

It will be appreciated that the module 10 of Figure 1 may also be provided with partitions similar to the partitions 132 shown in Figures 8 and 9. The partitions divide the ring into a plurality of compartments running along the ring. These compartments may, although not necessary, correspond to the sectors used in the ring by the different currents and partial flows flowing along the ring.

The use of partitions 132 reduces the mixing caused by diffusion or turbulence at the interfaces of said flows as they flow along the ring. The more partitions 132 there are, the less mixing occurs. Thus, in general, as many partitions as possible are used, with the practicality of the structure and economic considerations limiting the total number.

In general, the steeper the circumferential concentration gradient in the ring formed by the channels 16 and 18, the more important the partitions 132 are when said partitions prevent mixing and the disappearance of the concentration gradient as described above. Thus, in a module that includes only a few stages 2, e.g., two stages as shown in Figure 5, the partitions, although desirable, may not be necessary. In modules involving many degrees, e.g. 10, which number may be typical for division ratios of 1/10 or less, the importance of the partitions increases.

In the case of Figure 1, where there are no partitions, it is desirable that the heat exchanger 22 and the tapered portion of the duct 16 have an axially cylindrical central member 112 (dashed lines) extending from the shaft 20.1 to the compartment 32 in the central member 112 of Figures 8 and 9, respectively. The purpose of this central member is to prevent mixing of the flows flowing on opposite sides of the channel 16.

In the examples shown in connection with Figures 1-7, elements 26 with a split ratio of 1/5 and in which the enriched and depleted flows are at the same pressure have been used. In cases where the enriched flows 7 of steps 2 (Figure 1A) are at a different pressure than the depleted flows, lower pressure flows may be passed through the auxiliary compressor before joining the other flows to equalize the pressures, then pass through the common compressor 20 and common heat exchanger 22 (Figure 1). Thus, for example, an auxiliary compressor can be placed in the channel 40 of Fig. 1 when the flows 50 (Fig. 2) are at a lower pressure than the flows 52 and 58 »or an additional compressor can be placed in the section 16.2 of the channel 16 when said flows 8 and 9 have an additional compressor. shown at 124 corresponding to the case where the flows 50 are at a lower pressure than the flows 52 and 58.

It is further contemplated that the module 10 need not include an integer number of degrees groups or a group or groups having an integer number of degrees. Thus, it is conceivable that an arbitrary number of groups or portions thereof, including an arbitrary number of degrees or portions thereof, may be included in the module. Appropriate flow interfaces are established as needed. Thus, the method and apparatus are not limited to any particular division ratios, e.g., 1/3, 1/4, or 1/5, but an arbitrarily small division ratio of 1/20 or less can be used.

It should also be noted that the deflection plates need not necessarily deflect the flow from a particular compartment to an adjacent or other designated compartment. In practice, the deflection plates can reverse the flow from the compartment an arbitrary amount as long as the deflection is large enough to reverse the flow to the adjacent sector, bearing in mind that the sectors do not have to correspond to the compartments between the partitions 132. The amount of deflection of the deflection plates actually depends on the equilibrium aspects of the mass flow in the module 10, i.e. the magnitude of the impoverished flows flowing between the modules.

A further advantage of the invention is that standardization of modules is possible. In addition, isotope separation may require compression (causing the flow to pass through the compressor to keep it moving) and heat transfer (e.g., cooling the flow after compression) whenever the flow has passed through the isotope separation elements. A further advantage of the invention is that each module has one compressor 20 and one heat exchanger 22 for internal circulation, regardless of the number of different gas flows flowing or countercurrently through the cascade arrangement and through the module. If necessary, each module also has only one compressor 124 to equalize the pressures between the enriched flows entering the module and the internal circulating flows. Thus, the use of multiple compressors and heat exchangers (at least one for each stage shown in Figure 1A) is avoided and relatively few compressors and heat exchangers of the same type can be used. When partitions are used, the only parts of the ring in which the different flows and partial flows come into contact with each other are the part of the tire with the compressor 20 and the part of the tire where the deflection plates 140 are located. In the case of Figures 8 and 9, contact also occurs at the point where the compressor 124 is located with respect to the enriched flows from the previous module. The function of the partitions 132 is thus to reduce the mixing between adjacent flows and sub-flows while maintaining the advantages of having one compressor 20, possibly one compressor 124, one heat exchanger 22 and one separator 24 for each module 10.

The use of the method and module of the invention at a split ratio of about 1/20 235 in the enrichment of uranium hexafluoride (UF 2) to U is expected to result in a reduction in plant costs of at least about 20% and possibly 50% or more. The reduction in efficiency due to diffusion-induced gas mixing at the points where the gas flows and their partial flows are in contact with each other is believed to be less than 10% compared to conventional cascade arrangements and the savings from standardized and relatively large modules are more than offset by the cost of the modules.

Claims (24)

33. . 60505 A method for treating a fluid, characterized in that a channel flow containing only one phase is fed into the channel (16, 18) and its composition varies in a known manner with respect to its specific property in a cross-section of the flow perpendicular to the direction of flow by passing it through an impeller or propeller (20) located in the channel downstream of the feed point, without eliminating the flow composition variation, and before at least some portions of the flow are separated through the impeller or propeller through the impeller or propeller; , which have different compositions compared to each other, and are removed from the channel. A method according to claim 1, characterized in that the variation of the composition is substantially continuous. Method according to claim 1, characterized in that the variation of the composition is substantially stepwise. Method according to one of Claims 1 to 3, characterized in that the channel has an annular cross-section with a circumferential flow composition varying from one minimum to one maximum with respect to a given characteristic, the minimum point and the maximum point being circumferentially spaced apart. Method according to one of the preceding claims, characterized in that the impeller or propeller is an impeller or propeller (20) which provides axial flow. A method according to any one of the preceding claims, characterized in that it comprises changing the temperature of the flow medium before separating said parts of the flow from each other and after the flow has been fed into the channel. Method according to Claim 6, characterized in that the temperature of the fluid is changed by means of a porous heat exchanger element (22) extending across the duct. Method according to one of the preceding claims, characterized in that the fluid is removed from the stream by an isotope separator (24), 34 6050S, which changes the isotopic composition of the stream. Method according to one of the preceding claims, characterized in that the fluid is removed from the flow or added to the flow by means of lines (34, 40) which open from the channel to the channel. Method according to one of the preceding claims, characterized in that partitions (132) running parallel to the flow are used in a part of the channel to separate the parts of the flows from each other, thus preventing the variation in the composition of the flow from disappearing. Method according to one of the preceding claims, characterized in that the channel forms an endless ring or the part along which the flow moves, at least part of the flow circulating around the ring more than once. A method according to claim 11, characterized in that the fluid passes around the ring as it flows following different helical paths! the axis of each helical track being perpendicular to the direction of flow along the channel and the complete loop of each helical track extending over the entire length of the ring. A method according to claim 12, insofar as claim 12 is dependent on claim 4, characterized in that there are two helical tracks running in circumferential directions in opposite circumferential directions with respect to the circumference of the channel, represented by a cross-section through the channel perpendicular to the channel, from a minimum point to a maximum point with each track passing more than once around the ring, the other track comprising substantially half of the channel and the other track comprising the other side. A method according to claim 13, characterized in that it comprises deflecting the flow of at least part of the flow in the channel to direct the flow of material to said helical paths. A method according to claim 14, characterized in that the ring is formed by an inner cylindrical housing (L2) extending inside the outer cylindrical housing Ö.4) when opposite ends of the inner housing open at opposite ends of the outer housing, the helical tracks having axes extending perimeter in opposite directions with respect to the housings from minimum to maximum. 35 60505 Apparatus (10) for treating a fluid, characterized in that it has means (12, 14) forming a ring comprising a channel (16, 18), at least one inlet (36) to the ring and at least one outlet (38) a ring, an impeller or a propeller (20) for causing a single phase flow of material to flow along the ring and circulating at least one portion of the flow more than once around the ring, said inlet and outlet and said impeller or propeller being arranged so that said portion or portions each run helically , the axis of each helical track being perpendicular to the direction of flow along the channel and the complete loop of each helical track extending over the entire length of the ring. Device according to claim 16, characterized in that it comprises deflection means (140) for deflecting the fluid flowing along the ring to cause said part or parts to run along said path or paths. Device according to Claim 16 or 17, characterized in that it comprises in the part of the channel one or more partitions (132) running in the direction of flow. Device according to one of Claims 16 to 18, characterized in that the impeller or propeller (20) is an impeller or propeller provided by axial flow. Device according to any one of claims 16 to 19, characterized in that it comprises a porous heat exchanger element (22) extending across said duct to change the temperature of the material flow as it flows along the ring. Device according to one of Claims 16 to 20, characterized in that the channel is annular, one sector of the channel having a main feed point (36) and the circumferentially spaced channel sector having a main outlet point (38) for distributing the fluid entering the main feed point into two parts running along different helical paths around the ring to the main discharge point. Device according to claim 21, characterized in that the ring is formed by an inner cylindrical housing (12) extending inside the outer cylindrical housing (14) as the opposite ends of the inner housing open to the opposite ends of the outer housing. Method according to one of Claims 16 to 22, characterized in that the ring includes an isotope separator (24) for separating the isotopes of the substance flow as it flows along the ring. Device according to one of Claims 16 to 23, characterized in that a plurality of spaced-apart partial feed points (42, 126) lead to the ring and that a plurality of spaced-apart partial discharge points (34, 16) leave the ring. 37 60505