EP1742006B1 - Process and apparatus to guide the fluid in tube bundle heat exchangers for thermal treatment of suspensions. - Google Patents

Abstract

A dairy industry heat exchanger has a group of pipes that heat a suspension also incorporating lumpy material or elongated fibers. Prior to introduction to the heat exchanger, the suspension is sub-divided into a number of fractions that are separated by a distance which is at least as wide as the longest fiber component in the suspension. Each fraction passes individually through the heat exchanger.

Description

TECHNICAL AREA

The invention relates to a method for flow guidance in tube bundle heat exchangers for the thermal treatment of suspensions, which include lumpy and / or long-fiber components, according to the preamble of claim 1 and an arrangement for carrying out the method according to the preamble of the independent claim 2. Such an arrangement or Processes are eg from the WO 2004/051174 known.

STATE OF THE ART

It is known, in each case two adjacent, substantially parallel, connected in series tube bundle of tube bundle heat exchangers, as for example from DE 94 03 913 U1 are known to connect each other via 180-degree pipe bend together (see also WO 2004/051 174 A1 ; WO 2004/083 761 A1 ). In the representations selected there, only half of the relevant connecting sheets are shown.

The known tube bundle heat exchangers have in common that the isolated in the inner tubes of the respective tube bundles partial flows of the inner channel are combined at the outlet of the tube support plate and this combined total flow is supplied together via the connected connection sheet the adjacent tube bundle. There, in the entry region of the tube bundle, this total flow is again separated into partial flows in the inner tubes that are streamed there.

If the product to be thermally treated in the shell-and-tube heat exchanger is such with fibrous admixtures, for example juices with pulp, deposits may occur at the inlet openings of the inner tubes of the tube carrier plate. The treatment at relatively high temperatures favor the agglomeration of fibers and the formation of pulp. These store preferably at the webs between the multiple parallel arranged inner tubes and at the transverse to the flow direction oriented surfaces of the tube support plate and can lead to blockages there. Remedy here measures, as in the aforementioned WO 2004/083 761 A1 are provided in the critical inflow of the respective pipe support plate. It is proposed, inter alia, that in the inflow region of the respective tube support plate and concentric to this a displacement body is arranged, which divides the flow axially symmetrical to the inner channel formed by the inner channel and thereby influenced fluidically such that the aforementioned undesirable deposits are largely avoided or removed.

The US 2003/0111 216 A describes a plate heat exchanger suitable for treating gas laden with blocking substances. This is made possible, inter alia, by a plate which distributes this gas and, viewed in the direction of flow, is arranged slightly behind the inlet connection for the gas in question before the latter enters the channels of the heat exchanger.

In the EP 0 246 111 A Leitvorrichtungen are already described, which influence a laden with solids gas flow in the inflow of a pipe support plate of a tube bundle heat exchanger. For this purpose, each of the gas flowed through the inner tube of the tube bundle heat exchanger carries a conically widened in the direction of the incoming gas flow inlet pipe. In each case four in a square array adjacent inlet pipes are preferably sized so that they touch each other punctiform and that the surface which is formed between the touching four circular pipe sections, each equipped with the aforementioned guide device. The guide completely fills the area with its foot cross-section and, viewed from the four boundary arc of the foot cross-section and seen in the direction of the incoming gas flow, it tapers conically in each case. By the respective guide device on each of the said surfaces of the tube matrix formed by a plurality of inner tubes, the solid constituents of the inflowing gas are prevented from intervening between them deposit conically enlarged pipe sockets on the pipe support plate. Instead, the gas flow and thus the solids contained in it are introduced into the respective nearest conical inlet pipe by the respective guide device.

However, it has been shown that the known measures for preventing deposits in the inflow of the Rohträgerplatte can no longer fully satisfy when the product to be thermally treated are suspensions containing particulate and / or long-fiber constituents, wherein the fiber lengths can reach up to 100 mm. Such suspensions are for example in the context of methods for energy production by biofermentation. Here, a fermentation tank (fermenter), in which the biofermentation takes place, fed a suspension continuously, for example, this suspension consists essentially of corn and manure or whole plant silage (GPS) and manure or grass silage and manure. The fermentation reaction provides so-called. Biogas, which consists for the most part of methane and a (one) coupled to a generator for generating electricity gas piston engine (gas turbine) is supplied. In the disperse system maize / manure or GPS / manure or grass silage / manure, the liquid manure essentially forms the continuous phase, while the disperse phase through the maize or the other vorg. lumpy constituents and possibly other particulate constituents, such as lumpy foods and their waste products and other long-fiber constituents is formed.

The above-mentioned biofermentation in the fermenter requires a certain optimum reaction temperature (fermentation temperature). However, the continuous supply of suspension consisting essentially of the above enumerated products to be fermented, means a disturbance of the reaction in Fermenter, which inevitably results from feed-related temperature and concentration changes and then particularly significant, for example, if in the cold season, the supplied suspension is not sufficiently preheated to the fermentation temperature in the fermenter or can be. For example, in order to ensure this heat input, an attempt has been made internally to heat the fermentation tank. For this purpose, a heating device is arranged in the interior of the fermenter. This can be formed in a cylindrical configuration of the fermentation as a heating wall, which is then preferably elevated stands on the bottom of the fermenter ( DE 202 18 022U1 ). Another embodiment provides in this regard, to arrange heating pockets on the inner wall of the fermenter.

It has also been attempted to preheat the feed to be fermented, essentially consisting of the products to be fermented, by heating outside the fermenter in a shell-and-tube heat exchanger of the type described above and then to supply it to the fermentation tank in a sufficiently heated state. It was found in this "external" warming that the suspension in question in the tube bundle heat exchanger lead to blockages and there could also learn a segregation.

In summary, it can be stated that the measures and procedures that have hitherto been known in biofermentation for the production of biogas are not suitable for keeping the fermentation temperature in the fermenter constant, even when new suspension is added. When heating the products to be fermented within the fermenter in the context of a so-called "internal" heating shows a very poor or inadequate heat transfer into the fermented products with the result of local temperature differences in the fermenter. This results in a slowing down of the fermentation process and a concomitant reduction in the yield of biogas. The so-called "external" heating of the supplied suspension, the products to be fermented within a tube bundle heat exchanger of the known type is problematic insofar as the lumpy and / or langfaserigen components of the disperse system to blockages and segregation in the tube bundle heat exchanger As a result of these disturbances, in turn, local temperature differences result, which results in a slowing down of the fermentation process and a concomitant reduction in the yield of biogas.

It is an object of the present invention to provide a method of the generic type and an arrangement for its implementation, with which the clogging susceptibility of the tube bundle heat exchanger is largely eliminated.

SUMMARY OF THE INVENTION

This object is achieved by a method having the features of claim 1. An arrangement for carrying out the method is characterized by the features of the independent claim 2. Advantageous embodiments of the proposed arrangement are the subject of the dependent claims.

The basic inventive process idea involves three approaches. A first approach provides that the total flow of a lumpy and / or fibrous suspension is separated before entering the tube bundle heat exchanger in a number of sub-streams. According to a second approach, the partial streams are generated in each case with a distance which is at least as great as the greatest length of the fibrous constituents of the suspension. These measures ensure that the longest fibrous constituents can not simultaneously extend into two separation points. If one were to allow such a bridging by long fibers, one would run the risk that these "bridge formations" can not be resolved by the subsequent flow and flow of the suspension. It then comes in these areas preferred to further related deposits with the result that the separation points are finally completely clogged completely by long-fiber components and in cooperation with other lumpy admixtures.

A third approach is that the individual streams separated, each separated, are passed through the entire shell and tube heat exchanger. It is in the proposal according to the invention in this regard, therefore, in each case to a single deflection of the partial flow, seen in the flow direction, in front of and behind the respective inner tube. In known shell-and-tube heat exchangers, on the other hand, the partial flows of all parallel-connected inner tubes of a tube bundle are first combined, and the resulting total flow is then deflected and fed to the next tube bundle as the total flow. The separation of the total current in one of the number of inner tubes corresponding number of partial flows is then carried out, as is known, by acting as a distributor tube support plate.

The proposed arrangement is also characterized by three basic approaches. The first approach is that, viewed in the flow direction, the first tube bundle upstream of an inlet and distribution device with a distributor body, which forms a distributor space on the inside. The second solution concept includes that the distributor space is separately connected to each inner tube of the first tube bundle via a respective distributor tube from a group of distributor tubes, wherein the distance of adjacent distributor tubes is at least as long as the largest length of the fibrous components. According to a third approach, each inner tube of a tube bundle is separately connected to an associated inner tube of the following tube bundle via a connecting bend from a group of connecting bend of the connecting fitting.

In the distribution chamber, the separation is made in the respective partial flows of the inner tubes, which is provided in tube bundle heat exchangers according to the prior art only in the region of the raw plate of the first tube bundle. By dimensioning the distances of adjacent, emanating from the distribution space distribution pipes so-called. "Bridging" is largely avoided by langfaserige components and by the separate connection of each inner tube of the first tube bundle with the distributor space via a respective manifold from a group of distribution pipes is a clear feed ensures each of these inner tubes, which is eliminated in the tube bundle heat exchangers of the prior art critical inflow region of the tube support plate of the first tube bundle. If one were to allow such a bridging by long fibers, one would run the risk that these "bridge formations" can not be resolved by the subsequent flow and flow of the suspension. It then comes in these areas preferably further related deposits with the result that the branching points are completely completely clogged by long-fiber components and in cooperation with other lumpy admixtures.

The principle of continuous separation of the mutually associated inner tubes passing partial flows prevents the repetitive formation of critical Anströmbereiche the pipe support plate in tube bundle heat exchangers according to the prior art. It is in the proposal according to the invention thus to a single deflection of the respective inner tube flowing through partial flow, while in known tube bundle heat exchangers, the partial flows of all parallel inner tubes are first combined and the resulting total flow is then deflected and fed to the next tube bundle.

An advantageous embodiment of the arrangement according to the invention further provides that the respective partial flow has to overcome through the inner tubes from the distributor space to the entry into an outflow and collection device fed by all inner tubes of the last tube bundle equivalent or approximately equivalent flow resistance. The relevant design of all partial flow paths ensures a uniform flow through all parallel connected areas of the tube bundle heat exchanger and uniform thermal treatment of these parallel partial flows. It is achieved that on the way through the entire shell-and-tube heat exchanger separately guided partial flows of the interconnected inner tubes experience the same residence time in the tube bundle heat exchanger and thus treated uniformly thermally. Leading or lagging streams with different Exit temperatures and solids concentrations are thus avoided.

According to another advantageous embodiment of the arrangement, it is provided that a first shell-and-tube heat exchanger and a second shell-and-tube heat exchanger are connected in parallel to the inlet and distribution device. With this arrangement, it is possible for a single inlet and distribution device to supply two identical tube bundle heat exchangers.

In this context, it is further provided that the inner tubes of the respective last tube bundle open into an outlet and collection device with a collecting body, which forms a collecting space on the inside. This embodiment relates both to a single shell-and-tube heat exchanger arrangement and to one in which two shell-and-tube heat exchangers are connected in parallel.

The design of the outlet and collection device designed according to a further proposal is particularly simple when the collecting body is designed as an elongated hollow cylinder. In order to ensure homogenization of the combined in the outlet and collecting part streams of all parallel partial streams of the inner tubes on the one hand, as far as this is necessary in view of the inventive arrangement, and to prevent unwanted emptying of the tube bundle heat exchanger on the other hand, which is a burning of the Provides a further proposal that the collecting body in the region of the connection fittings on one side of the tube bundle heat exchanger initially substantially vertically ascending and then laid down substantially vertically descending provides the inner surface of the inner tubes. The outlet and collection device acts in this case as a so-called. Flow tube, the necessary length is to install space-saving by the proposed installation, and on the other hand as a siphon to prevent unwanted idling of the tube bundle heat exchanger.

It has proved to be advantageous if the distributor body, as further provided, is designed as an elongate hollow cylinder with an inner diameter D, if the group of distribution pipes emanating from the distributor body is furthermore arranged in the longitudinal direction of its branch pipe stubs and if the distributor pipes are arranged inside their group each have an axial distance a from each other, which is equal to or greater than the inner diameter D. The latter is expediently carried out about as large as the largest length of the fibrous constituents of the suspension. The aforementioned dimensioning of the distributor body creates favorable conditions for long fibers not being able to lay over the intermediate region between two distributor tubes in the sense of a so-called "bridge formation".

Run as a further embodiment of the arrangement according to the invention provides, the longitudinal axis of the manifold body parallel to the tube bundle heat exchanger and the group of manifolds in the region of their branch pipe stubs in a meridian plane of the manifold body, the latter perpendicular to an assembly plane of the tube bundle heat exchanger stands, then the distributor body provides space for a second group of distribution pipes, which can supply a second shell-and-tube heat exchanger if required.

An absolutely identical piping between the respective first tube bundle of the two tube bundle heat exchanger and the distributor body is achieved according to a further proposal in that the second group of distributor tubes of the first group distribution pipes is arranged diametrically opposite the distributor body.

By the vorg. Measures on the distributor body is already ensured a uniform feed of the inner tubes of each connected to the distribution chamber first tube bundle.

If each distributor pipe has a shut-off device in the region of its branch pipe socket opening out at the distributor body, as is also provided, then each inner pipe can be used individually and independently of the others Shut off. This shut-off option allows the flushing or flushing of each inner tube, if necessary. This shut-off device can be operated independently of the others either manually or remotely controlled optional. The actuation is expediently controlled as a function of a pressure of the suspension which is significant for the flow through the inner tube. To measure this pressure, a connection for a pressure measuring device is provided on each distributor pipe, viewed in the flow direction, behind the respective shut-off device. Due to the above configuration, each individual inner tube can be purposely flushed or flushed separately, if required, while all other inner tubes are shut off. Thus, the need for flushing or flushing in the event of blockage can be automatically detected and, with suitable equipment, automated. A clogged inner tube leads to a suitable measuring point to a pressure increase, which either generates an alarm message or causes an automatic flushing of the clogged inner tube, while all other inner tubes or partial streams are shut off or interrupted in the course of this Freispülens.

Regardless of whether the branching off at the branch points from the distribution chamber inner tubes are shut off or shut off, the vorg. Flow through the distributor space a cross flow at these branching points, with the possibly deposited there fibers can be eliminated. In connection with the above-described selection of the inner tubes for the purpose of their targeted flushing thus all clogging prone areas of the tube bundle heat exchanger according to the invention are a treatment accessible.

The distributor body has, as another embodiment provides, at its end facing away from its inflow end on a closable by means of a shut-off flushing port. As a result, the distributor body can be flushed through in its longitudinal direction and the transverse flow generated thereby allows flushing of the branch pipe outlets leading from the distributor body to the respective inner pipes, whereby the fibers possibly deposited there are effectively removed and discharged via the flushing connection.

The shut-off device is expedient to operate manually or remotely, so that the latter variant in conjunction with the vorg. Pressure measurement allows the greatest possible automation of the through- or Freeispülvorganges.

In order to achieve the same flow conditions for all partial flows in the inner tubes in the region of the connection fittings, a further embodiment of the arrangement according to the invention provides that the connection fitting maps an arrangement pattern of the inner tubes complementary in their connecting flange in the two tube carrier plates of adjacent tube bundles to be respectively tightly connected, the connection fittings produce the flow connection between the respective inner tubes at the ends of two adjacent tube bundles on the one hand and at the subsequent ends of the adjacent tube bundles on the other hand, and that the respective flow path through the respective two connection fittings between the adjacent tube bundles always has the same flow resistance in the sum , This measure ensures that regardless of the number of series-connected, parallel tube bundles alone, the deflection is configured from one to the other tube bundle that present in each relevant portion of the tube bundle heat exchanger equivalent flow resistance and thus on the inner tubes to each contemplated tube bundle same flow conditions and thus the same residence times are present.

A particularly useful arrangement in this respect is further achieved in that a number of four to seven, preferably four, inner tubes are provided in a tube bundle.

In a preferred number of four inner tubes in the tube bundle results in a particularly simple embodiment of the connection fitting, if these inner tubes, as another proposal provides, are distributed evenly distributed on a common pitch diameter such that two adjacent tube bundles are connected to only two different connection arc , wherein two long, same connecting arc the four outer inner tubes and two short, equal connecting arc associated with the four inner inner tubes. This means that, based on a partial flow within inner tubes connected to one another, a long connection bend on the one hand follows a short connection bend on the other hand and that this arrangement pattern continues steadily over the subsequent interconnected tube bundles.

The arrangement according to the invention for guiding the flow in tube bundle heat exchangers is not only suitable for particularly effectively heating the products to be fermented outside the fermenter in order to ensure a sufficient fermentation temperature, but also in contrast to "internal" and "external" heating devices according to the prior art The technology is particularly well suited, for example, to protect the fermented products in the fermenter from overheating. Such "external" cooling of the products to be fermented is indicated, for example, when in the summer for several weeks outside temperature θ _a > 25 ° C prevails, so in the fermenter without cooling an optimal fermentation temperature of about θ _F = 37 ° C does not comply is. In this case, the products to be fermented are taken from the fermenter in the partial stream and circulated through the tube bundle heat exchanger according to the invention, with well water preferably being used as the heat transfer medium (cooling medium). Overheating of the fermenter has comparable effects on the fermentation process, such as insufficient heating of the products to be fermented.

BRIEF DESCRIPTION OF THE DRAWINGS Starting from the prior art shows

FIG. 1

a central section through a so-called tube bundle as a modular part of a possibly consisting of a plurality of such tube bundle shell and tube heat exchanger, wherein on each side a circular connecting arc is arranged.

This known embodiment will be explained in the introduction.

Figur 2

in perspektivischer Darstellung zwei parallel angeordnete Rohrbündel-Wärmeaustauscher, die, in Strömungsrichtung des zu behandelnden Produktes gesehen, am Eintritt ihres jeweils ersten Rohrbündels mit einer erfindungsgemäßen Einlauf- und Verteilervorrichtung, an den Enden benachbarter, strömungsmäßig in Reihe geschalteter Rohrbündel jeweils mit einer erfindungsgemäßen Verbindungsarmatur und, in Strömungsrichtung gesehen, hinter ihrem jeweils letzten Rohrbündel mit einer erfindungsgemäßen Auslauf- und Sammelvorrichtung ausgestattet sind;

Figur 3a

in der Ansicht die Rohrbündel-Wärmeaustauscher in Verbindung mit den erfindungsgemäßen Anordnungen gemäß Figur 2 ;

Figur 3b

in der Draufsicht die Rohrbündel-Wärmeaustauscher gemäß Figur 3a ;

Figur 3c

in der Seitenansicht die beiden Rohrbündel-Wärmeaustauscher gemäß den Figuren 3a und 3b ;

Figur 4

in perspektivischer Darstellung die Einlauf- und Verteilervorrichtung, wie sie in den Figuren 2 bis 3c dargestellt ist;

Figur 4a

in perspektivischer Darstellung die Einlauf- und Verteilervorrichtung gemäß Figur 4 in einer modifizierten Ausführungsform;

Figur 5a

in perspektivischer Darstellung die Verbindungsarmatur, die in den Figuren 2 bis 3c jeweils in Verbindung mit den zugeordneten Rohrbündeln gezeigt ist und

Figur 5b

die Verbindungsarmatur gemäß Figur 5a in einer dort mit "Z" gekennzeichneten Blickrichtung, wobei die jeweils zugeordnete Rohrträgerplatte des zu verbindenden Rohrbündels strichpunktiert angedeutet ist.

An embodiment according to the invention is shown in the further figures of the drawing and will be described below. Show it

FIG. 2

in perspective view two parallel tube bundle heat exchangers, seen in the flow direction of the product to be treated, at the entrance of their respective first tube bundle with an inlet and distributor device according to the invention, at the ends of adjacent, fluidly connected in series tube bundles each with a connection fitting according to the invention and , seen in the flow direction, are equipped behind their respective last tube bundle with an outlet and collecting device according to the invention;

FIG. 3a

in the view of the tube bundle heat exchanger in conjunction with the inventive arrangements according to FIG. 2 ;

FIG. 3b

in plan view, the tube bundle heat exchanger according to FIG. 3a ;

Figure 3c

in the side view, the two tube bundle heat exchanger according to the FIGS. 3a and 3b ;

FIG. 4

in a perspective view of the inlet and distribution device, as shown in the Figures 2 to 3c is shown;

FIG. 4a

in a perspective view of the inlet and distribution device according to FIG. 4 in a modified embodiment;

FIG. 5a

in perspective view of the connection fitting, which in the Figures 2 to 3c each shown in conjunction with the associated tube bundles and

FIG. 5b

the connection fitting according to FIG. 5a in a direction indicated there with "Z", with the respectively associated Pipe support plate of the pipe bundle to be joined is indicated by dash-dotted lines.

DETAILED DESCRIPTION

A tube bundle heat exchanger 100 according to the prior art, generally composed of a multiplicity of tube bundles 100.1 to 100.n, wherein 100.i denotes an arbitrary tube bundle ( FIG. 1 ; see also DE-U-94 03 913 ), consists in its middle part of an outer channel 200 * limiting outer shell 200 with respect to the display position, left side disposed fixed bearing side Außenmantelflansch 200a and a right side arranged loslagerseitigen Außenmantelflansch 200b. At the latter, a first transverse channel 400a * bounded by a first housing 400.1 with a first connecting piece 400a closes and the outer jacket flange 200a adjoins a second transverse channel 400b * bounded by a second housing 400.2 with a second connecting branch 400b. A number of axially parallel to the outer shell 200 through the outer channel 200 * extending, together an inner channel 300 * forming inner tubes 300, starting with four and then rising to nineteen and possibly more in number, are each end in a fixed bearing side tube support plate 700th or a loslagerseitigen pipe support plate 800 (both also referred to as tube mirror plate) supported and welded at its pipe outside diameter in this, this overall arrangement introduced via an unspecified opening on the second housing 400.2 in the outer shell 200 and a festlagerseitigen Ausauscherflansch 500 with the second housing 400.2 is clamped together with the interposition of one flat gasket 900 (fixed bearing 500, 700, 400.2).

The two housings 400.1, 400.2 are likewise sealed off from the respectively adjacent outer jacket flange 200b, 200a by a flat gasket 900, the first housing 400.1 arranged on the right side being connected to the outer jacket 200 via a replacement bearing 600 with the interposition of an O-ring 910 against the left arranged fixed bearing 500, 700, 400.2 is pressed. The loose bearing tube carrier plate 800 engages through an unspecified bore in the loose bearing side Ausauscherflansch 600 and is compared to the latter their seal by means of the dynamically stressed O-ring 910, which also seals the first housing 400.1 statically against the loslagerseitigen Ausauscherflansch 600. The latter and the loose bearing tube support plate 800 form a so-called. Floating bearing 600, 800, which allows the changes in length of welded in the loslagerseitigen tube support plate 800 inner tubes 300 due to temperature change in both axial directions.

Depending on the arrangement of the respective tube bundle 100.1 to 100.n in the tube bundle heat exchanger 100 and its respective wiring, the inner tubes 300, based on the display position, either from left to right or vice versa of a product P are flowed through, wherein the average flow velocity in Inner tube 300 and thus in the inner channel 200 * is marked with v. The cross-sectional interpretation is usually such that this mean flow velocity v is also present in a connecting sheet 1000, which is connected on the one hand to the fixed bearing side Ausauscherflansch 500 and on the other hand indirectly with a firmly connected to the loslagerseitigen pipe support plate 800 loslagerseitigen connecting piece 800d. With the two connecting sheets 1000 (so-called 180-degree pipe elbows) shown only half in each case in the drawing, the bundle of tubes 100.i in question is connected in series with the respectively adjacent bundle of tubes 1 00.i-1 and 100.i + 1 connected. Therefore, once the fixed bearing side exchanger flange 500 forms an inlet E for the product P and the loose bearing side fitting 800d accommodates an associated outlet A; in the respectively adjacent tube bundle 100.i-1 or 100.i + 1, these inlet and outlet conditions are reversed accordingly.

The fixed bearing side exchanger flange 500 has a first connection opening 500a, which corresponds to a nominal diameter DN and thus to a nominal passage cross section A _{0 of} the connection bend 1000 connected there and which is generally dimensioned such that there the mean flow velocity v in the inner tube 300 and Innenkanal 300 * corresponding flow velocity is present. In the same way, a second connection opening 800a in the loslagerseitigen connection piece 800d dimensioned, wherein the respective connection opening 500a or 800a on a respective enlarged passage cross section 500c and 800c in the region to the adjacent pipe support plate 700 or 800 through a conical transition 500b or 800b extended. The extended passage cross section 500c or 800c is substantially cylindrical and designed with a diameter which is usually one to two nominal diameters greater than the nominal diameter DN of the connecting bend 1000 (nominal passage cross section A _{o of} the connecting bend) and accordingly correspondingly larger than the total passage cross section of all the fixed bearing side exchanger flange 500 entering inner tubes 300 is dimensioned with a respective pipe inner diameter D _i .

Depending on the direction of the flow velocity v in the inner tube 300 or inner channel 300 *, the product P to be treated either flows via the first connection opening 500a or the second connection opening 800a to the tube bundle 100.1 to 100.n, so that either the fixed-bearing-side tube support plate 700 or the loslagerseitige pipe support plate 800 is flown. Since in each case a heat exchange between product P in the inner tubes 300 and the inner channels 300 * and a heat transfer medium M in the outer jacket 200 and in the outer channels 200 * has to be made in countercurrent, this heat transfer medium M flows either the first port 400a or the second connecting piece 400b with a mean flow velocity in the outer jacket c too.

A first shell-and-tube heat exchanger 101 (FIG. FIG. 2 and FIGS. 3a, 3b, 3c ) consists of a number n connected in series, parallel tube bundles 101.1 to 101.n, wherein in the embodiment n = 8 tube bundles 101.i (i = 1 to 8) are provided. Parallel to the first shell-and-tube heat exchanger 101, a second shell-and-tube heat exchanger 102 is provided which likewise consists of a number n of series-connected, parallel-arranged tube bundles 102.1 to 102.n (i = 1 to 8), both of which form the overall arrangement 100. Both Tube bundle heat exchangers 101 and 102 are connected according to the invention together to an inlet and distribution device 10, which consists of a manifold body 10.3, which continues on the input side into a first conical transition body 10.4 with a first flange 10.5 ( FIGS. 4 . 4a ). The distributor body 10.3 is preferably designed as an elongate hollow cylinder with an inner diameter D, which forms a distributor space V on the inside. This is with each inner tube 300, 300 * (see FIG. 1 ) of the respective first tube bundle 101.1, 102.1 ( FIG. 2 ) via a respective manifold 10.1.1 to 10.1.4 (10.1.i) from a first group of manifolds 10.1 and via a respective manifold 10.2.1 to 10.2.4 (10.2.i) from a second group of manifolds 10.2 separately connected, wherein an axial distance a of adjacent distributor tubes is at least as great as the maximum length of the fibrous components ( FIG. 4 ). It has proven to be advantageous to execute the axial distance a equal to or greater than the inner diameter D, wherein the design of the inner diameter D, taking into account the volume flow of the suspension P durchzusetzenden the desired average flow rate c of a respective partial flow P (T) allow in the respective inner tube got to.

A suspension P to be treated thermally enters the inlet and distribution device 10 via the first connection flange 10.5 in conjunction with the first conical transition body 10.4 (total flow of the suspension at the inlet P (E)), where it is located at the beginning of the flow Distributor body 10.3 can be visually observed via a sight glass 10.7 ( Figures 2 . 4 ). Within the distribution space V of the distributor body 10.3, the total flow of the suspension P (E) branches into the respective distribution pipes 10.1.1 to 10.1.4 on the one hand and into the distribution pipes 10.2.1 to 10.2.4 on the other. Such isolated partial flows P (T) of the suspension P (E) pass via a second connecting flange 10.6 arranged at the ends of the respective distributor tubes 10.1.1 to 10.1.4 and 10.2.1 to 10.2.4 to the respective first tube bundles 101.1 and 102.1 (FIG. FIG. 2 and FIGS. 3a , 3b , 3c . 4 ). The connection in the region of the second connecting flange 10.6 is designed such that here a tight connection with the respective corresponding inner tube of the first tube bundle 101.1, 102.1 is given. For flushing the distribution chamber V is located, in the flow direction seen, at the end of the manifold body 10.3 a controllable via a drive 11 a shut-off device 11, for example a ball valve, wherein the shut-off device 11 on its side facing away from the manifold body 10.3 side has a flushing port 11 b ( FIGS. 4 . 4a ).

The longitudinal axis of the distributor body 10.3 ( Figures 2 . 4 ) runs parallel to the tube bundle heat exchanger 101 and thus also to the tube bundle heat exchanger 102 arranged parallel to it. The first group of distributor tubes 10.1 is arranged in a meridian plane of the distributor body 10.3, the latter being perpendicular to an assembly plane AE of the first shell-and-tube heat exchanger 101 stands ( Figure 3c ). The second group of distribution pipes 10.2 is arranged diametrically opposite the first group 10.1. As a result of this symmetrical arrangement, identical flow conditions prevail in the inlet and distributor region of the two shell-and-tube heat exchangers 101, 102.

For the purpose of a targeted flushing of the manifolds 10.1.i, 10.2.i each group distribution pipes 10.1, 10.2 and the thus associated respectively inner tubes 300 is in FIG. 4 illustrated intake and distribution device 10 modified. This modified inlet and distribution apparatus 10 * shows FIG. 4a , There, each distributor tube 10.1.i, 10.2.i has a shut-off device 10.8.i or 10.9.i (10.8.1, 10.8.2, 10.8.3, 10.8.4, 10.9.1) in the region of its branch pipe connection opening at the distributor body 10.3. 10.9.2, 10.9.3, 10.9.4), wherein the first mentioned a first group shut-off 10.8 and the second mentioned form a second group shut-off 10.9. Each of these shut-off 10.8.i, 10.9.i is independent of the other either manually or remotely controlled selectively operable. To determine whether a manifold 10.1.i, 10.2.i and / or the respectively associated inner tube 300 is affected by deposits in its flow passage, is seen at each manifold 10.1.i, 10.2.i, in the flow direction, behind the respective shut-off device 10.8.i, 10.9.i a connection for a pressure measuring device 10.10 is provided. Blockages lead at the measuring point to an easily measurable, significant pressure change, with the at least one alarm message or a targeted flushing and flushing in question coming distribution pipes 10.1.i, 10.2.i (for example, flushing / cleaning R1 of the first manifold 10.1.1 in the first group distribution pipes 10.1) in conjunction with the associated inner tubes 300 and / or a flushing of the manifold body 10.3 (flushing / cleaning R) generated can be.

Each inner tube 300, 300 * (see FIG. 1 ) of a tube bundle (by way of example, the tube bundle 101.i is selected here; FIG. 2 and FIGS. 3a, 3b, 3c ) is separately connected to an associated inner tube 300, 300 * of the subsequent tube bundle 101.i + 1 via a connecting bend 20.1.i from a group connecting bend 20.1 a connection fitting 20 (see also FIGS. 5a and 5b ). The connection is made via a connection flange 20.5 bridging the two pipe support plates 700 and 800, respectively.

A number N = 4 inner tubes is, as in FIG. 5a is shown, evenly distributed on a common pitch diameter, wherein the arrangement is selected so that two adjacent tube bundles 101.i, 101.i + 1 are connected to only two different length connecting arc. Two long, identical connecting bows 20.1.1 and 20.1.2 are assigned to the four outer inner tubes (see also connecting bows 20.1.1 at the right-hand end of the tube bundles 101.i, 101.i + 1). Two short, identical connecting elbows 20.1.3 and 20.1.4 are assigned to the four inner inner tubes.

The partial flows P (T) of the two outer inner tubes of the adjacent tube bundles 101.i and 101.i + 1 ( Figures 2 and 3a ) take in the deflection valve 20, as shown above, the long flow path L _l (s FIG. 5b ). In the subsequent deflection of these partial flows P (T) at the left-hand end of the adjacent tube bundles 101.i + 1 and 101.i + 2, the two outer inner tubes of the tube bundle 101.i + 1 with respect to the tube bundle 101.i + 2 as it were to inside lying inner tubes, which are connected to the likewise inner inner tubes of the tube bundle 101.i + 2 via two short, same connecting arc 20.1.3 and 20.1.4. The partial flows P (T) of the two inner inner tubes of the adjacent tube bundles 101.i + 1 and 101.i + 2 ( Figures 2 and 3a ) take in the deflection valve 20 now the short flow path L _k (see also FIG. 5b ). As a result, the inventive approach is realized that the partial flow P (T) in the deflection of the inner tube 300, 300 * of the tube bundle 101.i to the associated inner tube 300, 300 * of the subsequent tube bundle 100.i + 1 on the one hand and from there to the associated inner tube 300, 300 * of the subsequent tube bundle 100.i + 2 on the other hand always has to overcome in the sum always equivalent or approximately equivalent flow resistance.

The inner tubes 300, 300 * of, as seen in the flow direction, each last tube bundle 101.n and 102.n open via a first collection sheet 30.2 and a second collection sheet 30.3 in a collecting body 30.1 a discharge and collection device 30 (connection via third connection flange 30.4). The collecting body 30.1 is preferably designed as an elongate hollow body and defines on the inside a collecting space S. The collecting body 30.1 is adjoined by a second conical transition body 30.5 and a fourth connecting flange 30.6. The outlet and collecting device 30 is space-saving in the area of the connection fittings 20 on one side of the tube bundle heat exchangers 101, 102 first substantially vertically ascending and then laid down substantially vertically, thereby emptying the tube bundle heat exchanger 101, 102 and thus a burning is prevented by residual suspension. In addition to this siphon effect, it homogenizes a suspension P (A) emerging from the last tube bundles 101.n and 102.n with regard to temperature and solids concentration, if this is still necessary in view of the arrangement according to the invention.

The heat exchange between the suspension P (partial flows P (T)) flowing at the mean flow velocity v in the inner tubes 300 and the inner channels 300 * and a heat transfer medium M flowing in the outer jacket 200 or in the outer channels 200 * takes place in countercurrent. In this case, the heat transfer medium M (E), for example hot water or, in the case of cooling of the products to be fermented, cooling water flows to the nth tube bundle 101.n on the one hand via the first connecting piece 400a with the mean flow velocity c in the outer shell ( FIG. 2 ). It leaves the tube bundle 101.n on the other hand via the second connecting piece 400b, which is connected to the first connecting piece 400a of the adjacent tube bundle 101.n-1 on a short path. Finally, the heat transfer medium M (A) leaves the first tube bundle 101.1 via the second connecting piece 400b with the mean flow velocity c in the outer jacket.

REFERENCE LIST OF ABBREVIATIONS USED FIG. 1 (prior art)

100

Shell and tube heat exchangers

100.1

100.2, ..., 100.i, ...

..., 100.n

Tube bundle; i = 1 to n

100.i

i'th tube bundle

200

outer sheath

200 *

outer channel

200a

fixed bearing side outer jacket flange

200b

loose-side outer jacket flange

300

inner tube

300 *

internal channel

400.1

first housing

400a

first connection piece

400a *

first cross channel

400.2

second housing

400b

second connection piece

400b *

second cross channel

500

fixed bearing side exchanger flange

500a

first connection opening

500b

first conical transition

500c

first extended passage cross-section

600

loose bearing side exchanger flange

700

fixed bearing pipe support plate (tube mirror plate)

800

loose-side tube carrier plate (tube mirror plate)

800a

second connection opening

800b

second conical transition

800c

second extended passage cross-section

800d

loose bearing side connection

900

gasket

910

O-ring

1000

compound bow

c

mean flow velocity in the outer jacket

n

Number of tube bundles 100.i

v

mean flow velocity in the inner tube

A

exit

A _o

Nominal passage cross-section of the connecting bow

D _i

Inner tube diameter (inner tube 300)

DN

Nominal diameter of the connecting elbow (A _o = DN ² π / 4)

e

entry

P

Product / suspension (temperature-treated side)

M

Heat transfer medium, general

Figures 2, 3a, 3b, 3c, 4, 4a, 5a, 5b

101

first shell-and-tube heat exchanger

102

second shell and tube heat exchanger

101.1, 101.2, ..., 101.i, ...

..., 101.n

first to nth tube bundles of the first shell and tube heat exchanger 101; i = 1 to n

102.1, 102.2, ..., 102.i, ...

..., 102.n

first to nth tube bundles of the second shell and tube heat exchanger 102; i = 1 to n

101.i

i-tes tube bundle of the first shell-and-tube heat exchanger 101

101.i + 1

the tube bundle 101.i downstream tube bundle

100.i + 2

the tube bundle 100.i + 1 downstream tube bundle

101.i-1

the tube bundle 101.i upstream tube bundle

102.i

i-th tube bundle of the second shell-and-tube heat exchanger 102

102.i + 1

the tube bundle 102.i upstream tube bundle

102.i-1

the tube bundle 102.i upstream tube bundle

10

Inlet and distribution device

10 *

modified inlet and distribution device

10.1

first group distribution pipes

10.1.1

first manifold of the first group

10.1.2

second manifold of the first group

10.1.3

third distributor pipe of the first group

10.1.4

fourth distributor tube of the first group

10.1.i

Manifold of the first group, general

10.2

second group of distribution pipes

10.2.1

first manifold of the second group

10.2.2

second manifold of the second group

10.2.3

third distribution pipe of the second group

10.2.4

fourth distributor tube of the second group

10.2.i

Manifold of the second group, general

10.3

distributor body

10.4

first conical transition body

10.5

first connection flange

10.6

second connection flange

10.7

sight glass

10.8

first group shut-off devices

10.8.1

first shut-off device of the first group

10.8.2

second shut-off device of the first group

10.8.3

third shut-off device of the first group

10.8.4

fourth shut-off device of the first group

10.8.i

Shut-off device of the first group, general

10.9

second group shut-off devices

10.9.1

first shut-off device of the second group

10.9.2

second shut-off device of the second group

10.9.3

third shut-off device of the second group

10.9.4

fourth shut-off device of the second group

10.9.i

Shut-off device of the second group, general

10:10

Connection for pressure measuring device

11

Shut-off device (eg ball valve)

11 a

drive

11 b

Flushing connection

20

connection fitting

20.1

Group connection sheet

20.1.1

first, long connecting bow

20.1.2

second, long connecting bow

20.1.3

first, short connection sheet

20.1.4

second, short connecting bow

20.1.i

Connecting bow, general

20.5

flange

30

Outlet and collection device

30.1

collecting body

30.2

first collection sheet

30.3

second collection sheet

30.4

third connection flange

30.5

second conical transition body

30.6

fourth connection flange

a

axial distance of the distribution pipes

AE

Arrangement plane of the (first) shell-and-tube heat exchanger 100 (101)

D

Inner diameter of the distributor body (distributor tube)

L _l

long flow path in the diversion valve

L _k

short flow path in the deflection valve

P

Suspension (e.g., biomass)

P (A)

Total flow of the suspension after exit

P (E)

Total flow of the suspension before entry

P (T)

Partial stream of the suspension

M (A)

Heat transfer medium, discharge (for example water)

M (E)

Heat transfer medium, inlet (for example water)

N

Number of inner tubes 300 of a tube bundle 100.i, 102.i

R

Rinsing / cleaning of the distributor body 10.3

R1

Rinsing / cleaning of the first distributor tube 10.1.1 of the first group

S

plenum

V

distribution space

Claims (18)

1. A process to guide the fluid in tube bundle heat exchangers (100; 101, 102) for thermally treating suspensions (P) containing particulate and/or long fiber components, wherein the tube bundle heat exchanger (100; 101, 102) consists of a plurality of equivalent, series-connected, substantially parallel tube bundles (100.1, 100.2, , 100.i, ..., 100.n; 101.1, 101.2, , 101.i,..., 101.n and 102.1, 102.2, 102.i..., 102.n), each tube bundle having an outer channel (200*) surrounded by an outer jacket (200) for a heat carrier medium (M) and a number of inner tubes (300) extending axially parallel to the outer jacket (200) through the outer channel (200*) and jointly forming an inner channel (300*), the end of which is supported in a tube carrier plate (700, 800), and through which a partial flow P(T) flows, and neighboring tube bundles are connected with each other by means of a flow connection ensuring the fluid guidance in the inner tubes (300; 300*),
   characterized in that

   - the collective flow of the suspension (P) is divided before entering the tube bundle heat exchanger (100; 101, 102) into a number of partial flows (P(T)),

   - the partial flows (P(T)) are generated at a distance that is as least as large as the greatest length of the fibrous components of the suspension (P), and

   - the individual partial flows (P(T)) are guided separate from each other through the entire tube bundle heat exchanger (100; 101, 102).
2. An apparatus to guide the fluid in tube bundle heat exchangers (100; 101, 102) for thermally treating suspensions (P) containing particulate and/or long fiber components, wherein the tube bundle heat exchangers (100; 101, 102) consist of a plurality of equivalent, series-connected, substantially parallel tube bundles (100.1, 100.2, , 100.i, ..., 100.n; 101.1, 101.2, , 101.i,..., 101.n and 102.1, 102.2, , 102.i,..., 102.n), each tube bundle having an outer channel (200*) surrounded by an outer jacket (200) for a heat carrier medium (M) and a number of inner tubes (300) extending axially parallel to the outer jacket (200) through the outer channel (200*) and jointly forming an inner channel (300*), the end of which is supported in a tube carrier plate (700, 800), and through which a partial flow P(T) flows, and neighboring tube bundles are connected with each other by means of a connection fitting (20) ensuring the fluid guidance in the inner tubes (300; 300*), characterized in that

   - viewed in the direction of flow, the first tube bundle (100.1; 101.1, 102.1) is assigned an inlet and distribution device (10) having a distribution body (10.3) that forms a distribution chamber (V) on the inside,

   - the distribution chamber (V) is separately connected to each inner tube (300; 300*) of the first tube bundle (100.1; 101.1, 102.1) by means of a distribution tube (10.1.i; 10.1.i, 10.2.i) from a group of distribution tubes (10.1; 10.1, 10.2), where the distance between neighboring distribution tubes is at least as large as the greatest length of fibrous components, and

   - each inner tube (300; 300*) of a tube bundle (100.i; 101.i, 102.i) is separately connected to an associated inner tube (300; 300*) of the following tube bundle (100.i+1; 101.i+1; 102.i+1) by means of a connecting bend (20.1.i) from of a group of connecting bends (20.1) of the connecting fitting (20),
3. The apparatus according to claim 2,
   characterized in that
   the respective partial flow P(T) through the inner tubes (300; 300*) from the distribution chamber (V) to the inlet of an outflow and collecting device (30) fed by all the inner tubes (300; 300*) of the last tube bundle (100.n; 101.n, 102.n) must overcome equivalent or approximately equivalent flow resistances.
4. The apparatus according to claim 2 or 3,
   characterized in that
   a first tube bundle heat exchanger (101) and a second tube bundle heat exchanger (102) are parallelly connected to the inflow and distribution device (10).
5. The apparatus according to one of claims 2 to 4,
   characterized in that
   the distribution body (10.3) is designed as an elongated hollow cylinder having an inner diameter (D), that the group(s) of distribution tubes (10.1; 10.1, 10.2) leaving the distribution body (10.3) is/are arranged in the lengthwise direction of the branch tube socket in the area of its/their branch pipe socket, and the distribution tubes (10.1.i; 10.1.i, 10.2.i) within their group have an axial distance (a) from each other that is greater than or equal to the inner diameter (D) (a≥ D).
6. The apparatus according to claim 5,
   characterized in that
   the lengthwise axis of the distribution body (10.3) runs parallel to the tube bundle heat exchanger(s) (100; 101, 102), and that the (first) group of distribution tubes (10.1) is arranged in a meridian plane of the distribution body (10.3), the latter lying perpendicular on an arrangement plane (AE) of the (first) tube bundle heat exchanger (100; 101).
7. The apparatus according to claim 6,
   characterized in that
   the second group of distribution tubes (10.2) is arranged diametrically opposite to the first group of distribution tubes (10.1).
8. The apparatus according to one of claims 5 to 7,
   characterized in that
   each distribution tube (10.1.i; 10.1.i, 10.2.i) has a shutoff device (10.8.i; 10.8.i, 10.9.i) in the area of its branch tube socket leaving the distribution body (10.3).
9. The apparatus according to claim 8,
   characterized in that
   each shutoff device (10.8.i; 10.8.i, 10.9.i) is actuated independent of the other optionally either manually or by remote control.
10. The apparatus according to claim 8 or 9,
    characterized in that
    viewed in the direction of flow, a connection is provided for a pressure measuring device (10.10) on each distribution tube (10.1.i; 10.1.i ,10.2.i) following the respective shutoff device (10.8.i; 10.8.i, 10.9.i).
11. The apparatus according to one of claims 2 to 10,
    characterized in that
    the distribution body (10.3) has a purging connection (11b) at its end facing away from its inflow side that can be shut off by means of a shutoff device (11).
12. The apparatus according to claim 11,
    characterized in that
    the shutoff device (11) is actuated either manually or by remote control.
13. The apparatus according to one of claims 2 to 12,
    characterized in that
    the connecting fitting (20) forms a complementary arrangement pattern in their connecting flange (20.5) of the inner tubes in the two tube support plates (700 or 800) to be tightly joined of neighboring tube bundles, and that the connecting fittings (20) create the flow connection between the respective inner tubes (300; 300*) on the ends of two neighboring tube bundles (100.i-1, 100.i; 101.i-1, 101.i and 102.i-1, 102.i) and the subsequent ends of the neighboring tube bundle (100.i, 100.i+1; 101.i, 101.i+1 and 102.i, 102.i+1) such that the respective flow path through the respective two connecting fittings (20) between the neighboring tube bundles always has the same cumulative flow resistance.
14. The apparatus according to claim 13,
    characterized in that
    s number N = 4 to N = 7, preferably N = 4, of inner tubes (300; 300*) is provided in a tube bundle (100.i; 101.i, 102.i).
15. The apparatus according to claim 14,
    characterized in that
    a number N = 4 of inner pipes (300; 300*) is arranged distributed evenly on a common pitch circle diameter such that two neighboring tube bundles are connected to only two connecting bends (20.1.1, 20.1.2 and 20.1.3, 20.1.4) of different length, wherein two long, equivalent connecting bends (20.1.1, 20.1.2) are assigned to the four inner pipes lying to the outside (300; 300*), and two short, equivalent connecting bends (20.1.3, 20.1.4) are assigned to the four inner pipes lying to the inside (300; 300*).
16. The apparatus according to one of claims 10 to 15,
    characterized in that
    the inner pipes (300; 300*) of the last tube bundle (100.n; 101.n, 102.n) end in an outflow and collection device (30) with a collecting body (30.1) that forms a collection chamber (S) on the inside.
17. The apparatus according to claim 16,
    characterized in that
    the collecting body (30.1) is designed as an elongated hollow cylinder.
18. The apparatus according to claim 16 or 17,
    characterized in that
    the collecting body (30.1) in the area of the connecting fittings (20) on one side of the tube bundle heat exchanger (100; 101, 102) is first run to rise substantially vertically, and then is run to descend substantially vertically.

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