Discontinuously operated desublimator with at least one flow disruptor

Abstract

Discontinuously operated desublimator (1) for removing at least one gas component to be desublimated from a gas mixture flow, comprising a housing wall (7) as an outer boundary, an inlet (2) on the housing wall (7) for supplying the gas mixture flow into the desublimator (1), an outlet (6) on the housing wall (7) for discharging the treated gas mixture flow from the desublimator (1), a desublimation zone (4) with temperature-controlled flow channel walls, wherein the flow channel walls are temperature-controlled such that during a loading process the at least one gas component to be desublimated desublimates at the flow channel walls, and that during a subsequent melting process the at least one gas component desublimated in the loading process melts at the flow channel walls, a gas inlet distribution chamber (3) located between the inlet (2) and the desublimation zone (4), and a gas outlet space (5) located between the outlet (6) and the desublimation zone (4), characterized by the fact that at least one first flow disruptor (8) is arranged in the gas inlet distribution chamber (3) to ensure the uniform distribution of the gas mixture flow through the flow channels formed by the flow channel walls of the desublimation zone (4), whose geometric center of gravity is a distance (A T ) to the geometric centroid of the inlet surface (9) in the range of 0.2*D to 10.0*D, preferably in the range of 0.5*D to 3.0*D, wherein D corresponds to the equivalent diameter of a circle with the same area as the inlet surface (9) and the distance (A T ) along the normal vector (n E ) the inlet area (9) is measured.

Description

[0001] The invention relates to a discontinuously operated desublimator for removing at least one gas component to be desublimated from a gas mixture flow, comprising a housing wall, an inlet on the housing wall for supplying the gas mixture flow, an outlet on the housing wall for discharging the treated gas mixture flow and a desublimation zone with temperature-controlled flow channel walls, The flow channel walls are temperature-controlled such that, during a loading process, at least one gas component to be desublimated desublyzes at the flow channel walls, and during a subsequent melting process, at least one gas component desublimated during the loading process melts at the flow channel walls. Furthermore, the desublimator comprises a gas inlet distribution chamber located between the inlet and the desublimation zone, and a gas outlet chamber located between the outlet and the desublimation zone.

[0002] Known batch-operated desublimators have internal flow channel walls, which can be in the form of bundles of finned tubes. Finned tubes are characterized by the fact that their tubes are surrounded by fins, which can be heated or cooled by a fluid flowing through the tubes. During the loading process, a gas component to be desublimated, contained in a gas or gas-vapor mixture, is obtained by desublimating it on the cooled fins. In a subsequent melting process, the desublimated gas component is melted on the now heated walls of the finned tubes and discharged from the desublimator. Instead of finned tubes, other flow channel wall designs, such as lamellae or honeycomb structures, can also be arranged in the desublimator.When using fins, the cooling or heating medium is usually guided through fluid lines, which are generally located on the outside of the housing walls, so that the heat transfer essentially takes place between the externally located fluid lines and the housing wall and between the housing wall and the fins.

[0003] In such desublimators as described above, the gas mixture flow exhibits poor uniformity with respect to the flow through the flow channels during the loading process, resulting in uneven desublimation of the gas component to be desublimated at the flow channel walls. Consequently, the pressure drop between the inlet and outlet of the desublimator increases more rapidly during the loading process, necessitating more frequent regeneration of the desublimator, even though its maximum loading capacity has not yet been reached. The desublimator is typically regenerated through the melting process and an optional subsequent cooling process.

[0004] German patent DE 3407104 A1 discloses batch-operated desublimators for separating products from gas mixtures. These desublimators feature internal fins as flow channel walls, which are attached to the housing side walls. A cooling or heating medium is conveyed through fluid lines located only on the outer housing side walls. Heat transfer occurs from the fluid lines to the housing side walls and from the housing side walls to the fins when the fins are heated, whereas heat transfer occurs from the fins to the housing side walls and from the housing side walls to the fluid lines when the fins are cooled. These desublimators are used, for example, in the production of phthalic anhydride (PSA).

[0005] However, this results in greater parasitic heat losses to the environment, as the desublimator is only heated or cooled externally. This is especially true for larger desublimators with an internal volume of, for example, more than 1 m³. 3 However, during operation of the desublimator, the heat transfer between the housing sidewalls and the fins located further away from the housing sidewalls is generally too low, resulting in a temperature gradient within the fins during the loading process. This leads to different desublimation rates. Consequently, the pressure drop increases more rapidly during the loading process, and the desublimator must be regenerated more frequently, even though its maximum loading capacity has not yet been reached.

[0006] DE102015101398 A1 discloses a discontinuously operated desublimator in a cylindrical design for removing a gas component to be desublimated from a gas flow. The desublimator comprises a housing containing an inner fluid channel and fins as flow channel walls, which are arranged on an inner side of the housing wall and directed inwards. The fins can also be cooled by a coolant flowing through the inner fluid channel or heated by a heating medium flowing through the inner fluid channel. However, if such desublimators have an internal volume of, for example, more than 1 m³ 3If the heat transfer from the inner fluid line to the areas of the lamellae further away from the fluid line is generally too low, a temperature gradient develops within the lamellae. This leads to varying desublimation rates during the charging process. With longer desublimators, the disadvantage arises that desublimation occurs particularly at the lamellae located near the gas mixture inlet. This can cause the lamellae in the inlet area to clog rapidly, even if desublimation has not yet occurred on all lamellae surfaces. Due to the disadvantages described above, the pressure drop increases more rapidly during the charging process, and the desublimator must therefore be regenerated more frequently, even though its maximum charging capacity has not yet been reached.

[0007] The challenge, therefore, was to provide a desublimator that achieves the most uniform possible gas mixture flow through the flow channels of the desublimation zone during its loading process. A further challenge was to ensure that the pressure drop between the desublimator's inlet and outlet increased as slowly as possible during the loading process, thus allowing for longer regeneration intervals. Finally, the task was to provide a desublimator with a greater loading capacity for desublimating gas components at a given maximum pressure drop between the inlet and outlet, or at a given maximum loading time.

[0008] These problems are solved according to the present invention by a discontinuously operated desublimator according to claim 1. Advantageous embodiments of the desublimator are given in claims 2 to 16.

[0009] The discontinuously operated desublimator according to the invention for removing at least one gas component to be desublimated from a gas mixture flow comprises a housing wall, an inlet on the housing wall for supplying the gas mixture flow into the desublimator, an outlet on the housing wall for discharging the treated gas mixture flow from the desublimator, a desublimation zone with temperature-controlled flow channel walls, wherein the flow channel walls are temperature-controlled such that during a loading process the at least one gas component to be desublimated desublimates on the flow channel walls, and that during a subsequent melting process the at least one gas component desublimated in the loading process melts on the flow channel walls, a gas inlet distribution chamber located between the inlet and the desublimation zone, and a gas outlet chamber located between the outlet and the desublimation zone.

[0010] According to the invention, at least one first flow disruptor is arranged in the gas inlet distribution chamber for the uniform distribution of the gas mixture flow through the flow channels resulting from the flow channel walls of the desublimation zone, the geometric center of which has a distance to the geometric center of the inlet surface in the range of 0.2*D to 10.0*D, preferably in the range of 0.5*D to 3.0*D, wherein D corresponds to the equivalent diameter of a circle with the same area as the inlet surface and the distance is dimensioned along the normal vector of the inlet surface.

[0011] In a preferred embodiment, the maximum possible distance between the geometric center of gravity of the first flow disruptor and the geometric center of gravity of the inlet surface is 0.7*L, preferably 0.5*L, particularly preferably 0.3*L, where L corresponds to the length of the longitudinal axis of the gas inlet distribution chamber and the distance is dimensioned along the normal vector of the inlet surface.

[0012] This limits both the aforementioned range of 0.2*D to 10.0*D and the aforementioned preferred range of 0.5*D to 3.0*D to the maximum possible value of 0.3*L if the distance of the geometric center of gravity of the first flow disturbance to the geometric center of gravity of the inlet area should be greater than 0.3*L, where D corresponds to the equivalent diameter of a circle with the same area as the inlet area and L to the length of the longitudinal axis of the gas inlet distribution chamber, and where the distance is measured along the normal vector of the inlet area.

[0013] The first or subsequent flow baffles in the gas inlet distribution chamber distribute the incoming gas mixture flow more evenly through the individual flow channels of the desublimation zone during the loading process, resulting in more uniform desublimation at the flow channel walls. This more uniform flow through the flow channels and the more uniform desublimation at the flow channel walls prevent excessively high gas mixture flow velocities, which can sometimes be well over twice the average velocity of the gas mixture flow through the desublimation zone. Furthermore, the interaction between the flow channel walls and the gas mixture flow is enhanced.

[0014] The desublimation of at least one gas component to be desublimated coats the surfaces of the flow channel walls, causing a corresponding increase in the pressure drop across the individual flow channels during the loading process. Due to the more uniform flow through the flow channels and the more uniform desublimation on the flow channel walls, the pressure drop across the individual flow channels increases less. Consequently, the pressure drop between the inlet and outlet of the desublimator according to the invention also increases less during the loading process, and the desublimator can therefore be regenerated at longer intervals.Furthermore, compared to a desublimator without a flow disruptor, the desublimator according to the invention can desublimate more of the at least one gas component to be desublimated at its flow channel walls at the same pressure loss between the inlet and the outlet of the desublimator, thereby enabling the desublimator according to the invention with at least one first flow disruptor to achieve a greater loading capacity at the same pressure loss.

[0015] In this document, the term "gas mixture flow" generally refers to a flowing gas mixture. The gas mixture can also be a gas-vapor mixture. In principle, the gas mixture may contain liquid droplets or solid particles, provided that the desublimator is not damaged or clogged.

[0016] In this document, the term "a gas component to be desublimated" generally refers to a gas component that predominantly desublimates at the flow channel walls within a desublimation zone, where the flow channel walls have a lower temperature than the desublimation temperature during a loading process. In thermodynamics, desublimation is the process of the direct transition of a substance from the gaseous to the solid state. The desublimation temperature indicates the maximum temperature at a given pressure below which a gas component transitions into the solid state.

[0017] In this document, the term "fluid line" refers to a flowable conduit through which a cooling or heating medium can flow. The fluid line can be located on the outside of the housing wall and / or inside the desublimator. If one or more fluid lines are located externally, heat transfer occurs between the fluid line(s) and the housing wall, thus allowing the temperature control of the gas mixture flow in contact with the inside of the housing wall. Additionally, the flow channel walls can also be temperature controlled if they are thermally coupled to the inside of the housing wall. If one or more fluid lines are located inside the desublimator, heat transfer generally occurs predominantly between the fluid line(s) and the flow channel walls, thus allowing the temperature control of the flow channel walls.

[0018] In this document, the term "housing wall" generally refers to the outer boundary of the desublimator. The housing wall is also typically referred to as the casing in the literature. The walls of the housing wall exhibit sufficient technical tightness. Typically, the outer surface of the housing wall is at least partially heated by an external heating element. This external heating element is usually provided by one or more fluid lines, which are typically mounted directly to the outer surface of the housing wall. During operation of the desublimator, a cooling or heating medium is usually circulated through the fluid line(s) to appropriately temperature-control the gas mixture flow and / or the flow channel walls. One or more inlet and outlet surfaces are provided by corresponding recesses in the housing wall.

[0019] In this document, the term "desublimation zone with temperature-controlled flow channel walls" generally refers to an area in which, during a loading process, at least one gas component to be desublimated desublyzes at the flow channel walls, and the remaining gas mixture flow, also referred to as the treated gas mixture flow, flows out of the desublimation zone and thus reaches the gas outlet chamber. In a melting process following the loading process, the flow channel walls of the desublimation zone are heated to melt the desublimated gas component(s) at the flow channel walls and discharge them from the desublimator.

[0020] The temperature-controlled flow channel walls of the desublimation zone can be formed, for example, by the outer walls of finned tubes, finned tube bundles, tube bundles, lamellar bodies, honeycomb bodies, pipe rods, pipe rod bundles, or plate bodies. Lamellar, plate, or honeycomb bodies are defined as internal components containing lamellae, plates, or honeycombs, respectively. In the case of a lamellar body, the cavities between the individual lamellae form the flow channels. Accordingly, the flow channel walls are defined by the lamella surfaces. In the case of finned tubes, the adjacent lamellae form a cavity as a supporting flow channel through which a fluid, such as a gas mixture, can flow.Typically, bundles of finned tubes are arranged in the desublimation zone, whereby, for example, adjacent finned tubes can form further flow channels or individual finned tubes in combination with correspondingly adjacent finned tubes can form continuous flow channels.

[0021] The flow channels can all have the same diameter by spacing the fins of the finned tube(s) equidistantly. Preferably, however, the flow channels have different diameters by spacing the fins of the finned tube(s) differently. For more uniform flow through the channels, it can be advantageous if the channel diameter at the inlet of each flow channel is larger than at the outlet. Furthermore, the at least one gas component to be desublimated desublys more uniformly along the length of the flow channel walls. The finned tube(s) can be circular, oval, or rectangular.

[0022] Furthermore, the inlet area of ​​the desublimation zone is defined by the fictitious interface between the gas inlet distribution chamber and the desublimation zone, whereby the surfaces of the respective flow channel walls located in the interface are also assigned to the inlet area of ​​the desublimation zone for simplification.

[0023] The outlet surface of the desublimation zone is defined by the fictitious interface between the gas outlet distribution chamber and the desublimation zone, whereby the surfaces of the respective flow channel walls located in the interface are also assigned to the outlet surface of the desublimation zone for simplification.

[0024] The ratio between the inlet area of ​​the desublimation zone and the distance between the inlet and outlet areas of the desublimation zone should preferably be greater than 5 [m²]. 2 / m], where the inlet area in square meters [m²] is used to calculate the ratio. 2] and the distance between the inlet and outlet surfaces of the desublimation zone is to be measured in meters [m].

[0025] Maintaining the preferred range for the ratio prevents significantly excessive desublimation at the flow channel walls in the region of the desublimation zone's inlet area. Increased desublimation at a flow channel wall significantly reduces the minimum free gas passage area of ​​the channel within a very short loading time. This would cause the pressure drop across the flow channel to increase rapidly at the beginning of the loading process, ultimately leading to blockage of the channel after a very short loading time, even if desublimation at the flow channel wall were to occur primarily in the region of the desublimation zone's inlet area.

[0026] The more inlet area is available, the less likely increased desublimation at the flow channel walls in the area of ​​the inlet area of ​​the desublimation zone is to lead to a significantly greater pressure loss or even a blockage.

[0027] In order for a desublimator to be designed to be cost-efficient and space-saving, the ratio between the inlet area of ​​the desublimation zone and the distance between the inlet and outlet areas of the desublimation zone should preferably be less than 100 [m²]. 2 / m], where the inlet area in square meters [m²] is used to calculate the ratio. 2 ] and the distance between the inlet and outlet surfaces of the desublimation zone is to be measured in meters [m].

[0028] To regulate the temperature of the flow channel walls in the desublimation zone, one or more flowable fluid lines can be arranged within the desublimation zone. These lines can be filled with a heating or cooling fluid, thus tempering the walls of the fluid line(s). The heat transfer between the flow channel walls and the flowable fluid line(s) results in the corresponding temperature regulation of the flow channel walls. Additionally or alternatively, temperature regulation can be achieved by an external flowable fluid line or by several external flowable fluid lines arranged on the outside of the housing wall.In this process, the flow channel walls of the desublimation zone are tempered accordingly by the heat transfer between the flow channel walls of the desublimation zone and the outer, flowable fluid line(s), whereby the heat transfer naturally also takes place through the intermediate housing wall.

[0029] If a coolant flows through the inner or outer fluid line(s) during the loading process, the walls of the flow channels are cooled due to heat conduction between the flow channel walls and the fluid line(s), allowing at least one gas component to desublimate on the walls of the flow channels. If a heating medium flows through the inner or outer fluid line(s) during the melting process, the walls of the flow channels are heated due to heat conduction between the flow channel walls and the fluid line(s), allowing the gas component(s) desublimated on the walls of the flow channels to melt. For example, a different or the same heat transfer oil, such as Diphyl DT, can be used as the heating or cooling medium.

[0030] In this document, the term "desublimated on the flow channel walls" generally refers to a deposition process in which at least one gas component to be desublimated, contained in a gas mixture flow, is cooled to such an extent that it desublimates and deposits on the flow channel walls. The desublimated gas component(s) then adhere to the flow channel walls in a solid state. Depending on the prevailing thermodynamic conditions, the term "desublimated" can also be understood in this document to mean that, within the desublimation zone, a phase change first occurs in at least a portion of the gas mixture flow from a gaseous to a liquid state, followed by a phase change from the liquid to the solid state. The flow channel walls of the desublimation zone are accordingly at least partially wetted by the liquid resulting from the phase change.Due to the cooled flow channel walls, the phase change from liquid to solid state occurs at the flow channel walls within a very short time. In summary, the gas component to be desublimated also desublimates at the flow channel walls of the desublimation zone and adheres to the flow channel walls in the solid state.

[0031] In this document, the term "gas inlet distribution chamber" generally refers to a space within the desublimator, bounded by the desublimator housing wall, the desublimator inlet surface, and the desublimation zone. During a loading process, a gas mixture flows through the gas inlet distribution chamber, entering through an inlet on the desublimator. The desublimation zone, with temperature-controlled flow channel walls, adjoins the gas inlet distribution chamber. The gas mixture typically exits the gas inlet distribution chamber only through this desublimation zone.

[0032] In this document, the term "gas outlet chamber" generally refers to a chamber into which a gas mixture flow can be supplied from its adjacent desublimation zone. This chamber typically also has an outlet through which the treated gas mixture flow can escape from the desublimator. Typically, there is also a second outlet port with a drain valve, which may, for example, be a sealing cap. During a melting process, the drain valve is open, allowing the generated molten metal to flow out of the desublimator. During a loading process, the drain valve is closed, preventing any fluid from flowing out of the outlet port. This second outlet port is typically located at the lowest point of the gas outlet chamber, allowing the molten metal to flow to it due to gravity.

[0033] In this document, the term "discontinuously operated desublimator" generally refers to a desublimator that is typically operated discontinuously with two or three different process cycles. The first process cycle is a loading process in which at least one gas component to be desublimated desublyzes on the flow channel walls of the desublimation zone. During the loading process, the flow channel walls are cooled. The second process cycle is a melting process in which the desublimated gas component(s) melts due to heating of the flow channel walls of the desublimation zone and is / are discharged from the desublimator.

[0034] The third process cycle represents an optional recooling process in which the flow channel walls of the desublimation zone are cooled after the desublimated gas component(s) have been removed from the desublimator. Alternatively, the cooling of the flow channel walls can take place at the beginning of the loading process.

[0035] In this document, the term "distance along the longitudinal axis of the flow channel walls" generally refers to the determination of the distance between two points in three-dimensional space. In a first step, a connecting vector between the two points is calculated by finding the difference between the two points. In a second step, the dot product of this previously calculated connecting vector and a vector parallel to the longitudinal axis of the flow channel walls, whose magnitude is normalized to one, is calculated. The magnitude of this dot product represents the distance along the longitudinal axis of the flow channel walls between the two points.

[0036] In this document, the term "distance along the normal vector" generally refers to the calculation of the distance between two points in three-dimensional space. First, a connecting vector between the two points is calculated by finding their difference. Then, in a second step, the dot product of this previously calculated connecting vector and the normal vector is calculated. The magnitude of this dot product represents the distance along the normal vector between the two points.

[0037] In an example case, the distance along the normal vector of the inlet surface between the geometric centroid of the flow disturbance and the geometric centroid of the inlet surface is determined as follows. In a first step, a connecting vector between the geometric centroid of the flow disturbance and the geometric centroid of the inlet surface is calculated by finding the difference between these two points. Then, in a second step, the dot product of this previously calculated connecting vector and the normal vector of the inlet surface is calculated. The magnitude of this dot product represents the distance along the normal vector of the inlet surface between the geometric centroid of the flow disturbance and the geometric centroid of the inlet surface.

[0038] If the normal vector of the inlet surface does not substantially coincide with the main flow direction of the gas mixture flow into the desublimator during the loading process, then the distance along the main flow direction is preferable.

[0039] In this document, the term "loading process" generally refers to a process cycle during the operation of a desublimator, in which the desublimator is operated until a predetermined loading of one or more desublimated gas components is reached on the flow channel walls of the desublimation zone. Here, the loading is understood as the deposited mass of one or more desublimated gas components on the flow channel walls.

[0040] In this document, the term "loading capacity" generally refers to the total mass of desublimated gas component(s) that desublimates on the flow channel walls during a loading process before the pressure drop between the inlet and outlet of the desublimator exceeds a predetermined value and / or until a predetermined loading time is reached.

[0041] In this document, the term "melting process" generally refers to a process cycle during the operation of a desublimator, in which the desublimator has reached its loading capacity and subsequently the desublimated gas component(s) melts by heating the flow channel walls and can flow out of the desublimator, for example, through a drain nozzle located at the bottom of the desublimator. Typically, the gas mixture flow into the desublimator is stopped during the melting process. The melting process is also commonly referred to as the regeneration process.

[0042] In this document, the term "recooling process" generally refers to an optional process cycle during the operation of a desublimator, in which the flow channel walls of the desublimation zone are cooled after the desublimated gas component(s) have been removed from the desublimator. Typically, the recooling process, in conjunction with the upstream melting process, is also referred to as the regeneration process.

[0043] In this document, the term "flow disruptor" generally refers to a component that deflects a gas mixture flowing from the inlet during the loading process and distributes it within the gas inlet distribution chamber in such a way that the gas mixture flows as uniformly as possible through the flow channels of the desublimation zone. This deflection of the gas mixture flow causes, for example, a local, significant change in the magnitude and direction of the gas mixture flow velocity.

[0044] In this document, the term "flow surface" is generally understood to mean a surface that is subjected to a fluid flow and thus experiences a flow pressure in the direction of the surface.

[0045] In this document, the term "the flow area of ​​the flow disruptor projected onto the plane of the inlet surface" generally refers to the area resulting from the projection of the flow area of ​​the flow disruptor onto the plane in which the inlet surface lies. The inlet surface is thus part of this plane. Furthermore, the projection is perpendicular to the plane of the inlet surface.

[0046] In this document, the term "free gas passage area between the flow disruptor and the desublimation zone" generally refers to an area between the flow disruptor and the desublimation zone through which a fluid can flow unimpeded. The free gas passage area extends over the entire width of the desublimator, and is bounded by the region between the flow disruptor and the desublimation zone, with this boundary extending over the entire width of the free gas passage area.

[0047] In this document, the term "an essentially rectangular design" generally refers to a rectangular design, which may also have rounded corners. Furthermore, the interior angle at each corner of the rectangle may deviate from the ideal interior angle of 90° by up to 10°, provided, of course, that the sum of the interior angles of all corners also equals 360°. In addition, the term "an essentially rectangular design" can also refer to a regular or irregular polygon, where the corners of the polygon may also be rounded. Finally, the term "an essentially rectangular design" can also refer to an ellipse or a rectangle with an arch placed on top of it.

[0048] In this document, the term "static mixer" generally refers to a mixer comprising multiple elements, such as several baffle plates positioned at a specific angle to each other, for example, 90°. In principle, the mixer can contain flat and / or curved elements. For instance, the static mixer can consist of one or more crossbeam elements.

[0049] In a preferred embodiment of the desublimator according to the invention, the desublimation zone is arranged between the gas inlet distribution chamber and the gas outlet chamber such that the gas inlet distribution chamber is separated from the gas outlet chamber by the desublimation zone. The gas mixture can only flow through the flow channels of the desublimation zone from the gas inlet distribution chamber to the gas outlet chamber, or, in the case of backflow, from the gas outlet chamber to the gas inlet distribution chamber. This has the advantage that, in this case, no bypass from the gas inlet distribution chamber to the gas outlet chamber is necessary. While a bypass would guarantee a constant flow of the gas mixture through the desublimator during the loading process, this would require a controllable valve in the bypass, which could itself become clogged with at least one gas component to be desublimated during the loading process.

[0050] In a preferred embodiment of the desublimator according to the invention, when several flow baffles are present, the distance between the geometric centers of adjacent baffles is in the range of 0.01 L to 0.5 L, preferably in the range of 0.05 L to 0.33 L, where L corresponds to the length of the longitudinal axis of the gas inlet distribution chamber and this respective distance is dimensioned along the normal vector of the inlet surface. This offers the advantage that, during the loading process, the gas mixture can flow more uniformly through the flow channels of the desublimation zone when several flow baffles are present.

[0051] In a further embodiment of the aforementioned preferred configuration of the desublimator according to the invention, the distance between the adjacent flow disruptors is equidistant. This has the advantage that, during the loading process, the gas mixture can flow more uniformly through the flow channels of the desublimation zone when several flow disruptors are present.

[0052] In a preferred embodiment of the desublimator according to the invention, a distance is obtained between the desublimation zone and the first flow disruptor, or in the case of several flow disruptors, a distance is obtained between the desublimation zone and each flow disruptor which is at least 0.5*D. This offers the advantage that during the loading process, the gas mixture can flow into the flow channels of the desublimation zone at a less excessive speed near the flow disruptor present.

[0053] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor has a width in the range of 1*D up to the maximum width, whereby the at least first flow disruptor extends to the two opposite housing walls of the desublimator. This offers the advantage that, during the loading process, the flow channels of the desublimation zone can be permeated more uniformly with the gas mixture over a wider area or even over the entire width of the desublimation zone.

[0054] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor is movable both before and during the loading process. In particular, at least the first flow disruptor can also be tilted or moved. Alternatively, at least the first flow disruptor can also be fixed in place so that it cannot move during the loading process. This offers the advantage that, depending on the prevailing flow conditions, the corresponding flow disruptor can be adjusted in its orientation and / or position during the loading process.

[0055] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor is heated during the loading process so that no gas components to be desublimated or no other fluids can desublimate on the flow disruptor. In particular, at least the first flow disruptor can have a double wall through the inner cavity of which a heating medium can flow. This has the advantage that the at least one gas component to be desublimated cannot desublimate, or can only desublimate to a minimal extent, on the corresponding flow disruptor.

[0056] In a preferred embodiment of the desublimator according to the invention, the desublimator has a horizontal longitudinal axis that is oriented perpendicular to the longitudinal axis of the flow channels of the desublimation zone, and the gas inlet distribution chamber is arranged above the desublimation zone. Here, the longitudinal axis of the flow channels of the desublimation zone is preferably oriented parallel to the gravity vector. This creates the advantage that, during the loading process, the cooling of the gas mixture flow taking place in the flow channels of the desublimation zone causes the gas mixture to flow more strongly towards the gas outlet space due to the resulting convection effect.

[0057] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor has a distance between its geometric center of gravity and the geometric center of gravity of the inlet area in the range of 0 to 2.0*D, preferably in the range of 0 to 0.5*D, wherein the distance is dimensioned along the longitudinal axis of the flow channels of the desublimation zone and the geometric center of gravity of the first flow disruptor is preferably located below the geometric center of gravity of the inlet area. This offers the advantage that during the loading process, the flow disruptor(s) can distribute the gas mixture more evenly through the flow channels of the desublimation zone.

[0058] In a preferred embodiment of the desublimator according to the invention, in the case of multiple flow disruptors, each individual flow disruptor downstream of the first flow disruptor has a distance between its geometric center of gravity and the geometric center of gravity of its directly adjacent flow disruptor in the direction of the inlet in the range of 0 to 1.0*D, preferably in the range of 0 to 0.5*D, wherein the distance is dimensioned along the longitudinal axis of the flow channels of the desublimation zone. This offers the advantage that the gas mixture can flow more uniformly through the flow channels of the desublimation zone during the loading process.

[0059] In a preferred embodiment of the desublimator according to the invention, in the case of several flow disruptors, the flow disruptors with a greater distance to the inlet surface are arranged higher than those with a smaller distance to the inlet surface, wherein the distance to the inlet surface is dimensioned along the normal vector of the inlet surface.

[0060] This has the advantage that the gas mixture can flow more evenly through the flow channels of the desublimation zone during the loading process.

[0061] In a further embodiment of the desublimator according to the invention, at least the geometric center of gravity of the first flow disruptor is arranged laterally offset in the horizontal plane from the geometric center of gravity of the inlet surface. For example, the height of the geometric center of gravity of the first flow disruptor and the height of the geometric center of gravity of the inlet surface can be the same.

[0062] This offers the advantage that during the loading process the gas mixture can flow more evenly through the flow channels of the desublimation zone, should a corresponding asymmetric gas flow be present in the gas inlet distribution chamber.

[0063] In a preferred embodiment of the desublimator according to the invention, in the case of several flow disruptors, the geometric center of gravity of the flow disruptor with the greatest distance to the inlet surface has a distance between its geometric center of gravity and the geometric center of gravity of the inlet surface 9 in the range of 0 to 2.0*D, preferably in the range of 0 to 1.0*D, wherein the distance is dimensioned along the longitudinal axis of the flow channels of the desublimation zone.

[0064] This offers the advantage that the gas mixture can flow more evenly through the flow channels of the desublimation zone during the loading process.

[0065] In the case that more than two flow disruptors are present in the above embodiment, the flow disruptors are preferably arranged such that the respective distance between two adjacent flow disruptors is equidistant, with this distance being measured along the normal vector of the inlet surface.

[0066] This has the advantage that the gas mixture can flow more evenly through the flow channels of the desublimation zone during the loading process.

[0067] In a preferred embodiment of the desublimator according to the invention, a free gas passage area is provided between the desublimation zone and the first flow disruptor, or, in the case of multiple flow disruptors, between the desublimation zone and each of the existing flow disruptors. This free gas passage area is greater than 0.75, preferably greater than 1.0, relative to the inlet area. This offers the advantage that, during the loading process, the gas mixture can flow into the flow channels of the desublimation zone at a less excessive velocity near the respective flow disruptor.

[0068] In a preferred embodiment of the desublimator according to the invention, the flow area of ​​the first flow disruptor, projected perpendicularly onto the plane of the inlet surface, or, in the case of several flow disruptors, the flow area of ​​each flow disruptor projected perpendicularly onto the plane of the inlet surface, is greater than 1 in relation to the inlet surface. This has the advantage that the gas mixture can flow more uniformly through the flow channels of the desublimation zone during the loading process.

[0069] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor has a ratio between its longest side and its shortest side in the range of 1 to 100, preferably in the range of 1 to 10. This offers the advantage that the gas mixture can flow more uniformly through the flow channels of the desublimation zone during the loading process.

[0070] In a preferred embodiment of the desublimator according to the invention, the first flow disruptor, or in the case of multiple flow disruptors, the respective flow disruptor is a static mixer or a baffle plate, preferably a baffle plate with a substantially rectangular design. This offers the advantage that the gas mixture can flow more uniformly through the flow channels of the desublimation zone during the loading process.

[0071] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor is provided by a static mixer composed of several crossbeam elements, each individual crossbeam element comprising two elements, and at least the first flow disruptor is composed of at least two elements, preferably four to sixteen elements, and particularly preferably six elements, wherein the adjacent element is arranged with an internal angle directed towards the inlet surface in the range of 60 to 120 degrees, preferably in the range of 85 to 95 degrees, and particularly preferably in the range of 89 to 91 degrees, relative to the respective element. For example, the internal angle directed towards the inlet surface can be 90 degrees.

[0072] Preferably, the internal angle between the mutually opposed elements described above can be varied before or during the loading process.

[0073] This offers the advantage that the gas mixture can flow more evenly through the flow channels of the desublimation zone during the loading process.

[0074] In a preferred embodiment of the desublimator according to the invention, at least the first flow disruptor has a geometrically averaged normal vector over its surfaces facing the inlet, and the interior angle formed by the geometrically averaged normal vector and the normal vector of the inlet surface directed outwards from the desublimator is in the range of -60 to 60 degrees, preferably in the range of -45 to 45 degrees, and particularly preferably in the range of -15 to 15 degrees. In the particular case that the corresponding flow disruptor is a static mixer, the static mixer can be composed of several crossbeam elements. In this case, the geometrically averaged normal vector corresponds to the angle bisector of a crossbeam element directed towards the inlet surface. Preferably, the interior angle described above can be varied before or during the loading process.This has the advantage that the gas mixture can flow more evenly through the flow channels of the desublimation zone during the loading process.

[0075] In a preferred embodiment of the desublimator according to the invention, the flow channel walls are formed by the outer walls of a tube bundle, a finned tube, a finned tube bundle, a lamellar body, a honeycomb body, and / or a plate body. This offers the advantage that, during the loading process, the at least one gas component to be desublimated efficiently desublimates at the flow channel walls of the desublimation zone, and that the pressure drop across the desublimation zone is kept to a minimum during the loading process.

[0076] In a preferred embodiment of the desublimator according to the invention, the desublimator has a length of 7.240 m, a width of 2.850 m, a height of 4.560 m, and a circular inlet area with a diameter of 0.79 m. The desublimator contains four static mixers as flow disruptors. Each static mixer is composed of three crossbeam elements, each individual crossbeam element comprising two elements, with the adjacent element arranged at an internal angle of 90 degrees to the inlet area relative to the respective element. Each crossbeam element is 1.130 m long, 0.20 m wide, and 0.005 m thick. Thus, the composition of the individual elements results in a total width of 1.200 m for each static mixer. Each static mixer has a geometrically averaged normal vector over its surfaces facing the inlet.The geometrically averaged normal vector corresponds in this case to the angle bisector of a crossbeam element pointing towards the inlet surface. Each static mixer has an interior angle determined by the geometrically averaged normal vector and the normal vector of the inlet surface pointing outwards from the desublimator. The interior angle is 0 degrees for all static mixers. The geometric centroid of the first flow disruptor is 1.36 m from the geometric centroid of the inlet surface, with the distance measured along the normal vector of the inlet surface. The distance between the geometric centroids of adjacent flow disruptors is 1.4 m, with the distance measured along the normal vector of the inlet surface. The existing flow disruptors each have a distance of 0.284 m between the desublimation zone and the respective flow disruptor.The respective distance between the geometric center of gravity of the respective flow disruptor and the geometric center of gravity of the inlet area is 0.000 m, whereby the respective distance is measured along the longitudinal axis of the flow channels of the desublimation zone.

[0077] Another object of the invention is a method for operating a desublimator according to the invention.

[0078] In the inventive method for operating a desublimator according to the invention, during the loading process, the gas mixture flow containing at least one gas component to be desublimated flows at a mass flow rate of at least 0.01 kg / s, at a temperature in the range of above the desublimation temperature at the given pressure up to 300 °C above the desublimation temperature of the at least one gas component to be desublimated at the given pressure, and at an absolute pressure in the range of 0.1 to 10.00 bar, preferably in the range of 0.5 to 1.5 bar, particularly preferably in the range of 1.05 to 1.10 bar. The flow channel walls of the desublimation zone are cooled to a temperature in the range of 150 °C below the desublimation temperature at the given pressure up to 1 °C below the desublimation temperature at the given pressure.The at least one gas component to be desublimated in the gas mixture flow desublimates at least partially within the desublimator. Preferably, the at least one gas component to be desublimated desublimates in the range of 10 to 100 wt.%, based on the at least one gas component to be desublimated flowing into the inlet of the gas mixture flow. Particularly preferably, the at least one gas component to be desublimated desublimates in the range of 50 to 100 wt.%, based on the at least one gas component to be desublimated flowing into the inlet of the gas mixture flow. In the case that several gas components to be desublimated are present in the gas mixture flow, the ranges specified above refer to the respective gas component to be desublimated.

[0079] This offers the advantage that, during the loading process, at least one gas component to be desublimated efficiently desublimates at the flow channel walls of the desublimation zone, and that the pressure drop across the desublimation zone is minimized during the loading process. Furthermore, the gas mixture flows more uniformly through the flow channels of the desublimation zone.

[0080] In a preferred embodiment of the inventive method for operating a desublimator according to the invention, the pressure drop between the inlet and outlet of the desublimator during the loading process is a maximum of 80 mbar, preferably a maximum of 40 mbar, and particularly preferably a maximum of 20 mbar. This offers the advantage that the pressure drop does not become too high during maximum load operation of the loading process. If the pressure drop were to become too high, the mass flow rate of the gas mixture at the inlet could decrease. In this case, a pump could be used to achieve the desired mass flow rate of the gas mixture at the inlet. However, this poses the risk that the pump will become clogged with the gas component to be desublimated during operation and thus have to be switched off.

[0081] In a preferred embodiment of the inventive method for operating a desublimator according to the invention, the pressure loss during the loading process caused by the first flow disruptor, or, in the case of multiple flow disruptors, by all flow disruptors, is less than 0.1, preferably less than 0.01, relative to the pressure loss between the inlet and outlet of the desublimator. This has the advantage that the flow disruptor(s) does not make a significant contribution to the pressure loss between the inlet and outlet of the desublimator. The pressure loss across the flow disruptors is therefore small and can be neglected.

[0082] In a preferred embodiment of the inventive method for operating a desublimator according to the invention, after reaching a predetermined loading of at least one desublimated gas component on the flow channel walls of the desublimator or after reaching a predetermined loading time, a melting process takes place which comprises the following steps: • Shutting off the supply of the gas mixture flow to the desublimator, • Heating the flow channel walls of the desublimation zone to a temperature in the range from the desublimation temperature at the given pressure to 300 °C above the desublimation temperature of at least one gas component to be desublimated at the given pressure, • Melting of at least one desublimated gas component in the desublimator to obtain a melt, and • Removal of the melt from the desublimator, wherein the removal preferably takes place through an outlet nozzle on the housing wall of the gas outlet chamber.

[0083] This offers the advantage that the melting process is efficient. For example, it is not necessary to scrape the desublimated gas component(s) from the flow channel walls of the desublimation zone.

[0084] In a preferred embodiment of the inventive method for operating a desublimator according to the invention, a cooling process takes place after the melt has been removed from the desublimator. In this process, the flow channel walls of the desublimation zone are cooled to a temperature in the range of 150 °C below the desublimation temperature at the given pressure, or even 1 °C below. This offers the advantage that the flow channels of the desublimation zone already have the required temperature for desublimation before the loading process. Thus, at the very beginning of the loading process, the at least one gas component to be desublimated is efficiently separated from the gas mixture flow.

[0085] In a preferred embodiment of the inventive method for operating a desublimator according to the invention, the at least one gas component to be desublimated contains predominantly phthalic anhydride, preferably only phthalic anhydride, in its mass fraction.

[0086] In a preferred embodiment of the inventive method for operating a desublimator according to the invention, the concentration of the at least one gas component to be desublimated in the gas mixture flow at the inlet is in the range of 0.001 to 50 wt.%, preferably in the range of 0.1 to 10 wt.%. This has the advantage that the at least one gas component to be desublimated is efficiently separated from the gas mixture flow.

[0087] The invention is explained in more detail below with reference to the drawings. The drawings are to be understood as schematic representations. They do not represent any limitation of the invention, for example with regard to specific dimensions or embodiments. They show: Fig. 1: A drawing of a first exemplary embodiment of a desublimator according to the invention in longitudinal section. Fig. 2: A drawing of the first exemplary embodiment of a desublimator according to the invention. Fig. 1 in cross-section. Fig. 3: A drawing of the first exemplary embodiment of a desublimator according to the invention. Fig. 1 in cross-section, showing not only the inlet area but also the flow area of ​​the flow disruptor projected onto the plane and the free gas passage area. Fig. 4: A drawing of a second exemplary embodiment of a desublimator according to the invention in longitudinal section. Fig. 5: A drawing of a third exemplary embodiment of a desublimator according to the invention in longitudinal section. Fig. 6: A drawing of a first exemplary embodiment of a flow disruptor according to the invention, which has a rectangular and flat design. Fig. 7: A drawing of a second exemplary embodiment of a flow disruptor according to the invention, which has a rectangular and curved design. Fig. 8: A drawing of a third exemplary embodiment of a flow disruptor according to the invention, which has a rectangular and curved design, wherein the design has a hole. Fig. 9: A drawing of a fourth exemplary embodiment of a flow disruptor according to the invention, wherein at least the first flow disruptor is a static mixer. Fig. 10: A perspective view of a fourth exemplary embodiment of a desublimator according to the invention, wherein four static mixers are provided as flow disruptors. Fig. Figure 11: A perspective view of a first comparative example of a desublimator without a flow disruptor, showing the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels on the surface shown at the beginning of the loading process. The surface shown lies on the uppermost surface of the desublimation zone. Fig. Figure 12: A perspective view of a fifth exemplary embodiment of the desublimator according to the invention with a static mixer as a flow disruptor according to the invention, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels are shown on the surface at the beginning of the loading process. Here, the surface shown lies in the uppermost surface of the desublimation zone. Fig. 13: A vector plot of the gas mixture flow velocities at the beginning of the loading process within a desublimator according to Fig. 11, which has no flow disturbance, where the vector plot is shown on the cross-sectional surface of the desublimator longitudinal section. Fig. 14: A vector plot of the gas mixture flow velocities at the beginning of the loading process of the fifth exemplary embodiment of the desublimator according to the invention. Fig. 12, which has a static mixer as a flow disruptor according to the invention, wherein the vector plot is shown on the cross-sectional surface of the desublimator longitudinal section. Fig. 15: A perspective view of a sixth exemplary embodiment of the desublimator according to the invention with a static mixer as a flow disruptor according to the invention, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels are shown on the surface at the beginning of the loading process. Here, the surface shown lies in the uppermost surface of the desublimation zone. Fig. 16: A perspective view of a seventh exemplary embodiment of the desublimator according to the invention with a static mixer as a flow disruptor according to the invention, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels are shown on the surface at the beginning of the loading process. Here, the surface shown lies in the uppermost surface of the desublimation zone. Fig. 17: A perspective view of an eighth exemplary embodiment of the desublimator according to the invention with a static mixer as a flow disruptor according to the invention, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels are shown on the surface at the beginning of the loading process. Here, the surface shown lies in the uppermost surface of the desublimation zone. Fig. 18: A perspective view of a ninth exemplary embodiment of the desublimator according to the invention with a static mixer as a flow disruptor according to the invention, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels are shown on the surface at the beginning of the loading process. Here, the surface shown lies in the uppermost surface of the desublimation zone. Fig. 19: A perspective view of a second comparative example of a desublimator without a flow disruptor, showing the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels on the surface shown at the beginning of the loading process. The surface shown lies on the uppermost surface of the desublimation zone. List of reference symbols used: 1 desublimator 2 Entrance 3 Gas inlet distribution room 4. Desublimation zone 5 Gas outlet room 6 Outlet 7 Housing wall 8 flow disruptors 9 Inlet area 10 inlet nozzles 11 outlet nozzles 12 outlet area 13 Projected flow area of ​​the flow disruptor onto the plane of the inlet surface 14 Free gas passage area between the flow disturbance and the desublimation zone 15 Curved or flat baffle plate with or without holes 16 Curved or flat elements of a mixer with or without extinguishers 17 Additional outlet nozzle with a drain valve 18 Second flow disruptor 19 Third flow disruptor 20 Boundary frame of a flow disruptor 21 Fourth flow disruptor α1 Angle between the negative normal vector n E the inlet surface and the geometrically averaged normal vector n A α2 Angle between two adjacent elements of a mixer A H1 Distance between the geometric center of gravity of the first flow disturbance and the geometric center of gravity of the inlet surface, where the distance is along the normal vector n E the inlet area is measured. A H2 Distance between the geometric center of gravity of the second flow disturbance and the geometric center of gravity of the inlet surface, where the distance is along the normal vector n E the inlet area is measured. A H3 Distance between the geometric center of gravity of the third flow disturbance and the geometric center of gravity of the inlet surface, where the distance is along the normal vector n E the inlet area is measured. A H4Distance between the geometric center of gravity of the fourth flow disturbance and the geometric center of gravity of the inlet surface, where the distance is along the normal vector n E the inlet area is measured. A H,max Distance between the geometric center of gravity of the flow disruptor with the greatest distance to the inlet surface and the geometric center of gravity of the inlet surface, where the distance A H,max are measured along the longitudinal axis of the flow channels of the desublimation zone. A T Distance between the geometric center of gravity of a first flow disturbance and the geometric center of gravity of the inlet surface, where the distance is along the normal vector n E the inlet area is measured. A T2 Distance between the geometric center of gravity of a second flow disturbance and the geometric center of gravity of the first flow disturbance. A T3Distance between the geometric center of gravity of a third flow disturbance and the geometric center of gravity of the second flow disturbance. A T4 Distance between the geometric center of gravity of a fourth flow disturbance and the geometric center of gravity of the third flow disturbance. A T,max Distance between the geometric center of gravity of the inlet surface and the flow disturbance furthest from the inlet surface. A S1 Distance between a first flow disturbance and the desublimation zone A S2 Distance between a second flow disturbance and the desublimation zone A S3 Distance between a third flow disturbance and the desublimation zone A S4 Distance between a fourth flow disturbance and the desublimation zone B Width of the desublimator B S Width of the flow disruptor D equivalent diameter g gravity vector H Height of the desublimator L Length of the desublimator n A Geometrically averaged normal vector of the surfaces of the flow disturbance exposed to the inlet n E Normal vector of the inlet surface S L Length of the flow disruptor S H Height of the flow disruptor

[0088] Fig. Figure 1 shows a first exemplary embodiment of a desublimator 1 according to the invention with a length L in longitudinal section, wherein the lower right in the Fig. 1 the gravity vector g by an arrow and at the bottom left in the Fig. Figure 1 shows the xy-coordinate system. The desublimator 1 has a horizontal longitudinal axis that is perpendicular to the longitudinal axis of the flow channels of the desublimation zone 4. The desublimator 1 has an inlet 2 with an inlet nozzle 10, through which a gas mixture flow containing at least one gas component to be desublimated flows into the gas inlet distribution chamber 3 of the desublimator 1 during a loading process. For this purpose, an inlet surface 9 is provided on the housing wall 7, with the housing wall 7 serving as the outer boundary of the desublimator 1. A desublimation zone 4 with temperature-controlled flow channel walls separates the gas inlet distribution chamber 3 from a gas outlet chamber 5. The desublimation zone is connected to the gas inlet distribution chamber 3 in such a way that, during the loading process, the gas mixture flow can flow from the gas inlet distribution chamber 3 to the desublimation zone 4.Furthermore, the desublimation zone 4 is connected to a gas outlet chamber 5 such that, during the loading process, the gas mixture flow can pass from the desublimation zone 4 to the gas outlet chamber 5. An outlet 6 is arranged at the gas outlet chamber 5 to allow the gas mixture flow to escape from the desublimator 1 during the loading process. For this purpose, an outlet surface 12 is provided on the housing wall 7, with an outlet nozzle 11 arranged around the outlet surface 12. The desublimation zone 4 preferably has a volume in the range of 1 to 100 m³. 3A flow disruptor 8 is arranged in the gas inlet distribution chamber 3 such that the gas mixture flows more uniformly through the flow channels during the loading process. The gas mixture should flow through as large a proportion of the total surface area of ​​all flow channel walls in the desublimation zone 4 as possible, so that the gas mixture flows from the gas inlet distribution chamber 3 towards the gas outlet chamber 5.

[0089] This provides the largest possible surface area for desublimation. The maximum velocity at which the flow channels of the desublimation zone 4 are traversed should be as close as possible to the mean velocity through the flow channels to prevent rapid clogging of individual flow channels. Furthermore, backflow of the treated gas mixture from the gas outlet chamber 5 towards the gas inlet distribution chamber 3 should be avoided as much as possible to prevent a significant pressure drop across the desublimation zone 4. In this example, the flow disruptor according to the invention is a baffle plate. The geometric center of gravity of the flow disruptor 8 is at a distance A from the geometric center of gravity of the inlet surface 9. T in the range from 0.5*D to 3.0*D, where D corresponds to the equivalent diameter of a circle with the same area as the inlet area 9 and the distance A T along the normal vector nE the inlet area is 9.

[0090] Furthermore, an additional outlet nozzle 17 with a drain valve, which can be, for example, a sealing cap, is also present. During the loading process, the drain valve is closed, preventing any gas mixture from flowing out of the additional outlet nozzle 17. During a melting process, however, the drain valve is open, allowing the generated molten metal to flow out of the desublimator. Typically, this additional outlet nozzle 17 is located at the lowest point of the gas outlet chamber, so that gravity allows the molten metal to flow to it.

[0091] Fig. Figure 2 shows a cross-section of the first exemplary embodiment of a desublimator 1 according to the invention. Fig. 1, where the desublimator 1 has a height H and a width B. In the Fig. Figure 2 shows the zy-coordinate system in the lower left. The cross-section depicts the housing wall 7, the gas inlet distribution chamber 3, the desublimation zone 4, the gas outlet chamber 5, the outlet surface 12, and the inlet surface 9 with a diameter D. The rectangular boundary frame 20 of the flow disruptor 8 is illustrated with dashed lines. This rectangular boundary frame is defined by the dimensions of the flow disruptor 8 projected perpendicularly onto the plane of the inlet surface.

[0092] Fig. 3 shows further details about Fig. 2. In the Fig. Figure 3 shows, on the left, the inlet surface 9 and the rectangular boundary frame 20 of the flow disruptor 8 with dashed lines. In the center of the drawing, the inflow surface 13 of the flow disruptor 8, projected onto the plane of the inlet surface 9, is shown in the background, and the inlet surface 9 is shown in the foreground. On the right of the drawing, a free gas passage surface 14 between the boundary frame 20 of the flow disruptor 8 and the desublimation zone 4 is shown.

[0093] Fig. Figure 4 shows a second exemplary embodiment of a desublimator 1 according to the invention, wherein, in comparison to the first embodiment of the desublimator 1 according to the invention, a further baffle plate as a second flow disruptor 18 and a further baffle plate as a third flow disruptor 19 are arranged in the gas inlet distribution chamber 3.

[0094] A T1Here, A is the distance between the geometric center of gravity of the second flow disturbance 18 and the geometric center of gravity of the first flow disturbance 8. T2 is the distance between the geometric center of mass of the third flow disturbance 19 and the geometric center of mass of the second flow disturbance 18, where these distances are each along the normal vector n E are measured at the inlet area 9.

[0095] A S2 is the distance between the second flow disturbance and the desublimation zone 4 and A S3 is the distance between the third flow disturbance and the desublimation zone 4, wherein these distances are measured along the longitudinal axis of the flow channels of the desublimation zone 4.

[0096] Fig. Figure 5 shows a third exemplary embodiment of a desublimator 1 according to the invention, wherein, compared to the second embodiment of the desublimator 1 according to the invention, the second flow disruptor 18 and the third flow disruptor 19 are arranged at different heights. The rectangular boundary frame 20 of the flow disruptor 8 is illustrated with dashed lines, the geometric center of gravity of the individual flow disruptors 8, 18, 19 with a circle, and the connecting line between the geometric centers of gravity of the individual flow disruptors 8, 18, 19 with a dotted line. The horizontal longitudinal axis of the desublimator 1 is represented by a dashed line and passes through the geometric center of gravity of the inlet surface 9.

[0097] A T,maxHere, is the distance between the geometric center of gravity of the furthest flow disturbance 19 and the geometric center of gravity of the inlet surface 9, where the distance A T,max along the normal vector n E the inlet area is 9.

[0098] A H1 is the distance between the geometric center of gravity of the first flow disturbance 8 and the geometric center of gravity of the inlet area 9, A H2 is the distance between the geometric center of gravity of the second flow disturbance 18 and the geometric center of gravity of the first flow disturbance 8, A H3 is the distance between the geometric center of gravity of the second flow disturbance 18 and the geometric center of gravity of the third flow disturbance 19 and A H,max is the distance between the geometric center of gravity of the flow disturbance 19 with the greatest distance A T,maxto the inlet surface 9 and the geometric centroid of the inlet surface 9, wherein the individual distances A H,max , A H1 , A H2 , A H3 each is dimensioned along the longitudinal axis of the flow channels of the desublimation zone 4.

[0099] Fig. Figure 6 shows a first exemplary embodiment of a flow disruptor 8 according to the invention, which has a baffle plate 15 in the form of a rectangular and flat design. On the left side of the drawing, the height of the flow disruptor is shown with S. H and the length of the flow disruptor with S L The geometrically averaged normal vector n is shown in the center of the drawing. A the surface of the flow disturbance 8 approached by the inlet 2, as well as the normal vector n pointing in the negative direction EThe inlet surface 9 is shown. In addition, the angle α1 is presented, where the angle α1 is the interior angle between the negative normal vector n. E the inlet surface 9 and the geometrically averaged normal vector n A This specifies the geometrically averaged normal vector n. A The inlet 2 is determined by a geometric averaging of the normal vectors of its surfaces facing inlet 2. Inlet 2, inlet surface 9, and inlet nozzle 10 are shown on the right side of the drawing.

[0100] Fig. Figure 7 shows a second exemplary embodiment of a flow disruptor 8 according to the invention, which has a baffle plate 15 in the form of a rectangular and curved or flat design. On the left side of the drawing, the height of the flow disruptor is indicated by S. H and the length of the flow disruptor 8 with S Lspecified. On the right side of the drawing, a flat embodiment of the flow disruptor 8 and two exemplary embodiments with possible curvatures for the flow disruptor 8 are shown.

[0101] Fig. Figure 8 shows a third exemplary embodiment of a flow disruptor 8 according to the invention, which has a baffle plate 15 in the form of a rectangular and curved or flat design, wherein the flow disruptor 8 has a circular, flow-through hole. On the left side of the drawing, the height of the flow disruptor is indicated by S H and the length of the flow disruptor 8 with S L The drawing shows a flat embodiment of the flow disruptor 8 and two embodiments with possible curvatures for the flow disruptor 8. In principle, all hole shapes can be used, such as, for example, a circular, an oval, or a rectangular hole shape. In particular, the baffle plate may contain multiple flow-through holes. These flow-through holes can all be circular or oval in shape. A mixture of circular and oval holes is also possible.

[0102] Fig. Figure 9 shows a fourth exemplary embodiment of a flow disruptor 8 according to the invention, wherein the flow disruptor is a static mixer. On the left side of the figure, the black rectangles with the arrows contained therein indicate a specific orientation of a respective element 16 of the mixer, whereas the white rectangles with the arrows contained therein indicate another specific orientation of a respective element 16 of the mixer. In the center of the figure, the mixer is shown in cross-section, showing two adjacent elements 16 of the mixer. The black element 16 corresponds to the black rectangle on the left side of the drawing, and the white element 16 corresponds to the white rectangle on the left side of the drawing. Furthermore, the geometrically averaged normal vector n is shown. A the surface of the flow disturbance 8 approached by the inlet 2, as well as the normal vector n pointing in the negative direction EThe inlet surface 9 is shown. In addition, the two angles α1 and α2 are presented, where angle α1 is the interior angle between the normal vector n pointing out of the desublimator 1. E the inlet surface 9 and the geometrically averaged normal vector n A The angle α2 indicates the interior angle between two adjacent elements 16, directed towards the inlet surface 9. The inlet 2, the inlet surface 9, and the inlet nozzle 10 are shown on the right side of the drawing.

[0103] Fig. Figure 10 shows a perspective view of a fourth exemplary embodiment of a desublimator 1 according to the invention, wherein the desublimator 1 has a length L of 7.240 m, a width B of 2.850 m, a height H of 4.560 m and a circular inlet area 9 with a diameter of 0.79 m, and includes four static mixers 8, 18, 19, 21 as flow disruptors.

[0104] According to Fig. 9 is in the Fig. 10. Each static mixer 8, 18, 19, 21 is composed of three crossbeam elements, each individual crossbeam element comprising two elements 16, and the adjacent element 16 is arranged with an interior angle α2 of 90 degrees to the inlet surface 9 in relation to the respective element 16. Each element 16 of the crossbeam is 1.130 m long, 0.20 m wide, and 0.005 m thick. Thus, the composition of the individual elements 16 results in a total width of 1.200 m for each static mixer 8, 18, 19, 21. Each static mixer 8, 18, 19, 21 has a geometrically averaged normal vector n over its surfaces facing the inlet 2. AThe respective geometrically averaged normal vector corresponds in this case to the angle bisector of a crossbeam element directed towards the inlet surface. Each static mixer 8, 18, 19, 21 has an interior angle α1, which is defined by the geometrically averaged normal vector n A and the normal vector n directed out of the desublimator 1 E The inlet area is 9. For all static mixers, the internal angle α1 is 0 degrees. According to Fig. 1 has in the Fig. 10 the geometric center of gravity of the first flow disturbance 8 a distance A T to the geometric center of gravity of the inlet area 9 of 1.36 m, where the distance A T along the normal vector n E the inlet area is 9.

[0105] According to Fig. 4 is in the Fig. 10 the respective distance A T1 , A T2 , A T3between the geometric centers of gravity of each adjacent flow disturbance (8, 18), (18, 19), (19, 21) 1.4 m, where the respective distance A T1 , A T2 , A T3 along the normal vector n E the inlet area is 9. According to Fig. 4 have in the Fig. 10 the existing flow disruptors 8, 18, 19, 21 each a distance A S1, A S2 , A S3 , A S4 between the desublimation zone 4 and the respective flow disturbance 8, 18, 19, 21, which measures 0.284 m. According to Fig. 5 is in the Fig. 10 the respective distance A H1, A H2 , A H3 , A H4 The distance between the geometric center of gravity of the respective flow disruptor 8, 18, 19, 21 and the geometric center of gravity of the inlet area 9 is 0.000 m, where the respective distance A H1, A H2 , A H3 , A H4is dimensioned along the longitudinal axis of the flow channels of the desublimation zone 4. Examples

[0106] The following examples of the loading process of a desublimator are modeled using numerical fluid dynamics simulations. These simulations are also frequently referred to as "Computational Fluid Dynamics (CFD)." The software ANSYS Fluent was used for this purpose, which can be found at https: / / www.ansys.com / de-de / products / fluids / ansys-fluent (accessed on August 25, 2022). ANSYS Fluent is a comprehensive simulation software used for modeling, simulating, and optimizing fluid dynamics processes, systems, and components in industry.

[0107] The following examples are based on a steady-state simulation using the RANS turbulence model. The default settings of Fluent Solver version 22.1 are used. Example 1

[0108] A thermodynamic simulation of an embodiment of the method for operating a desublimator 1 according to the invention. Fig. 1 was conducted in Fluent.

[0109] The length L of the desublimator 1 is 7.24 m, the width B of the desublimator 1 is 2.85 m, the height H of the desublimator 1 is 4.56 m, the diameter D of the circular inlet area 9 is 0.79 m, the diameter of the circular outlet area 12 is 0.79 m, the internal volume of the gas inlet distribution chamber is 23.8 m³ 3 and the internal volume of the gas outlet chamber is 24.9 m³ 3 .

[0110] The ratio between the inlet area of ​​desublimation zone 4 and the distance between the inlet and outlet areas of desublimation zone 4 is 13.1 [m²]. 2 / m].

[0111] The desublimation zone 4 has a volume of 32.58 m³ 3 The surface area of ​​all flow channel walls in desublimation zone 4 is 5000 m². 2 This provides a cooling area of ​​5000 m² for the loading process. 2 A heating surface of 5000 m² is available before and for the melting process. 2 before.

[0112] In the simulation, however, the finned tubes are simplified due to the computational power required, so that a porous zone represents the four finned tube bundles. The pressure loss across the flow channels of desublimation zone 4 is thus calculated efficiently. The porous zone is described in more detail in section 6.2.3 of the ANSYS Fluent User's Guide dated February 17, 2016, provided by ANSYS, Inc. on their website "https: / / www.ansys.com / ". A similar porous zone is also illustrated on page 44 of the website Computational Fluid Dynamics (CFD) of Chemical Processes - Google Books (accessed September 5, 2022).

[0113] In this process, the flow directions of the gas mixture flow within the flow channels, which would deviate from the longitudinal axis of the flow channels, are at least predominantly aligned by a corresponding pressure loss so that these flow directions also point in the direction of the longitudinal axis of the flow channels.

[0114] The flow disruptor 8 according to the invention is designed in the following embodiment: The flow disruptor 8 according to the invention is a static mixer composed of three crossbeam elements, each individual crossbeam element comprising two elements 16, and the adjacent element 16 being arranged with an internal angle α2 of 90 degrees to the inlet surface 9 in relation to the respective element 16. Each element 16 of the crossbeam is 0.710 m long, 0.200 m wide, and 0.005 m thick. Thus, the total width of the static mixer is 1.200 m. The flow disruptor 8 has a geometrically averaged normal vector n over its surfaces facing the inlet 2. A The geometrically averaged normal vector in this case corresponds to the angle bisector of a crossbeam element pointing towards the inlet surface. An interior angle α1, defined by the geometrically averaged normal vector n Aand the normal vector n directed out of the desublimator 1 E The angle of the inlet area 9 is 0 degrees. The geometric center of gravity of the flow disruptor 8 has a distance A T to the geometric center of gravity of the inlet area 9 of 1.050 m, where the distance A T along the normal vector n E the inlet area is 9. The distance A S1, The distance between the flow disruptor 8 and a desublimation zone 4 is 0.460 m and the distance A H1 The distance between the geometric center of gravity of the inlet area 9 and the geometric center of gravity of the flow disruptor 8 is 0.000 m, where the distance A H1 is dimensioned along the longitudinal axis of the flow channels of the desublimation zone 4.

[0115] The simulation yields the following results: A gas mixture flow with a mass flow rate of 150 t / h, an absolute pressure of 1.086 bar and a temperature of 178 °C is fed to the desublimator 1 through an inlet 2. The mass flow of the gas mixture contains PSA as the gas component to be desublimated at a concentration of 8 wt%. Under the prevailing thermodynamic conditions, the density of the gas mixture is 4.4 kg / m³. 3 and the dynamic viscosity of the gas mixture flow is 2.5*10 -5 Pa*s. The housing wall has a temperature of 178 °C.

[0116] The pressure loss caused by the flow disruptor 8 is on the order of 1 mbar. The pressure loss between the inlet 2 and the outlet 6 of the desublimator 1 is 17 mbar.

[0117] The achieved uniform distribution of the gas mixture flow through the flow channels is evaluated based on the following results of the flow simulation: The desublimation zone 4 is accessed from the gas inlet distribution chamber 3 via a flow area of ​​9.8 m². 2 flowing onto the uppermost surface of the desublimation zone 4 according to Fig. 12 corresponds to this. A backflow occurs in the remaining portion of the inflow area. The maximum velocity of the gas mixture flow through the desublimation zone 4 is 7.6 m / s and the average velocity of the gas mixture flow through the desublimation zone 4 is 0.46 m / s.

[0118] The upstream surface of the desublimation zone 4 is in Fig. 12 shown, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels at the beginning of the loading process are shown, and wherein the inflow surface is located in the uppermost surface of the desublimation zone 4.

[0119] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0120] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 10 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s.

[0121] From the comparison of the two Fig. 11 and Fig. Figure 12 shows that in a desublimator 1 according to the invention, the gas mixture flows through a larger area of ​​the desublimation zone 4 in the direction of the gas outlet chamber 5. Furthermore, the flow disruptor 8 according to the invention causes the area of ​​the gas inlet distribution chamber 3 located further back in the main flow direction to exhibit velocity directions across the entire width B of the desublimator 1 that are oriented towards the gas outlet chamber 5. This prevents higher velocities in the flow channels of the desublimation zone 4 and the pressure drop across the desublimation zone 4 is correspondingly lower. A strong flow through individual flow channels would lead to their rapid clogging. In extreme cases, this could even result in desublimation at the flow channel walls only being partially successful due to the high velocities of the gas mixture flow.A flow disruptor 8 reduces excessive velocity and the resulting backflows in adjacent flow channels, thereby avoiding or at least partially avoiding the aforementioned effects.

[0122] A vector plot of the velocity vectors of the gas mixture flow at the beginning of the loading process is generated within the desublimator 1 according to the invention. Fig. Figure 14 shows the vector plot on the cross-sectional area of ​​the desublimator longitudinal section. The length of the vectors is constant and therefore independent of the velocity magnitude.

[0123] It can be seen that, essentially in the left-hand area of ​​desublimation zone 4, indicated by a rectangular frame, the gas mixture flows through desublimation zone 4 towards gas outlet chamber 5. The slanted, dashed line in desublimation zone 4 indicates the point of reversal where the velocity direction through the flow channels of desublimation zone 4 changes to the opposite direction. The more the line slopes downwards, the less the gas mixture flows through the flow channels of desublimation zone 4 towards gas outlet chamber 5. In the area to the right of the slanted, dashed line, the gas mixture flows from gas outlet chamber 5 through the flow channels of desublimation zone 4 towards gas inlet distribution chamber 3.

[0124] From the comparison of the two Fig. 13 and Fig. Figure 14 shows that in the desublimator 1 according to the invention, the gas mixture flows through a larger area of ​​the desublimation zone 4 towards the gas outlet chamber 5. This reduces the higher velocities in the flow channels of the desublimation zone 4, thereby correspondingly lowering the pressure drop across the desublimation zone 4 during the loading process. Furthermore, backflow from the gas outlet chamber 5 to the gas inlet distribution chamber 3 is also reduced.

[0125] Excessive flow through individual flow channels would lead to their rapid clogging. In extreme cases, the high velocities of the gas mixture flow could even result in sublimation at the flow channel walls being only partially successful. The flow disruptor 8 reduces excessive velocities, thereby preventing or at least partially mitigating the aforementioned effects. Example 2

[0126] A thermodynamic simulation of an embodiment of the method for operating a desublimator 1 according to the invention. Fig. Example 1 was performed in Fluent. This Example 2 differs from Example 1 only in the distance A. T of the flow disturbance 8. In this example 2, the distance A is T equals 0.395.

[0127] The upstream surface of the desublimation zone 4 is in Fig. 15 shown, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels at the beginning of the loading process are shown, and wherein the inflow surface is located in the uppermost surface of the desublimation zone 4.

[0128] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0129] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 10 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s.

[0130] From the comparison of the two Fig. 11 and Fig. Figure 15 shows that in a desublimator 1 according to the invention, the gas mixture flows through a larger area of ​​the desublimation zone 4 in the direction of the gas outlet chamber 5. Furthermore, the flow disruptor 8 according to the invention causes the area of ​​the gas inlet distribution chamber 3 located further back in the main flow direction to exhibit velocity directions across the entire width B of the desublimator 1 that are oriented towards the gas outlet chamber 5. This prevents higher velocities in the flow channels of the desublimation zone 4 and the pressure drop across the desublimation zone 4 is correspondingly lower. A strong flow through individual flow channels would lead to their rapid clogging. In extreme cases, this could even result in desublimation at the flow channel walls only being partially successful due to the high velocities of the gas mixture flow.A flow disruptor 8 reduces excessive velocity and the resulting backflows in adjacent flow channels, thereby avoiding or at least partially avoiding the aforementioned effects. Example 3

[0131] A thermodynamic simulation of an embodiment of the method for operating a desublimator 1 according to the invention. Fig. Example 1 was performed in Fluent. This Example 3 differs from Example 1 only in the distance A. T of the flow disturbance 8. In this example 3, the distance A is T equal to 2.37.

[0132] The upstream surface of the desublimation zone 4 is in Fig. 16 shown, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels at the beginning of the loading process are shown, and wherein the inflow surface is located in the uppermost surface of the desublimation zone 4.

[0133] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0134] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 10 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s.

[0135] From the comparison of the two Fig. 11 and Fig. Figure 16 shows that the area aft of the gas inlet distribution chamber 3, in the main flow direction, exhibits velocity directions across the entire width B of the desublimator 1 that are oriented towards the gas outlet chamber 5. This prevents higher velocities in the flow channels of the desublimation zone 4, and the pressure drop across the desublimation zone 4 is correspondingly lower. A strong flow through individual flow channels would lead to their rapid clogging. In extreme cases, this could even result in desublimation at the flow channel walls only being partially successful due to the high velocities of the gas mixture flow. A flow baffle 8 reduces excessive velocity and the resulting backflow in adjacent flow channels, thereby preventing or at least partially preventing the aforementioned effects. Example 4

[0136] A thermodynamic simulation of an embodiment of the method for operating a desublimator 1 according to the invention. Fig. Example 1 was performed in Fluent. This Example 4 differs from Example 1 only in the distance A. T of the flow disturbance 8. In this example 3, the distance A is T equal to 5.53.

[0137] The upstream surface of the desublimation zone 4 is in Fig. 17 shown, wherein the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels at the beginning of the loading process are shown, and wherein the inflow surface is located in the uppermost surface of the desublimation zone 4.

[0138] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0139] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 10 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s.

[0140] From the comparison of the two Fig. 11 and Fig. Figure 17 shows that the area aft of the gas inlet distribution chamber 3, in the main flow direction, exhibits velocity directions across the entire width B of the desublimator 1 that are oriented towards the gas outlet chamber 5. This prevents higher velocities in the flow channels of the desublimation zone 4, and the pressure drop across the desublimation zone 4 is correspondingly lower. A strong flow through individual flow channels would lead to their rapid clogging. In extreme cases, this could even result in desublimation at the flow channel walls only being partially successful due to the high velocities of the gas mixture flow. A flow baffle 8 reduces excessive velocities and the resulting backflows in adjacent flow channels, thereby preventing or at least partially preventing the aforementioned effects. Example 5

[0141] A thermodynamic simulation of an embodiment of the method for operating a desublimator 1 according to the invention. Fig. Example 1 was performed in Fluent. This Example 5 differs from Example 1 only in the material properties and the mass flow rate of the gas mixture. In this Example 5, a gas mixture with a mass flow rate of 30 t / h, an absolute pressure of 1.086 bar, and a temperature of 178 °C is fed to the desublimator 1 through an inlet 2. The mass flow of the gas mixture contains PSA as the gas component to be desublimated at a concentration of 3 wt%, giving the gas mixture a molar mass of 29.7 g / mol. Under the given thermodynamic conditions, the dynamic viscosity of the gas mixture is 2.26 × 10⁻⁵ Pa s. The housing wall has a temperature of 178 °C.

[0142] The upstream surface of the desublimation zone 4 is in Fig. Figure 18 shows the velocities of the gas mixture flow in the direction of the longitudinal axis of the flow channels at the beginning of the loading process, and the inflow area is located at the uppermost surface of the desublimation zone 4. The inflow area is defined as 12.5 m². 2 The gas mixture flows from the gas inlet distribution chamber 3 to the gas outlet chamber 5. A reverse flow occurs in the remaining portion of the inlet area. The maximum velocity of the gas mixture flow through the desublimation zone 4 is 3.4 m / s, and the average velocity is 0.46 m / s. The pressure drop between the inlet 2 and the outlet 6 of the desublimator 1 is 3.3 mbar.

[0143] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0144] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 12 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s.

[0145] From the comparison of the two Fig. 12 and Fig. Figure 18 shows that, despite the different material properties and mass flows of the gas mixture flow, the flow disruptors 8 achieve a similar effect with regard to the uniform distribution of the gas mixture flow through the flow channels of the desublimation zone 4. In both Fig. 12 and Fig. 18 the loading process takes place predominantly on the opposite side of the inlet surface 9, whereby a significant area near the inlet surface 9 is traversed in the opposite direction to the main flow direction.

[0146] Consequently, a flow disruptor 8 also reduces excessive velocity and associated backflows in adjacent flow channels for other material properties and mass flows of the gas mixture flow.

[0147] It was shown that the flow disruptor 8 achieves its effect of better uniform distribution through the flow channels of the desublimation zone 4 under different material properties of the gas mixture flow or at different mass flows of the gas mixture flow. Comparative example 1

[0148] In contrast to example 1, no flow disruptor 8 is present. All other characteristics of the desublimator 1, as well as the process parameters for the loading process, remain the same. A simulation was also performed here using the Fluent software.

[0149] The achieved uniform distribution of the gas mixture flow through the individual flow channels is evaluated based on the following results of the flow simulation: The desublimation zone 4 is accessed from the gas inlet distribution chamber 3 via a flow area of ​​8.6 m². 2The flow area corresponds to the uppermost surface of the desublimation zone 4. Backflow occurs over the remaining portion of the flow area. The maximum velocity of the gas mixture flow through the desublimation zone 4 is 13.4 m / s and the mean velocity of the gas mixture flow through the desublimation zone 4 is 0.46 m / s.

[0150] The upstream surface of the desublimation zone 4 is in Fig. 11 shown, wherein the velocities of the gas mixture flow at the beginning of the loading process are shown on the inflow surface in the direction of the longitudinal axis of the flow channels, and wherein the inflow surface is located in the uppermost surface of the desublimation zone 4.

[0151] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0152] The inlet surface exhibits a gradient between the central axis and the housing walls 7, the gradient being determined by the uneven velocity distribution. Desublimation occurs particularly near the housing wall 7. In the area of ​​the inlet surface 9, hardly any desublimation takes place at the beginning of the charging process.

[0153] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 10 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s. Values ​​in the intermediate range are shown according to the scale as follows. Fig. 11 shown.

[0154] A vector plot of the velocity vectors of the gas mixture flow at the beginning of the loading process is generated inside the desublimator 1 in Fig. Figure 13 shows the vector plot on the cross-sectional area of ​​the desublimator longitudinal section. The length of the vectors is constant and therefore independent of the velocity.

[0155] It can be seen that, essentially in the left-hand area of ​​desublimation zone 4, indicated by a rectangular frame, the gas mixture flows completely through desublimation zone 4 towards gas outlet chamber 5. The curved, dashed line in desublimation zone 4 indicates the transition point where the velocity direction through the flow channels of desublimation zone 4 reverses. The more the curve slopes downward, the less the gas mixture flows through the flow channels of desublimation zone 4 towards gas outlet chamber 5. In the area to the right of the curve, the gas mixture flows from gas outlet chamber 5 through the flow channels of desublimation zone 4 towards gas inlet distribution chamber 3. Comparative example 2

[0156] In comparison to example 1, example 2 differs only in the material properties and the mass flow rate of the gas mixture. A simulation using the Fluent software was also performed here.

[0157] In this comparative example 2, a gas mixture flow with a mass flow rate of 30 t / h, an absolute pressure of 1.086 bar, and a temperature of 178 °C is fed through an inlet 2 to the desublimator 1. The mass flow of the gas mixture contains PSA as the gas component to be desublimated at a concentration of 3 wt%, resulting in a molar mass of 29.7 g / mol. Under the prevailing thermodynamic conditions, the dynamic viscosity of the gas mixture is 2.26 × 10⁻⁵ Pa s. The housing wall has a temperature of 178 °C.

[0158] The achieved uniform distribution of the gas mixture flow through the individual flow channels is evaluated based on the following results of the flow simulation: The desublimation zone 4 is accessed from the gas inlet distribution chamber 3 via a flow surface according to Fig. The flow area is 19, with the flow area corresponding to the uppermost surface of the desublimation zone 4. The pressure drop between the inlet 2 and the outlet 6 of the desublimator 1 is 3.2 mbar.

[0159] The inflow area is 8.7 m² 2 The gas mixture flows from gas inlet distribution chamber 3 to gas outlet distribution chamber 5. A reverse flow occurs in the remaining portion of the inlet area. The maximum velocity of the gas mixture flow through the desublimation zone 4 is 11.2 m / s, and the average velocity of the gas mixture flow through the desublimation zone 4 is 0.46 m / s.

[0160] The upstream surface of the desublimation zone 4 is in Fig. 19 shown, wherein the velocities of the gas mixture flow at the beginning of the loading process are shown on the inflow surface in the direction of the longitudinal axis of the flow channels, and wherein the inflow surface is located in the uppermost surface of the desublimation zone 4.

[0161] At the beginning of the loading process, desublimation on the flow channel walls of desublimation zone 4 occurs predominantly in an area located on the opposite side of the inlet surface 9. As the loading process progresses, the location of desublimation shifts towards the inlet surface 9.

[0162] The inlet surface exhibits a gradient between the central axis and the housing walls 7, the gradient being determined by the uneven velocity distribution. Desublimation occurs particularly near the housing wall 7. In the area of ​​the inlet surface 9, hardly any desublimation takes place at the beginning of the charging process.

[0163] Velocities whose velocity vectors are oriented in the direction of the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in black if the velocity magnitude is greater than or equal to 12 m / s. Velocities whose velocity vectors are oriented in the opposite direction to the main flow of the gas mixture through the flow channels of desublimation zone 4 are shown in white if the velocity magnitude is greater than 0 m / s. Values ​​in the intermediate range are shown according to the scale as follows. Fig. 19 shown. Conclusion:

[0164] Example 1 has a frontal area that is approximately 12% larger than the frontal area in comparison example 1. Furthermore, example 1 has a maximum speed that is approximately 44% lower than the maximum speed in comparison example 1.

[0165] The larger the inflow area, the more flow channels are traversed from the gas inlet distribution chamber to the gas outlet distribution chamber. In particular, this allows a greater proportion of the available desublimation surface, which is represented by the walls of the flow channels, to be utilized. As a result, the flow channel walls are loaded more evenly, and the corresponding flow channels clog less quickly.

[0166] The higher the maximum velocity through the associated flow channel, the greater the pressure loss that occurs during the loading process. In particular, at maximum velocity, a very small proportion of the available desublimation area is subjected to a very high volume flow. Consequently, desublimation occurs significantly more frequently in this area, causing these channels to quickly become clogged and unusable in the further course of the loading process. Furthermore, at very high volume flows, the risk increases that at least one gas component to be desublimated cannot be completely separated in this area.

[0167] Furthermore, a smaller flow area means that the gas mixture only flows through a small area of ​​the desublimation zone 4, and individual flow channels of the desublimation zone 4 become occupied more quickly by desublimation.

[0168] Furthermore, excessive velocities can cause backflow in adjacent flow channels or intensify existing backflow areas in adjacent flow channels, thereby significantly increasing the pressure loss across the desublimation zone 4.

[0169] Examples 2 to 5 show similar improvements compared to example 1. For instance, example 2 has a frontal area approximately 12% larger than example 1. Furthermore, example 2 has a maximum speed approximately 40% lower than the maximum speed of example 1.

[0170] And while example 3 has a frontal area that is approximately 7% smaller than comparison example 1, example 3 has a maximum speed that is approximately 32% lower than the maximum speed in comparison example 1.

[0171] Furthermore, although example 4 has a frontal area that is approximately 28% smaller than comparison example 1, example 4 has a maximum speed that is approximately 20% lower than the maximum speed in comparison example 1.

[0172] Furthermore, example 5 has a frontal area that is approximately 43% larger than that of comparison example 1. Additionally, example 5 has a maximum speed that is approximately 74% lower than the maximum speed of comparison example 1.

[0173] Finally, the so-called "Uniformity Index Mass Weighted" is given below, which is described in the Fluent Version 2022R1 manual starting on page 986. The manual can be found on the website https: / / www.ansys.com / de-de / products / fluids / ansys-fluent (accessed on June 12, 2023).

[0174] A higher uniformity index is desirable because it results in a more uniform flow across the flow channel walls, consequently leading to more uniform desublimation. This allows the desublimator to be operated for a longer period during the loading process, thereby increasing its loading capacity. Furthermore, it reduces the risk of locally excessive velocities causing at least one gas component to be desublimated to not be completely deposited in the desublimation zone and / or the flow channels to become impermeable within a very short loading time.

[0175] For the examples, this “Uniformity” index refers only to the flow area through which the flow passes from the inlet surface of the desublimation zone towards the outlet surface of the desublimation zone.

[0176] Example 1 shows a "Uniformity" Index that is approximately 12% higher than the "Uniformity" Index in comparison example 1, Example 2 shows a "Uniformity" Index that is approximately 13% higher than the "Uniformity" Index in comparison example 1, Example 3 shows a "Uniformity" Index that is approximately 15% higher than the "Uniformity" Index in comparison example 1, Example 4 shows a "Uniformity" Index that is approximately 20% higher than the "Uniformity" Index in comparison example 1, and Example 5 shows a "Uniformity" Index that is approximately 7% higher than the "Uniformity" Index in comparison example 1. QUOTES INCLUDED IN THE DESCRIPTION

[0000] This list of documents cited by the applicant was automatically generated and is included solely for the reader's convenience. The list is not part of the German patent or utility model application. The DPMA accepts no liability for any errors or omissions. Cited patent literature

[0000] DE 3407104 A1

[0004] DE 102015101398 A1

[0006] Cited non-patent literature

[0000] https: / / www.ansys.com / de-de / products / fluids / ansys-fluent

[0106] https: / / www.ansys.com /

[0112] Uniformity Index Mass Weighted” is specified in the manual of the Fluent version 2022R1 from page 986

[0173] The manual is available on the website https: / / www.ansys.com / de-de / products / fluids / ansys-fluent (accessed on 12.06.2023

[0173]

Claims

[1] Discontinuously operated desublimator (1) for removing at least one gas component to be desublimated from a gas mixture flow comprising a housing wall (7) as an outer boundary, an inlet (2) on the housing wall (7) for supplying the gas mixture flow into the desublimator (1), an outlet (6) on the housing wall (7) for discharging the treated gas mixture flow from the desublimator (1), a desublimation zone (4) with temperature-controlled flow channel walls, wherein the flow channel walls are temperature-controlled such that during a loading process the at least one gas component to be desublimated desublimates at the flow channel walls, and that during a subsequent melting process the at least one gas component desublimated in the loading process melts at the flow channel walls, a gas inlet distribution chamber (3) located between the inlet (2) and the desublimation zone (4), and a gas outlet space (5) located between the outlet (6) and the desublimation zone (4), characterized by , that at least one first flow disruptor (8) is arranged in the gas inlet distribution chamber (3) to ensure the uniform distribution of the gas mixture flow through the flow channels formed by the flow channel walls of the desublimation zone (4), whose geometric center of gravity is a distance (A T ) to the geometric centroid of the inlet surface (9) in the range of 0.2*D to 10.0*D, preferably in the range of 0.5*D to 3.0*D, wherein D corresponds to the equivalent diameter of a circle with the same area as the inlet surface (9) and the distance (A T ) along the normal vector (n E ) the inlet area (9) is measured. [2] Desublimator (1) according to claim 1, wherein, in the case of several flow disruptors (8, 18, 19), a distance (A) is formed in each case T1 , A T2) between the geometric centers of gravity of each adjacent flow disruptor ((8, 18), (18, 19)) in the range of 0.01*L to 0.5 *L, preferably in the range of 0.05*L to 0.33*L, where L corresponds to the length of the longitudinal axis of the gas inlet distribution chamber (3) and this respective distance (A T1 , A T2 ) along the normal vector (n E ) the inlet area (9) is measured. [3] Desublimator (1) according to claim 1 or 2, wherein a distance (A) S1 ) between the desublimation zone (4) and the first flow disturbance (8) or in the case of several flow disturbances (8, 18, 19) a distance (A) is maintained in each case S1 , A S2 , A S3 ) between the desublimation zone (4) and the respective flow disturbance (8, 18, 19) which is at least 0.5*D. [4] Desublimator (1) according to any one of claims 1 to 3, wherein at least the first flow disruptor (8) has a width (B S) in the range of 1*D up to the maximum width, where at least the first flow disruptor (8) extends to the two opposite housing walls (7) of the desublimator (1). [5] Desublimator (1) according to one of the preceding claims, wherein the desublimator (1) has a horizontal longitudinal axis oriented perpendicular to the longitudinal axis of the flow channels of the desublimation zone (4), and the gas inlet distribution chamber (3) is arranged above the desublimation zone (4). [6] Desublimator (1) according to claim 5, wherein at least the first flow disruptor (8) has a distance (A H1 ) between the geometric center of gravity of the flow disruptor (8) and the geometric center of gravity of the inlet area (9) in the range of 0 to 2.0*D, preferably in the range of 0 to 0.5*D, wherein the distance (A H1) is dimensioned along the longitudinal axis of the flow channels of the desublimation zone (4) and the geometric center of gravity of the first flow disruptor (8) is preferably located below the geometric center of gravity of the inlet surface (9). [7] Desublimator (1) according to claim 5 or 6, wherein in the case of several flow disruptors (8, 18, 19) each individual flow disruptor (18, 19) after the first flow disruptor (8) has a distance (A H2 , A H3 ) between its geometric center of gravity and the geometric center of gravity of its flow disruptor (8, 18) directly adjacent in the direction of inlet (2) in the range of 0 to 1.0*D, preferably in the range of 0 to 0.5*D, wherein the distance (A H2 , A H3 ) is dimensioned along the longitudinal axis of the flow channels of the desublimation zone (4). [8] Desublimator (1) according to any one of claims 5 to 7, wherein in the case of several flow disruptors (8, 18, 19) the flow disruptors (8, 18, 19) with a greater distance to the inlet surface (9) are arranged higher than those with a smaller distance to the inlet surface (9), wherein the distance to the inlet surface (9) is along the normal vector (n E ) the inlet area (9) is measured. [9] Desublimator (1) according to one of claims 5 to 8, wherein in the case of several flow disruptors (8, 18, 19) the geometric center of gravity of the flow disruptor (19) with the greatest distance (A T,max ) to the inlet surface (9) a distance (A H,max ) between its geometric center of gravity and the geometric center of gravity of the inlet area 9 in the range of 0 to 2.0*D, preferably in the range of 0 to 1.0*D, wherein in the case of more than two flow disruptors (8, 18, 19) the other flow disruptor(s) (19) are preferably arranged such that the respective distance (A T1, A T2 ) two adjacent flow disturbances ((8, 18), (18, 19)) is equidistant, where the distance (A T1 , A T2 ) along the normal vector (n E ) the inlet area (9) and the greatest distance (A H,max ) is dimensioned along the longitudinal axis of the flow channels of the desublimation zone (4). [10] Desublimator (1) according to one of the preceding claims, wherein between the desublimation zone (4) and the first flow disruptor (8) or, in the case of several flow disruptors (8, 18, 19), between the desublimation zone (4) and the respective flow disruptor (8, 18, 19) there is a free gas passage area (14) which is greater than 0.75, preferably greater than 1.0, in relation to the inlet area (9). [11] Desublimator (1) according to one of the preceding claims, wherein the flow area (13) of the first flow disruptor (8) projected perpendicularly onto the plane of the inlet surface (9) or, in the case of several flow disruptors (8, 18, 19), the flow area (13) of each flow disruptor (8, 18, 19) projected perpendicularly onto the plane of the inlet surface (9) is greater than 1 in relation to the inlet surface (9). [12] Desublimator (1) according to one of the preceding claims, wherein at least the first flow disruptor (8) has a ratio between its longest side (S L ) and its shortest side (S H ) in the range of 1 to 100, preferably in the range of 1 to 10. [13] Desublimator (1) according to one of the preceding claims, wherein the first flow disruptor (8) or, in the case of several flow disruptors (8, 18, 19), the flow disruptor (18, 19) present in each case is a static mixer or a baffle plate (15), preferably a baffle plate (15) with a substantially rectangular design. [14] Desublimator (1) according to one of the preceding claims, wherein at least the first flow disruptor (8) is provided by a static mixer composed of several crossbeam elements, each individual crossbeam element comprising two elements (16), and wherein at least the first flow disruptor (8) is composed of at least two elements (16), preferably four to sixteen elements (16), particularly preferably six elements (16), wherein the adjacent element (16) is arranged in relation to the respective element (16) with an internal angle (α2) directed towards the inlet surface 9 in the range of 60 to 120 degrees, preferably in the range of 85 to 95 degrees, particularly preferably in the range of 89 to 91 degrees. [15] Desublimator (1) according to one of the preceding claims, wherein at least the first flow disruptor (8) has a geometrically averaged normal vector (n) over its surfaces facing the inlet (2). A) possesses and is defined by the geometrically averaged normal vector (n) A ) and the normal vector directed out of the desublimator (n E ) the internal angle (α1) enclosed by the inlet surface (9) is in the range of -60 to 60 degrees, preferably in the range of -45 to 45 degrees, particularly preferably in the range of -15 to 15 degrees. [16] Desublimator (1) according to one of the preceding claims, wherein the flow channel walls are formed by the outer walls of a tube bundle, a finned tube, a finned tube bundle, a lamellar body, a honeycomb body and / or a plate body.

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