Apparatus for supplying or discharging heat, for carrying out reactions, and for mixing and dispersing flowing media.

Abstract

The present invention relates to an apparatus for supplying and removing heat, conducting reactions, and mixing and dispersing flowing media in a housing (1) having an inner diameter (D) for a medium (I). The housing preferably comprises a bundle of tubes (2) or other elongated elements with an outer diameter (d) parallel to the longitudinal axis of the housing, and webs or web layers (31, 41) intersecting and embedded between the elongated elements, the webs being inclined relative to the longitudinal axis of the housing and not in contact with each other. After a number or length (L) of axially consecutive webs, the webs are preferably rotated 90° and placed between the tubes. A heat transfer medium (II) can flow in parallel or countercurrent within the tubes, resulting in a mixer / heat exchanger or reactor with extremely high heat transfer capacity and near-plug flow.

Description

[Technical Field]

[0001] The present invention relates to an apparatus for supplying or discharging heat, carrying out a reaction, and mixing and dispersing a flowing medium within a housing having an incorporated member, according to the concept of claim 1. The apparatus preferably comprises a bundle of tubes or other elongated elements oriented parallel to the longitudinal axis of the housing, a web and / or web layer of a first arrangement configuration inserted between the tubes or elongated elements and inclined with respect to the longitudinal axis of the housing, and at least one web layer of a second arrangement configuration, wherein the inclination angle of the web of the first arrangement configuration has a sign (Vorzeichen) opposite to that of the arrangement of the second web layer, and intersects with each other but does not contact each other. The webs are incorporated between the tubes of the tube bundle and do not contact each other. Between the intersecting webs are the first and second arrangement configurations, which are preferably tubes or rows of tubes. The flowing medium (product) flows around the tubes within the housing in the axial direction of the main flow. The intersecting webs, inclined with respect to the tube and / or housing axis, cause the flowing medium to flow laterally around the tube while simultaneously being constantly cross-mixed. Within the tube, the heat exchange medium can flow in parallel or countercurrent with respect to the product, but this is not necessarily required. A round tube or the shell space of a tube bundle heat exchanger is preferred as the housing. The apparatus according to the present invention is preferably suited to laminar flow media, but can also be used with turbulent flow. The present invention further relates to a method for carrying out heterogeneous catalytic reactions or mass exchange in a medium flowing within the apparatus according to the present invention.

[0002] Background technology Patent document CH 642 564 describes a highly efficient static mixer apparatus for laminar flow of highly viscous products. In this apparatus, the mixing element consists of 6 to 10 web groups that intersect each other with respect to the cross-sectional projection and are arranged in intersecting planes. Here, the webs and / or planes are preferably inclined at 45° with respect to the flow direction, and adjacent webs are in contact at the intersections. The mixing element has a length of 0.75 to 1.5D, and consecutive mixing elements are assembled in a housing rotated by 90°. An extended modification (e.g., described in CH 627 263) is also known, which simply inclins the intersecting webs at 30° with respect to the flow direction in order to improve heat transfer in the pipe through which laminar flow passes. However, although the pressure loss coefficient is relatively low, the mixing and heat exchange effects are, of course, relatively low. These mixing elements, to this day, are available from many suppliers as so-called X-mixers (e.g., SMX, SMXL, KMX, GX, CSE-X, AMX, or UM, though with some variations; this list is not exhaustive). They are characterized by very good mixing, high heat transfer and / or Nusselt number (Nu = αD / λ), and a very narrow residence time spectrum. Here, α is the heat transfer coefficient on the product side, D (also called d) is the tube diameter, and λ is the thermal conductivity of the product. Furthermore, the Nusselt number, even in laminar flow, does not depend on the length of the tube, unlike empty tubes, due to constant cross-mixing and boundary layer renewal. The heat transfer coefficient α increases 5 to 10 times in laminar flow compared to empty tubes. The thermal transmittance k when using these devices for highly viscous materials is typically 150 to 250 W / (m 2 It is in the range of K). Static mixers with an X structure have the narrowest residence time spectrum of all known static mixers. The measured Bodenstein number Bo is 50-100 m -1Or, for example, in the case of a reactor with a length of 2m, it is a maximum of 200 (F. Streiff, “Waerme-uebertragung bei der Kunststoffaufbereitung”, p.241 / 275, VDI-Verlag, Duesseldorf 1986). This effectively achieves the ideal plug flow (Bo=∞). The Bodenstein number is given by the dispersion model (Bo=vL / D ax ) is a general dimensionless measure that represents the width of the residence time distribution and / or the width of axial inverse mixing, according to ). Here, v is the mean flow velocity in the axial direction, D axθ represents the axial dispersion coefficient, and L represents the axial length of the apparatus. Compared to the residence time spectrum of a cascade model of several j stirred tanks connected in series, Bo=2j corresponds to this. The residence time behavior of such a reactor with Bo=200 is equivalent to a cascade of 100 ideal stirred tanks. Many applications of static mixers require concentrated cross-mixing, high heat transfer capacity, and a narrow residence time spectrum simultaneously. An example of this is a reactor, especially a laminar flow reactor, such as a polymerization reactor. Other applications require heating or cooling the product quickly without causing undesirable reactions and product changes (polymerization, decomposition). In the case of an empty tower, there is no cross-flow against the wall in laminar flow. This is very detrimental to heat transfer, residence time distribution, and product quality. In some applications, the flowing medium is further two-phase (gas / liquid), and the apparatus is required to provide concentrated mixing and dispersion of the phases in addition to heat exchange. Examples include heating polymer solutions containing volatile components or cooling plastic melts containing foaming agents. For low throughput, an X-mixer in a housing that allows for external heating or cooling is an ideal solution to these problems. However, it cannot be scaled up to industrial throughput because the surface area-to-volume ratio decreases very rapidly in large diameter tubes, making it difficult to transfer heat effectively. A possible solution to this problem is to connect multiple tubes in parallel within a tube bundle heat exchanger and incorporate mixing elements within the tubes. While this certainly preserves the advantageous properties of the mixer, unfortunately, it only preserves them in one tube. Very large differences in throughput and residence time can occur between tubes. This risk is particularly high when cooling viscous products or when polymer solutions react simultaneously, or at least partially, within the heat exchanger. The differing temperatures and viscosities within each tube lead to so-called maldistribution. Maldistribution results in significant non-uniformity in flow velocity, temperature, and viscosity across the tubes. As a result, equipment malfunction or degradation of product quality can occur.

[0003] Because the pressure drop coefficient of X-type mixing elements is relatively high, tube bundle heat exchangers must be constructed with many short tubes. This makes the equipment very expensive, not only because of the cost of the incorporated elements, but also because the tube plates become thicker and the volume at the top of the tower becomes very large. In the case of product heaters with partial degassing, the pressure drop of the mixing element hinders early partial degassing, thereby damaging the product or preventing complete degassing. A further drawback of the X structure is its mechanical fragility in withstanding flow forces. Especially under tensile loads, the X structure behaves like a folding fence and easily breaks apart. Also, under pressure, the X structure behaves like a spring and is not stable. Therefore, in the case of high-viscosity products, the web must be constructed very thickly, which further increases the pressure drop. Attempts have been made to make the structure more stable by adding reinforcing elements or external rings.

[0004] Patent document DE 28 39 564 proposes a static mixer heat exchanger or reactor that adopts the basic concept of the X structure but replaces the web with a tube through which a heating or cooling medium flows. This provides a solution to maintain the heat exchange specific surface area per unit volume when scaled up to be equivalent to that when the housing diameter is relatively small, while obtaining mixing action and residence time behavior similar to that of an X mixer. This structure is formed from coiled tubes that meander and bend while intersecting each other. These tubes are also preferably inclined at 45° with respect to the flow direction and perform the function of a web. Each of these intersecting coils forms a mixing element, and consecutive elements are rotated 90° and incorporated into the housing. Each element must have its own collector for the heat transfer medium. The design and construction of these systems are very demanding and expensive. To keep costs to a minimum, the length of the elements is chosen to be as long as possible, but this, of course, has an unfavorable effect on the mixing action because it reduces the number of 90° rotations. The pressure loss on the product side is very large, as is the heat transfer side. The flow rate through each coiled tube can be very uneven. This problem is particularly pronounced when the housing is circular rather than square as originally intended for practical reasons. This creates a risk of further uneven distribution on the product side. By selecting the diameter and number of coiled tubes, a large ratio of heat exchange area A to volume V and / or a high specific heat capacity (Q / VΔT)=(kA / V)>10KW / m 3 It is also possible to realize very large reaction volumes with K independently of the reactor volume (see page 265 of the aforementioned document). In the equation, Q represents the transferable heat flow rate, ΔT represents the average temperature difference between the product and the heat transfer medium, and k represents the heat transfer coefficient. This facilitates scale-up and eliminates the need for parallel tubes. This reduces the risk of uneven distribution. However, the usability of the volume with heat exchange surface area is limited by the minimum bending radius and pressure loss of the coiled tubes. In this setup as well, the residence time distribution is narrow, as in the case of the X mixer. The measured Bodenstein number is similarly about 60 m -1However, due to the rounded shape of the web and the length of the elements, the homogenization length for laminar mixing is up to twice that of an SMX mixer (W. Mueller, Chem.-Ing.Tech. 54 1982, No. 6). This structure is not sufficiently stable and cannot be used for highly viscous products without the addition of support elements. According to US 2004 / 0125691, the addition of elongated support elements improves stability but leaves the weakness and is costly. Despite these drawbacks and difficulties, the value of this equipment, known as the SMR reactor, has been demonstrated and it is commonly used as a polymerization reactor or a cooler for viscous products, for example in fiber plants, or for cooling plastic molten materials.

[0005] Patent document EP 1 067 352 proposes another static mixer heat exchanger and / or reactor having an X-structure web with intersecting X-shaped webs integrated with a tube bundle. The X-structure has only four webs relative to the cross-sectional projection, and the tubes pass through holes in the webs that are inclined at 45° with respect to the flow direction. These webs are in a group of planes that intersect each other at an angle of 90°. The webs are in contact with each other and are at least partially connected to the tubes. First, the X-structure is fabricated from four webs across the cross-section, and the tubes are passed through the holes in the webs of the completed structure. The axial web spacing is said to be 0.2~0.4D. Patent document WO 2008 / 141472 presents an improvement on this structure, where the axial web spacing relative to the diameter of the inner tube is <6. Thus, the thermal conductivity is improved. Here too, by selecting the diameter and number of tubes, it is possible to achieve a very large reactor volume with a high ratio of heat exchange surface to volume and / or high specific heat capacity, as in the case of SMRs. The pressure loss on the heat transfer side is considerably reduced compared to the case of SMRs, and the mechanical limitations due to the bending radius are eliminated. According to this patent document, the residence time behavior of the structure is also very good and is equivalent to that of an X mixer. However, its configuration is very complex and requires very high precision. It is very difficult to align all the holes in the mixer and tube plate linearly and with little tolerance. As with the X structure, mechanical strength remains a problem. [Overview of the project]

[0006] The object of the present invention is to provide an apparatus for mixing and dispersing a flowing liquid, gaseous, or multiphase medium, having an X structure, for supplying and discharging heat, carrying out a reaction, or for photosynthesis, in a tubular housing, with a narrow residence time distribution without uneven distribution, preferably for viscous products, wherein the X structure allows for the manufacture of an apparatus having the X structure in a manner that is considerably simpler and more cost-effective than conventionally known apparatuses, and, if necessary, has high stability against flow forces and lower pressure loss on the heat transfer side as well as on the product side. This object is solved by the features described in claim 1. Particularly advantageous embodiments are the subject of the dependent claims.

[0007] Further aspects of the present invention are covered by the independent claim 20 relating to a method.

[0008] "Pitch t" or "tube pitch t" is understood to mean, in particular, the distance between the center points of two adjacent tubes in a row of tubes lateral to the tube axis and / or housing axis, or the distance between the center points of two adjacent elongated elements in a row lateral to the axis of the elongated elements and / or housing axis.

[0009] "Square pitch" specifically means that the spacing between adjacent tube center points is equal in a first direction lateral to the tube axis and / or housing axis and in a second direction lateral to the tube axis and / or housing axis, and that the second direction is perpendicular to the first direction. The same applies to elongated elements. This square pitch is shown and explained, for example, in VDI-Waermeatlas, 6th edition, 1991, Abschnitt Ob6, Bild 9.

[0010] Advantageous embodiments of the present invention are shown in the accompanying drawings and will be described in more detail below. [Brief explanation of the drawing]

[0011] [Figure 1]This is a side view showing part of one embodiment of the apparatus according to the present invention, which comprises nine tubes and has four intersecting webs with respect to the projection of the cross-section in a cut housing. [Figure 2] This is a cross-sectional projection in the flow direction of one embodiment of the apparatus according to the present invention, in which the apparatus has nine tubes and four web layers in the cross-sectional projection. The webs have a maximum width b=td and fit between the tubes. [Figure 3] This is a cross-sectional projection in the flow direction of one embodiment of the apparatus according to the present invention, which has 21 tubes and / or rods and 6 webs in the cross-sectional projection, where the maximum width of the web in the tube region is b=td and further decreases therein. The webs fit between the tubes. [Figure 4] This is a cross-sectional projection in the flow direction of one embodiment of the apparatus according to the present invention, which has 16 tubes and 5 webs in the cross-sectional projection. The width of the webs has notches in the area of ​​the tubes, and the web width b is smaller than the tube pitch but larger than the space between adjacent tubes. There are no tubes in the axial direction of the cross-section. This arrangement makes a U-shaped tube loop possible. [Figure 5] This is a cross-sectional projection in the flow direction of one embodiment of the apparatus according to the present invention, in which the apparatus has 16 tubes and 7 web layers in the cross-sectional projection. [Figure 6] Figure 5 shows a cross-sectional projection in the flow direction of one embodiment of the apparatus according to the present invention, where only a portion of the positions for the pipe or elongated element are utilized. [Figure 7] This is a cross-sectional projection in the flow direction of one embodiment of the apparatus according to the present invention, which has 45 tubes and 8 web layers in the cross-sectional projection, where the sign of the web inclination is the same for two adjacent web layers (shown by hatching) and alternates between groups. [Figure 8]A projection view in the flow direction of the cross-section according to an embodiment of the device according to the present invention, where the device has a cross shape with the webs intertwined with each other rotated by 90°. [Figure 9] A perspective view of an embodiment of the device according to the present invention, the device having webs (31a, 41b) partially cut off at the length L of the mixing element. The webs have a maximum width b > (t - d) and partially surround the tube. [Figure 10] A perspective view showing a further embodiment of the device according to the present invention, where the webs are at least partially displaced from each other in the longitudinal direction and the mixing elements are arranged axially spaced apart. [Figure 11] A perspective view of a further embodiment of the device according to the present invention, where the webs are intertwined in a cross shape rotated by 90° as shown in FIG. 8. [Figure 12] Possible further shapes and cross-sections for the webs and the elongated elements or tubes are shown. This description does not exclude other possibilities. [Figure 13] A perspective view showing an example of connecting the webs in a grid pattern by a holding bar to form a web layer. [Figure 14] A perspective view showing a modification of the web layer, where the inclined webs are connected to form a wavy web layer. [Figure 15] The results of a mixing test using the structure according to the present invention shown in FIG. 9 (RWX) are shown, compared with the static mixer according to CH642 564 having eight webs in the cross-sectional projection.

Embodiments for Carrying Out the Invention

[0012] Exemplary Embodiments According to the concept of the present invention, the apparatus comprises a housing 1, preferably circular, having an inner diameter D, and an incorporated tube bundle having tubes 2, having an outer diameter d, and parallel to the longitudinal axis and the main flow direction. Other elongated elements may be used instead of tubes. The tube bundle preferably has a square tube pitch t. Between the tubes are incorporated webs (31, 41) or web layers inclined at an angle α, preferably α = 30 to 60°, particularly preferably α = 45°, with respect to the longitudinal axis. The inclination angles of intersecting webs (31, 41) preferably have opposite signs, and the webs of web layers that are axially continuous between the tubes are preferably parallel to each other and preferably all have the same spacing m. Between intersecting webs, it is preferable to have tubes or rows of tubes, but it is also possible that the inclination angles of the webs have the same sign on both sides of the tubes or rows of tubes, and that the change of sign occurs only after a number of adjacent webs or web layers. The webs of the web layers are located in intersecting planes A and B, which are lateral, preferably parallel to each other, and have an inclination angle α with respect to the longitudinal axis. It is preferable that all webs have the same inclination angle α. However, the webs or web layers may optionally be offset from each other axially, and / or the orthogonal spacing m of the webs, the inclination angle within the web layers, or the inclination angle from the web position to the web layers may differ. In this case, the webs will not be aligned front to back in a common plane laterally. The webs have a width b, which is less than or at most equal to the pipe pitch t. The webs are preferably perpendicular to the pipe at their width b. However, it is also possible to incorporate webs of such width at an inclination relative to the pipe. The webs may reach the housing wall completely (but not necessarily), or may only make point contact. The flowing medium (I) and / or products can flow within the housing and / or shell space of the tube bundle, around the tubes and / or elongated elements, and inside the tubes, and the heat transfer medium (II) can flow inside the tubes in parallel or countercurrent directions, but is not necessarily required. In each case, there are several n axially continuous elements. aThe webs form web layers, and all web layers within a cross-section of length L form a mixing element. The web layers of a continuous mixing element are inserted between the tubes rotated 90°. Length L is preferably 0.5 to 4D. A longitudinally cut-off mixing element consists of a full-length web (31, 41) and a cut-off web (31a, 41b). The webs preferably have a width b smaller than the tube pitch t to reduce pressure loss, and their installation is particularly easy when the maximum width is at most b = td (see Figures 2 and 3). Wider webs have recesses for passing tubes through (Figure 4) and can be easily incorporated into existing tube bundles if positioned slightly diagonally during installation. Wider webs increase the contact lines with the tubes. This is advantageous for structural strength and heat transfer when the tubes are connected to the webs. Of course, not all webs in the device need to be the same width and shape. Figure 9 is a perspective view of one embodiment of the apparatus according to the present invention without a housing, which comprises a tube bundle consisting of nine tubes and a mixing element with length L=D having four webs in cross-section. The webs in this embodiment are slightly wider than the free space between the tube rows, with a maximum width b>(td). The webs do not necessarily have to be cut off at length L, and the webs of the web layer may protrude into the subsequent element as long as they do not compete with the subsequent web rotated by 90°, or the mixing elements may be spaced apart as shown in Figure 10. For the sake of cross-mixing and heat transfer to the tubes, it would be desirable to rotate the direction of the webs frequently by 90°. However, if the length L is too short, transport across the entire cross-section will be insufficient, and the structure will become more complex. On the other hand, if the number of 90° rotations is too few, the cross-mixing will decrease.

[0013] Surprisingly, the apparatus according to the present invention provides yet another, previously unknown type of web arrangement, as shown in Figures 8 and 11. Here, webs (31,41) and webs rotated 90° (31',41') are inserted between tubes 2 in a single element interwoven with each other. Thus, an element is created in which two lateral mixing occurs simultaneously. All consecutive elements have the same structure. These elements can be incorporated with gaps between them or nested with each other as much as possible. The typical 90° rotation of each element is omitted, creating a uniform structure.

[0014] Preferably, all mixing elements in the apparatus according to the present invention are identical and configured with the same web spacing. However, in special cases, such as for localized dispersion mixing or to increase localized heat transfer or mass exchange, it may be necessary to select a narrower and / or smaller web axial spacing m, web width b, or kissing element length L for each mixing element or group of mixing elements in the apparatus. To obtain high stability, the webs may be connected to the tube by welding, soldering, or bonding at all or some of the intersecting points. However, if this is undesirable for practical reasons, the webs do not necessarily have to be connected to the tube, and the webs or groups of web layers may be connected to each other by spacers and additional supports 5. However, if this is undesirable for practical reasons, the webs do not necessarily have to be connected to the tube, and the webs or groups of web layers may be connected to each other by spacers and additional supports 5. Finally, the web of a certain layer may be connected by a metal plate and may be inclined. In this case, the web layer may take the form of a corrugated sheet. Figure 2 shows a modified example of a linear web with width b=t, while Figure 4 shows a further embodiment in which the web is wider and a recess for a tube is provided. The width of the web may be variable over its length, and the lateral boundary may have a curved shape, as shown in Figure 3 as a further modification, where the maximum width is maximum b=t. In Figures 2 to 8, the different inclination angles of the intersecting webs are indicated by the different hatching directions. For simplicity of explanation, the following will be referred to as "tubes" or "tube bundles" (through which a medium preferably flows for heat supply or discharge), but if necessary, other elongated elements, such as rods, profiles, heating rods, rod-shaped luminaires, or tubes with semi-permeable or porous walls, may be used instead, even without a heat transfer medium. Furthermore, the applicability of the present invention is not limited to metallic materials. The web is preferably a flat plate-shaped profile made of metal sheet, or a U-shaped or V-shaped profile or tube, or a hollow profile or rod.Finally, the web surface may also be structured. Figure 12 shows possible profile shapes that can be used as both rods and elongated elements.

[0015] Possible manufacturing methods The manufacture of the apparatus according to the present invention for expandable tube bundles is very easy. The web or web group can be inserted into the completed tube bundle. This is especially true when the web width is less than td everywhere and it is connected to the tube only at externally accessible locations. However, wider webs up to b=t can also be easily incorporated individually between the tubes of the completed tube bundle by the appropriate inclination when incorporated. The web should only be introduced when constructing the tube bundle if it is desirable that the web connects to the tube even at locations that are not externally accessible. It is preferable to incorporate the web in a U-shaped tube bundle because this makes the apparatus expandable and prevents the generation of thermal stress. In this case, there are no tubes on the main axis of the housing cross-section. The disadvantage of this arrangement is that proper counterflow to the heat transfer medium cannot be achieved.

[0016] When constructing a heat exchanger using a fixed tube bed and baffle plates, it is common practice to first assemble the baffle plates into the shell and then pull in the tubes. This manufacturing method can also be applied to the apparatus according to the present invention. For this purpose, the web is connected only to a number of elongated elements, thereby forming a stable structure that can then be assembled into the shell of the apparatus in the same way as a normal baffle plate. Finally, the remaining tubes are inserted into place through the tube bed and X structure. In this case, the tubes are not connected to the web except for the support elements. In addition to the above manufacturing method, if the dimensions and materials allow, it is also possible to manufacture the entire assembly and tubes or elongated elements as a monolithic component using a 3D printer. In another manufacturing variation, the assembly is manufactured by 3D printing from a material that melts easily and is mostly coated with a ceramic-like substance. The material inside the hardened mold then melts, leaving a mold into which liquid metal (investment cast) or hardened resin is poured.

[0017] Further exemplary embodiments The number and size of the tubes parallel to the longitudinal axis are determined by the required ratio of the exchange area to the volume of the device, and / or by the required specific heat capacity (Q / VT)=(kA / V), or, when heat should not be transferred, by the support forces and stability required for the web and structure. The specific exchange area (A / V) in the reactor according to the invention is >50 m 2 / m 3 and can be up to 400 m 2 / m 3 . The specific heat capacity of the reactor according to the invention can reach more than 100 kW / m 3 K in the case of high-viscosity products. For example, in an exothermic polymerization reaction with high intensity, if the specific heat capacity of the reactor is not large enough, it will lead to the formation of hot spots and a runaway reaction. Therefore, such reactions can only be controlled in tubular reactors with a small diameter. The reactor according to the invention corresponds to a tubular reactor having an X-type mixing element with a tube diameter of 10 mm (A / V = 400 m 2 / m 3 ) to 80 mm (A / V = 50 m 2 / m 3 ) in terms of heat transfer capacity, mixing behavior and residence time distribution. In contrast to these tubular reactors, in the reactor according to the invention, the specific exchange area and the specific heat capacity can be selected almost independently of the volume of the reactor or the facility. This makes scaling up particularly easy. For example, the polymerization reaction is exothermic with high intensity and is carried out with high viscosity. In order to safely control the reaction with a narrow molecular weight distribution, a facility such as the device according to the invention is required. Due to the very high specific heat capacity and narrow residence time spectrum, the polymerization reaction can be controlled substantially isothermally under a small temperature difference. Since the reaction and heat transfer are carried out by a constant cross-mixing in the housing, there is no uneven distribution. The results of pilot tests with a small tubular reactor equipped with an X-type mixing element show that with the device according to the invention, it is possible to easily scale up to an industrial scale with equivalent mixing behavior and residence time behavior.

[0018] The tube pitch is preferably selected to be uniform across the entire cross-section. In the case of a square tube pitch, construction is particularly easy because all mixing element components are the same. It is also possible that the pitch and web width differ in both lateral directions, or that there are local deviations, for groups rotated 90°. However, it is also possible to select locally different pitches, or to remove one or a group of tubes, or, if the required heat transfer capacity allows, to use, entirely or partially, tubes or elongated elements with other properties, such as optical elements, or elements with semi-transparent or porous walls, or simple tubes or rods without a heat transfer medium, or other elongated profiles to reinforce the structure at the intended tube locations, in place of the heat exchange tubes. The number of webs n in projection onto the cross-sectional area. b is, n b =r m This corresponds to +1, where r m This is the number of tubes in a row of tubes along or near the cross-sectional axis. In contrast to the known X-mixer, the number of webs increases in this way with the number of tubes and / or the diameter of the housing. Surprisingly, the number of lateral webs has been found to have only a slight effect on pressure loss. Also, the number of webs is at least n b If = 4, the mixing action is very good, n b The value does not increase much beyond 8. Figure 5 shows a view in the flow direction of one embodiment of the apparatus according to the present invention, which has 32 tubes and 7 webs across its cross-section.

[0019] In many practical applications of the apparatus according to the present invention, it is sufficient to simply statically mix or disperse the flowing medium without the need to supply or remove heat simultaneously, or to temperature-control the product. In this case, the position of the tubes can be left unoccupied, and / or the tubes can be replaced entirely or partially with complete profiles that serve to reinforce the structure. This results in a static mixer that has very high stability against the flow forces generated during the extrusion or injection molding of viscous plastic molten materials.

[0020] Figure 6 shows a modification of Figure 5, where not all possible pipe positions are covered, and some pipes are replaced with complete rods or profiles. Figure 12 shows possible shape options for the elongated elements. These options are not exhaustive. These elongated elements can be installed axially in place of pipe 2, or inclined relative to pipe 2 as an alternative to the web (31, 41). The axially continuous web 31 can be connected by auxiliary elements 5 to form a web layer, which can be inserted between pipes (see Figure 13). Inclined metal plates can also be used as connections, and the web layer will have a corrugated sheet structure as shown in Figure 14.

[0021] Intersecting webs or profiles, inclined with respect to the housing axis, ensure concentrated cross-mix and cross-flow, improving heat transfer and mass exchange to the tubes. The orthogonal spacing m of webs continuous in the flow direction is a key indicator determining the pressure loss of the tube bundle structure according to the present invention, because this spacing m substantially affects the wetted surface of the components within the reactor. Therefore, when only good cross-mix is ​​required with minimal or no heat exchange, it is desirable to select the largest possible spacing m, preferably 0.2 to 0.4D. Frequent intersection of tubes and webs, and frequent rotation of the web direction, are expected to be advantageous for heat transfer to the tubes. In laminar flow, it has been found that heat transfer or mass exchange to the tubes increases significantly when the ratio m / d < 4. However, as the spacing m decreases, the pressure loss of the apparatus increases. Therefore, the optimal spacing m, the optimal inner diameter d of the inner tube, and the optimal tube pitch t depend on the specific needs of the application.

[0022] Test results In a mixing test using a curable polyester resin, the apparatus according to the present invention, which has a bundle of nine tubes and four webs inserted intersecting each other, was implemented as shown in Figure 9, projected in the flow direction of the cross-section. The length L of the elements rotated to 90° was 1D, and the maximum width b of the webs was 60% of the tube pitch t. The results were compared with a conventional X-mixer conforming to CH 642 564, which had eight webs in the flow direction projection of the cross-section, with the same axial web spacing m, the same element length, and the same web inclination angle. The cured mixture bars were each cut to a length of 1D, and the maximum layer thickness I was measured as an indicator of mixing quality and compared with the initial thickness I0. This measurement method is very simple and efficient for verifying the mixing process and mixing quality in a static mixer in the case of laminar flow, especially in the initial mixing region. The results of this mixing test are shown in Figure 15. Remarkably, the apparatus according to the present invention, which has only four webs, achieves almost the same maximum web thickness (mixing quality) as a conventional static mixer with eight webs! The wetted surface of the webs in the apparatus according to the present invention is only about 60% compared to the conventional design. Therefore, it is expected that the pressure loss in the case of laminar flow will also decrease by almost the same rate, because axially aligned pipes contribute very little to the pressure loss. From this test, it can be seen that the apparatus according to the present invention can achieve excellent mixing performance with low pressure loss even when the web width is considerably smaller than the pipe pitch, or even when the web is inserted between the pipes without any recesses (maximum web width b=td).

[0023] To demonstrate the narrow residence time distribution predicted by the apparatus according to the present invention, the residence time distribution of the above apparatus was simulated using CFD flow calculations and compared with known X mixers. The calculations confirmed that the residence time behavior of the apparatus according to the present invention is equivalent to that of known X structures, as predicted. Thus, the apparatus according to the present invention makes it possible to fabricate a static reactor with extremely large heat transfer capacity, good cross-mixing, and nearly ideal plug flow.

[0024] Application area The applications of the apparatus according to the present invention are not limited to the field of laminar flow. The X structure is known to be very well suited for dispersing liquids or gases in turbulent flow of low-viscosity media. Therefore, this apparatus is also suitable for low-viscosity media for high-exothermic reactions, or as a bioreactor. Photosynthesis is also possible by replacing the tubes with rod-shaped photogenerators or conductors. Furthermore, when installed vertically, catalyst carriers can be easily loaded into the housing for heterogeneous catalytic reactions with relatively high exothermic rates in a fixed bed or fluidized bed.

[0025] The apparatus according to the present invention is preferably used as a mixed heat exchanger with high lateral height and slight axial back mixing for the following applications: • All types of heat exchangers for laminar flow • Heating or cooling of polymer solutions or polymer melts. • Product heater with partial degassing before the degassing chamber • Cooling of viscous products • Heating of sensitive or reactive viscous products • Reactors, especially polymerization reactors • Gas-liquid reactor • Bioreactors that perform photosynthesis • Heterogeneous catalytic reactors equipped with fixed beds or fluidized beds Alternatively, it can be used as a static mixer with a stable structure and low pressure loss, preferably in the case of viscous products, without the use of a heat transfer medium. Static mixers for plastic molten materials need to withstand very large flow forces, and temperature control is always required to maintain the operating temperature within a desired range. For this purpose, this mixer is equipped with a heatable double-shell tube. The mixing element often needs to be supported by the housing wall so as to withstand the flow forces. In this case, the mixing element cannot be removed, and welded seam testing required by pressure vessel regulations is not always possible. The apparatus according to the present invention provides an X mixer for this application and similar applications that is easy to heat, very stable, and expandable. The very expensive double-shell tube is omitted and replaced with a U-tube coil through which a heat transfer medium flows. Further elongated profiles in the position of the tube serve to reinforce the structure as needed. In addition, the mixer according to the present invention can be heated rapidly to the operating temperature because high stresses are not expected within the housing, as is the case with the double-shell tube.

Claims

1. An apparatus for supplying or discharging heat, for carrying out a reaction, and for mixing and dispersing a flowing medium in a housing (1), A housing (1) having an inner diameter D is provided, The longitudinal axis of the housing (1) determines the main flow direction of the liquid, gaseous, or multiphase generated flow (I). The housing (1) includes an assembly member, The assembled member consists of a bundle of pipes (2) having an outer diameter d or a bundle of other elongated elements, a web (31) in at least one first arrangement configuration, and a second web (41) in at least one second arrangement configuration. The liquid, gaseous, or multiphase generating flow (I) flows around the tube (2) or the other elongated element in the direction of the main flow. The web (31) of the at least one first arrangement configuration is incorporated between the tube or other elongated elements, and the web of the at least one first arrangement configuration is inclined at an angle α = 30 to 60° with respect to the longitudinal axis of the housing. The web (31) of the at least one first arrangement configuration and the second web (41) of the at least one second arrangement configuration are intersected and inserted into each other. The apparatus wherein the web has a width b, which is less than or at most equal to the pitch t of the bundle of pipes, and the webs do not come into contact with each other.

2. The apparatus according to claim 1, wherein the web (31) of the at least one first arrangement configuration is a plate-shaped web, and the second web (41) of the at least one second arrangement configuration is a plate-shaped web.

3. The apparatus according to claim 1 or 2, wherein a web continuous in the axial direction forms a web layer between the tube or other elongated elements, the webs of the web layer are preferably parallel and spaced m apart, and the web layer is incorporated between the tubes after a certain number of webs and / or length L, preferably rotated 90° (31', 41').

4. The apparatus according to any one of claims 1 to 3, wherein a first web layer (31) is adjacent to a second web layer (41) that is incorporated in a crossing manner, with a tube or row of tubes between them, and the webs do not come into contact with each other.

5. The apparatus according to any one of claims 1 to 4, wherein there is a gap between adjacent webs in a direction laterally to the main flow direction, and the maximum width b of the web is preferably less than 85% of the pipe pitch t, ​​and more particularly less than 65%.

6. The apparatus according to any one of claims 1 to 5, wherein the web fits between the pipes of the bundle of pipes without recesses and has a maximum width b = t - d.

7. The apparatus according to any one of claims 1 to 6, wherein the webs are aligned laterally such that each web lies on a plane A and B that intersects with each other.

8. The apparatus according to any one of claims 1 to 7, wherein the axial spacing m of the webs is 0.2 to 0.4D at at least one web position.

9. The apparatus according to any one of claims 1 to 8, wherein the axial spacing m of the webs is < 4d at at least one web position.

10. The apparatus according to any one of claims 1 to 9, wherein a group of web layers forms a mixing element having an axial length L, the web layers of a continuous mixing element are inserted between the tubes rotated by 90°, and the length L of the mixing element is preferably 0.5 to 4D.

11. The apparatus according to any one of claims 1 to 10, wherein the intersecting webs (31, 41) of the first group are interwoven with the intersecting webs (31', 41') of the second group, which are rotated by 90°, thereby forming two lateral mixing elements.

12. The apparatus according to any one of claims 1 to 11, wherein at least a portion of the elongated element is a tube equipped with a supply and discharge device for a liquid, gaseous, or vaporous heat transfer medium (II), the heat transfer medium flows in the space outside the tube in a parallel or countercurrent flow with respect to the product flow (I).

13. The apparatus according to any one of claims 1 to 12, wherein at least a portion of the elongated element is an electric heating rod or an electric heating coil.

14. The apparatus according to any one of claims 1 to 13, wherein at least a portion of the elongated element has a porous or semipermeable wall for an exchange process.

15. The apparatus according to any one of claims 1 to 14, wherein at least a portion of the elongated element is fixedly bonded to the web or together with the web forms a monolithic portion.

16. The apparatus according to any one of claims 1 to 15, wherein the webs of at least one web layer are inclined toward each other and are connected toward each other by auxiliary elements or metal plates to form a corrugated web layer.

17. The apparatus according to any one of claims 1 to 16, wherein a group of web layers are interconnected laterally or longitudinally by auxiliary elements.

18. The ratio of the surface area of ​​the tube bundle to the empty volume of the apparatus or reactor is at least 50 m ２ / m ３ The apparatus according to any one of claims 1 to 17.

19. The apparatus according to any one of claims 1 to 18, wherein at least a portion of the tube or the elongated element is a light-emitting element, an element having a semi-transparent or porous wall, a tube or rod without a heat transfer medium, or another elongated external material for reinforcing the structure at an intended location of the bundle of tubes.

20. The apparatus according to any one of claims 1 to 19, wherein at least a portion of the space provided for the pipes in the bundle of pipes is not occupied.

21. The apparatus according to any one of claims 1 to 20, wherein the assembled member, which consists of a bundle of pipes (2) having an outer diameter d or a bundle of other elongated elements, is aligned parallel to the longitudinal axis of the housing and has a square pitch t.

22. The apparatus according to any one of claims 1 to 21, wherein the second web (41) of the at least one second arrangement configuration has the same inclination angle as the web (31) of the at least one first arrangement configuration, but has a reference numeral in the opposite direction.

23. A method for carrying out a heterogeneous catalytic reaction or for transferring mass through a flowing medium, in the apparatus according to any one of claims 1 to 22, A method wherein the product space (I) surrounding the tubes of the bundle of tubes is filled with a fixed bed or fluidized bed of catalyst support or ion exchange resin.

24. The flowing medium is a highly viscous solution or molten material in a single-phase or multi-phase aggregated state, and the ratio of the surface area of ​​the tube bundle to the empty volume of the apparatus or reactor is at least 50 m ２ / m ３ The method according to claim 23.

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