阅读说明：本技术 用于使用串联的n个塔的模拟移动床分离方法的使用子午线嵌板的新式分散系统 (Novel dispersion system using radial panels for simulated moving bed separation process using N towers in series ) 是由 A.罗永-勒博 F.奥吉耶 于 2018-10-17 设计创作，主要内容包括：本发明描述了一种模拟移动床分离单元的流体分散和收集装置,该单元包括N个板,这N个板自身划分为子午线嵌板,装置使得有可能针对流体的每个部分维持近似相同的停留时间。(The invention describes a fluid dispersion and collection device for a simulated moving bed separation unit comprising N plates which are themselves divided into radial panels, the device making it possible to maintain approximately the same residence time for each part of the fluid.)

1. A dispersion and collection device for a simulated moving bed separation unit, the diameter of the unit being greater than 4 meters, the unit comprising at least one column divided into N adsorbent beds, each bed being divided into radial panels, i.e. panels that are parallel and contiguous to each other so as to ensure complete coverage of the cross section of the bed, the dispersion and collection device comprising dispersion channels (4) and collection channels (8), and each panel being fed by a dispersion channel (4) and the extraction of effluent from the panel taking place via a collection channel (8), the height of the dispersion channels (4) and of the collection channels (8) surrounding each panel varying linearly over the entire length of the panel and such that the inlet velocity of each part of the fluid in the bed remains the same from the inlet section of the panel to its outlet section of the panel, and such that the sum of the heights of the dispersion channels and the collection channels taken at any point along the length of the panel remains constant.

2. A dispersion and collection device for a simulated moving bed separation unit according to claim 1, comprising an outer peripheral duct, wherein the transfer of the fluid from plate N to the next plate N +1 is carried out by means of a peripheral duct outside the column, and which makes it possible to connect the various collection channels of the plate N to the various dispersion plates of the plate N +1, said duct making it possible to carry out the injection of raw materials and solvents and the extraction of extracts and raffinates.

3. A dispersion and collection apparatus for a simulated moving bed separation unit according to claim 2, wherein dispersion of the fluid throughout each panel occurs by successively dividing two streams originating from the outer perimeter conduit (10) into a set of two inlets (14) for supplying adjacent panels, and further collection of the effluent from the bed N occurs by combining the outlets (13) of two adjacent panels two by two feeding the outer perimeter conduit (10) of the bed N + 1.

4. A dispersion and collection apparatus for a simulated moving bed separation unit according to claim 1 comprising a dispersion manifold (15) and a collection manifold (16), wherein dispersion of the fluid throughout each panel occurs from a dispersion manifold (15) that directly supplies a respective inlet (14) of each panel, and collection of the effluent from the bed N occurs directly in the same manner by means of a collection manifold (16) that recovers the effluent from the outlet (13) of each panel.

5. A method of using a dispersion and collection device according to any one of claims 1 to 4, in which an incoming fluid is introduced into each panel of the plate N by means of inlet ducts (14), each inlet (14) supplying a dispersion channel (4) whose height is greatest at the inlet of the channel and smallest at the outlet of the channel, each portion of fluid supplying a portion of the bed of particles immediately below the dispersion channel, and the portion of fluid leaving the bed of particles for entry into the collection channel (8) immediately below the bed of particles, the collection channel having its greatest height at the outlet, an outlet effluent then being recovered by means of the outer peripheral duct (10) and reintroduced into the dispersion channel of the bed N +1 via the inlet (14) of the bed N +1, the method is characterized in that: the residence time taken by each portion of fluid from the inlet to the outlet of the plate N is the same for each portion of fluid, and the outer peripheral ducts (10) do not add any dispersion to this residence time.

6. Use of the dispersion and collection device according to claim 1 for a process for the separation of xylenes in a simulated moving window, said simulated moving bed operating with a number of beds, said number being between 4 and 24 and preferentially between 8 and 12.

Technical Field

The present invention relates to a device for introducing and collecting fluids in a process for separating xylenes in a simulated moving bed (abbreviated to SMB) and to a unit using said process, more particularly a unit of large diameter (D >4 m) and having a plurality of separation stages, in which the product is injected or withdrawn between two stages.

The device according to the invention has the distinctive feature of complying with a residence time which is more or less equal for all fluid particles entering the dispersion channel, passing through the bed and being discharged via a collection channel symmetrical to the dispersion channel.

Background

The current technology for separation by simulated moving bed (abbreviated SMB in the remainder of this document) uses units with a certain number of common features:

a series of adsorbent beds, within which a "pump-around" stream flows. The pump-around flow generally represents several times (approximately between 1.5 and 6 times) of the incoming feedstock flow.

A system for injecting raw materials and solvents and for extracting the effluents, known as extracts and raffinates,

-a collection and re-distribution system for transfer from one bed to the next.

In processes for separation by simulated moving bed adsorption, there are generally multiple beds located in one or two adsorption columns. Located between each bed is a disperser-mixer-extractor or "DME" panel (panel) supplied by a line, which typically has the shape of a "dispersing/extracting spider". Each DME panel located between two successive beds is connected to the outside by means of one or two pipes or networks leading to valves which successively place each bed in communication with each stream entering or leaving the adsorption zone. This operation is performed sequentially and the time to return to the initial bed at the end is called the cycle time, which is an important element of the process.

For example, patent US2985589 explicitly shows that each injection or extraction network is connected via a single line to a valve which connectively connects the feedstock, extract, solvent and then raffinate. A disadvantage of this way of proceeding is that the performance of the process is greatly reduced, since each stream is thus contaminated by the contents of the common line. Therefore, it is essential to install a flushing system.

Several patents explain how these flushing operations are carried out, in particular the patents FR275188, FR2772634, FR 2870751.

Flushing operations generally prove to be expensive in terms of investment (additional valves and lines) and also in terms of operating costs (yield, productivity).

The "dispersion/extraction spiders" constitute obstacles within the adsorbent bed that interfere with the flow in the bed. Patent WO09133254 shows how to minimize the effect of obstacles on the fluid dynamics in the bed.

Augier et al in 2008 (Separation and Purification Technology 63, pages 466 to 474) paper evaluated the cost of obstacles.

Disclosure of Invention

The invention can be defined as a dispersion and collection system/device for a simulated moving bed separation unit, said unit having a diameter greater than 4 meters, preferably greater than 7 meters, comprising at least one separation column divided into N adsorbent beds supported by plates N, each plate N itself being divided into radial panels, i.e. panels that are parallel and contiguous to each other so as to ensure complete coverage of the cross section of the bed, and each panel being fed by a dispersion channel (4).

The extraction of effluent from the panels occurs via collecting channels (8), the height of the dispersing and collecting channels surrounding each panel varying linearly throughout the length of the panel, and such that the inlet velocity of each portion of fluid in the bed remains the same from the inlet section of the panel to its outlet section of the panel, and such that the sum of the heights of the dispersing and collecting channels taken at any point along the length of the panel remains constant. For purposes of clarity in various dimensions of a channel, length refers to the dimension of the channel corresponding to the distance separating the inlet of the channel from its outlet, the width of the channel refers to the horizontal dimension perpendicular to the length, and the height refers to the vertical dimension perpendicular to the length.

More specifically, the height of the dispersion channel decreases linearly from the inlet to the outlet, and the height of the collection channel increases linearly from the inlet to the outlet.

At each abscissa x corresponding to a standard point M on the length of the panel, the sum of the heights of the dispersion channel and of the collection channel is constant.

The dispersion and collection system according to the invention uses a peripheral duct (10) external to the column which makes it possible to connect the various collection channels of plate N to the various dispersion plates of plate N +1, said duct making it possible to carry out the injection of raw materials and solvents and the extraction of raffinate and extract.

In a first variant of the dispersion and collection system for SMB separation units according to the present invention (shown in figure 2), the dispersion of the fluid throughout the various panels of bed N occurs by successively dividing the two streams originating from conduit (10) so as to supply the inlets (14) of the two adjacent panels, and the collection of the effluent from bed N also occurs by combining the outlets (13) of the two adjacent panels two by two, feeding the conduit (10) of bed N + 1.

In a second variant of the dispersion and collection system for SMB separation units according to the invention (shown in figure 3), the dispersion of the fluid throughout the various panels of the plate N occurs from a dispersion manifold (15) directly supplying the various inlets (14) of each panel, and the collection of the effluent from the bed N occurs directly in the same way by means of a collection manifold (16) recovering the effluent from the outlets (13) of each panel.

The invention also relates to a method for using a dispersing and collecting device according to the invention, in which method, introducing the incoming fluid at the plate N into each panel of said plate N by means of an inlet duct (14), each inlet (14) supplying a dispersion channel (4), the height of the dispersion channel being greatest at the inlet of said channel and smallest at the outlet of said channel, each portion of the fluid supplying a portion of the bed of particles immediately below the dispersion channel, and said portion of the fluid leaves the particle bed to enter a collection channel (8) located immediately below the particle bed, said collection channel having its maximum height at the outlet and its minimum height at the inlet, the outlet effluent then being recovered through an outer peripheral duct (10), and reintroduced into the dispersion channel of bed N +1 via the inlet (14) of bed N + 1.

The present device is particularly applied to a process for separating xylenes in a simulated moving bed operating with a number of beds comprised between 4 and 24 and preferentially between 8 and 12.

Drawings

FIG. 1 shows a side view of 3 successive plates, which are labeled N-1 from top to bottom; n and N + 1. It makes it possible to clearly visualize the dispersion channel (4) and the collection channel (8) which are symmetrical with respect to each other and separated by a wall (11), wherein the fluid returns from the outlet (7) of the collection channel (8) to the inlet (10) of the dispersion channel in bed N + 1.

Fig. 2 corresponds to a cross section along the line a-a of fig. 1. It thus makes it possible to visualize and divide the plate into radial panels and also to collect the fluid by means of the elements (13) and to disperse said fluid by means of the elements (14). The collection by means of the element (13) is combined into two streams and then, if necessary, further combined. Similarly, the dispersion by the element (14) can be carried out by several subdivisions into two main streams originating from the duct (10).

Fig. 3 shows a variation of the dispersion/collection system in which all the streams collected by the ducts (13) on the various panels are manifolded into a single duct (10) and then redistributed in manifolded form into each panel by ducts (14).

Fig. 4 is a visualization produced by digital simulation. Which is a cross-sectional view of the panel along the same cutting plane as that of figure 1. The entrance into the dispersion channel is via the upper left edge. The adsorbent bed is the region between the two grids depicted by the dotted lines. The outlet of the collecting channel is via the lower right edge. The gray scale refers to the average internal residence time (average internal) of the fluid in the bed (M1), which is in seconds.

Detailed Description

The present invention relates to a device that can be adapted to a simulated moving bed unit, which makes it possible to:

-ensuring complete collection of the "pump around" stream, so as to eliminate flushing operations;

minimizing obstructions in the bed. "pumped circulation" is a term used by those skilled in the art to designate a stream that circulates throughout a column.

In a simulated moving bed unit, complete collection of the "pump around" stream is a paramount issue because it makes it possible to eliminate the flushing operation.

The technique described in the present invention uses the principle of compensating the residence times in the collection and dispersion zones in order to minimize the difference, i.e. the difference in residence time of the fluid circulating in the unit as a function of the starting and ending points of said fluid.

In addition, the interbed volume is minimized by operating at the same velocity in the collection and dispersion zones rather than at the same channel height. The total space requirement of the column is also minimized by stacking the beds. Therefore, there is no specific inter-bed volume management.

The stream originating from bed N-1 (1) is collected in conduit (3).

The injection or extraction is carried out through a network of conduits (2).

The dispersion channel (4) ensures that the flow in the bed N (indicated by (6) in fig. 1) is uniformly dispersed by the grid (5).

The flow is collected by a collecting channel (8) through a lower grid (7).

After injection or withdrawal via network (9), all the flow is collected in conduit (10) to be reinjected into bed N +1 located immediately below bed N.

The separation plate (11) separates the collection channel from the dispersion channel (4). It is important to ensure the flatness of the separator plate (11) by any means known to the person skilled in the art. For example, the separation plate (11) may be firmly attached to the lower grid (5) and the upper grid (7).

It is also possible to use tie rods extending over the entire width of the panel, which tie rods are linked to beams or plates that delimit the panel over the height of the collecting and dispersion channels.

The height at the inlet of the dispersion channel (4) is defined by the maximum allowable discharge velocity in order not to disturb the supply of the bed. Typically, the maximum allowable discharge velocity is between 0.1 m/s and 5 m/s, ideally between 0.5 m/s and 2.5 m/s.

The cross-section of the dispersion channel (4) decreases linearly in order to ensure an almost uniform velocity over the entire length of the channel, which is equal to the maximum discharge velocity. This constancy of speed stems from the fact that: the flow of the fluid is always proportional to the inlet cross section, which is the case at each inlet cross section of the channel.

Thus, the height profile of the dispersion channel is linear in order to ensure this proportionality.

The collecting channels (8) and the dispersion channels (4) are complementary in the sense that the dispersion channels (4) located immediately above the bed N are associated with the collecting channels (8) located immediately below the bed N. The stream leaving the collection channel (8) is then sent to the dispersion channel of bed N +1 by means of a conduit (10), which can be seen in fig. 2.

This duct (10) follows approximately the cylindrical perimeter of the unit so that it is in position to enter the dispersion channel of bed N + 1. The network is dimensioned so that the maximum discharge velocity does not exceed a certain maximum velocity, typically between 4 and 6 m/s (for vibration reasons).

Tissue dispersion and collection in the meridian panel (12). Radial panels are understood to mean the following facts: the panels are parallel and contiguous to each other so as to ensure complete coverage of the cross-section of the cell. The number of panels covering the cross section of the cell varies between 2 and 12, preferably between 4 and 8.

The plates are preferably organized in panels of constant cross-section. The flow rates are adjusted to have the same velocity within the bed.

The outer network of conduits (10) is also designed to operate with the same residence time (equivalent residence time) in both configuration 1 (fig. 2) and configuration 2 (fig. 3).

Configuration 1 corresponds to the combination of two streams exiting each panel.

Configuration 2 corresponds to the direct combination of all streams exiting each panel.

These two configurations are represented in fig. 2 and 3, fig. 2 and 3 corresponding to a cross section along a-a of fig. 1.

"network" residence time is used to indicate the residence time it takes for a fluid particle to travel from its exit point from the tower to its entry point into the tower, and this is true for each panel.

It is possible to distinguish between:

-a collection side network residence time, which is the residence time of the fluid particles from their exit point (13) from any panel leaving the column to the injection and extraction point (9),

-dispersed side network residence time, which is the residence time of the fluid particles from the injection and extraction point (9) to their entry point (14) into the column towards any of the panels.

In configuration 1, the network (10) is organized in such a way that all the fluid particles have:

-the same collection side network residence time within the network from the exit point (13) of each panel to the global injection or extraction point (9). That is, each fluid particle exiting the column from any panel takes the same time to travel within the network the distance from its exit point (13) from the column to the injection/extraction point (9).

-the same decentralized network residence time within the network from the global injection or extraction point (9) to the entry point of each panel (14). That is, each fluid particle takes the same time to travel within the network from the injection/extraction point (9) to its entry point (14) into the tower towards any panel.

The outlet (13) of each panel and the inlet (14) of each panel can be produced by means of 1 to 6 outlet (respectively inlet) points.

The outer network of conduits (10) may have a compensated residence time between the collection and dispersion zones, as shown in fig. 3, fig. 3 representing cross-section a-a of fig. 1 in configuration 2.

In configuration 2, the network residence time is different between the collection-side network residence time and the dispersion-side network residence time individually. In other words, in configuration 2, in addition to the dwell time desynchronization inherent in each panel, the fluid is also desynchronized between the panels. The desynchronization of the residence time at the entrance of the individual panels has no effect on the performance because: due to the inverse geometry of the supply and collection channels, performance is compensated by the inverse desynchronization performed by the collection network.

The external network (10) is organized in such a way that all fluid particles have the same residence time from the exit point (13) of the panel to the entry point (14) of the panel, but are dispersed in a different way depending on the panel between the residence time before the global injection or extraction point (9) (collection side network residence time) and the residence time after the total injection or extraction point (9) up to the entry point (14) into the column (dispersion side network residence time).

An entry (14) to each panel can be made by means of from entry point & to entry point.

The outlet (13) of each panel can be produced by means of from 1 to 6 outlet points.

Examples according to the invention

A simulated moving bed adsorption unit (or adsorber) having a diameter of 10 meters is divided into 6 radial panels of equivalent cross-section and supplied according to the principles of the present invention as presented in fig. 1.

Each bed has a height of 0.77 m.

The dispersion channel (4) had a height of 19 cm at the highest point, i.e. at the inlet (14) of the fluid. The height of the channel then decreases linearly with distance from the inlet wall (14). The collecting channel (8) is strictly symmetrical to the dispersion channel (4). The height of which increases from the left to the right in fig. 1.

Simulations carried out with the computational fluid dynamics software FLUENT18.0 show that: the compensation principle of the residence time between the inlet zone (3) and the outlet zone (13) operates correctly. This satisfactory operation is illustrated by fig. 4.

Fig. 4 is a visualization produced by the digital simulation. Which is a cross-sectional view of the panel along the cutting plane of figure 1. The inlet (14) into the dispersion channel is via the upper left edge. The adsorbent bed (6) is the region between the two grids (5) and (7) depicted by dotted lines. The outlet (13) from the collecting channel is via the lower right edge.

Fig. 4 shows a mapping of residence time (or internal mean residence time, i.e., time elapsed for significant fluid particles from inlet to outlet) at any point throughout the system including the dispersion channel, adsorbent bed, and collection channel.

The gray scale grid represented at the bottom of the graph indicates the change in total dwell time between 0 seconds represented by black and approximately 28.3 seconds represented by white. Thus, the fluid particles just entering the dispersion channel (4) at point (14) have a residence time of close to 0 seconds, and the start of the collection channel is shown as black, then dark grey.

Conversely, when the fluid particles leave the collection channel (7) at the lower right of point (13), their residence time is about 28.3 seconds, and the end point of the collection channel is shown as being very light grey, then white.

In the bed, the equivalent dwell timeline (line of equal dwell time) is not horizontal. On the same vertical side within the bed, the fluid particles re-entering the bed near the column inlet on the left side have an extremely short residence time in the dispersion zone and therefore a longer residence time in the dispersion channel for the particles re-entering the bed on the right side compared to the particles re-entering the bed on the right side, which has a still higher total residence time. However, the residence time of all fluid particles in the bed is the same.

Simulations show that at the outlet the residence time differences occurring in the dispersion channel (4) have been compensated by compensating them with the residence time variations in the collection channel (8). The residence time profile is almost perpendicular to the flow direction in the outlet and inlet channels.

The calculation shows about 2 s²Equivalent to a theoretical plate equivalent height of about 2 mm. This is an excellent result in terms of uniformity of residence time.

About one centimeter of HETP (theoretical plate equivalent height) specific to adsorption unit technology was found in Augier et al, 2008.

Reference may be made to page 473 of the cited paper, fig. 9, which represents HETP for various superficial velocities of liquid within the bed. A review of the curves corresponding to the two configurations of the different techniques in the absence of adsorption. The estimate is between 12 cm and 20 cm.

The present invention therefore concerns gains with a ratio of 5 to 10 which can be attributed to the dispersion of the fluid dynamics, which gains are known to the skilled person to directly affect the performance of the process.