WO2004052526A1 - Jacketed tube reactor comprising a bypass line for the heat transfer medium - Google Patents
Jacketed tube reactor comprising a bypass line for the heat transfer medium Download PDFInfo
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- WO2004052526A1 WO2004052526A1 PCT/EP2002/014189 EP0214189W WO2004052526A1 WO 2004052526 A1 WO2004052526 A1 WO 2004052526A1 EP 0214189 W EP0214189 W EP 0214189W WO 2004052526 A1 WO2004052526 A1 WO 2004052526A1
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- reactor
- tube reactor
- jacket tube
- heat transfer
- zone
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
- F28D7/0083—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium
- F28D7/0091—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium the supplementary medium flowing in series through the units
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
- F28D7/163—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing
- F28D7/1669—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing the conduit assemblies having an annular shape; the conduits being assembled around a central distribution tube
- F28D7/1676—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing the conduit assemblies having an annular shape; the conduits being assembled around a central distribution tube with particular pattern of flow of the heat exchange media, e.g. change of flow direction
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
- F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
- B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00389—Controlling the temperature using electric heating or cooling elements
- B01J2208/00407—Controlling the temperature using electric heating or cooling elements outside the reactor bed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00716—Means for reactor start-up
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/023—Details
- B01J2208/024—Particulate material
- B01J2208/025—Two or more types of catalyst
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F2250/00—Arrangements for modifying the flow of the heat exchange media, e.g. flow guiding means; Particular flow patterns
- F28F2250/06—Derivation channels, e.g. bypass
Definitions
- the invention relates to a tubular reactor according to the preamble of claim 1.
- a jacket tube reactor is a fixed bed reactor which offers the possibility of bringing about a heat exchange between the process gas mixture reacting in the fixed bed still within the fixed bed and also between the fixed bed itself and a separate heat transfer medium.
- the reaction can be either an endothermic or an exothermic one.
- the fixed bed - essentially a granular catalyst - is located in the tubes (reaction tubes) of a generally vertically arranged reaction tube bundle, the two ends of which are sealed in tube plates and which are surrounded by the heat transfer medium within a reactor jacket surrounding the tube bundle.
- the process gas mixture is fed to the tubes via a reactor hood spanning the tube plate in question and also discharged via a reactor hood spanning the other tube plate.
- the heat transfer medium - often a salt bath - is circulated by means of a circulation pump and heated or cooled by a heat exchanger depending on the type of reaction process.
- pumps and heat exchangers are usually outside the reactor jacket. Accordingly, the heat transfer medium enters the reactor jacket in the vicinity of a tube sheet and emerges from it in the vicinity of the other tube sheet.
- entry and / or exit points for the heat transfer medium can also be located in intermediate planes of the reactor jacket.
- a modern jacket tube reactor can contain up to 30,000 tubes or more - in the interest of a uniform reaction sequence and thus a high yield and good selectivity of the reaction product, it is important to find temperature differences in the heat transfer medium of the reactor jacket to keep small and above all to create the same possible flow conditions for all tubes.
- ring channels surrounding the reactor jacket have already been provided for the supply and removal of the heat transfer medium, and in the interior of the jacket distributor and deflection plates for the heat transfer medium - cf. about DE-A-2 207 166, which is assumed in the generic term -.
- alternating annular and disk-shaped deflection plates serve to bring about essentially transverse flows within the tube bundle by imparting a meandering course to the globally longitudinal flow within the reactor jacket.
- a heat exchanger in the form of a cooler is arranged in a slide-controllable shunt circuit to a main heat transfer circuit containing the reactor, circulation pump and an electric heater.
- the main flow passing through the reactor also inevitably changes, which in turn brings about changes in the inflow conditions for the individual reaction tubes.
- the pump must be sized accordingly in order to Driving phase of the reactor with cold and therefore relatively high viscosity heat transfer medium to be able to take into account the correspondingly high flow resistance of the same in the reactor.
- Changing the pump throughput on the other hand, for example by changing the speed, is relatively difficult to achieve.
- the invention is intended to remedy this. It is therefore based on the task of designing the heat exchange system in a tubular casing reactor in accordance with the preamble of claim 1 in such a way that the delivery capacity of the circulating pump in question is as low as possible at a constant nominal speed thereof and is independent of the heat output occurring in the reactor and of the viscosity of the heat transfer medium can.
- the relevant additional bypass makes it possible to compensate for any reduction or enlargement of the partial quantity passed through the heat exchanger without changing the pump output.
- the bypass in the start-up phase of the reactor when the heat transfer medium is still cold and therefore viscous enables the reaction vessel to be partially bypassed and thus the size and power requirements of the circulation pump and drive unit to be kept low.
- DE-A-1 963 394 already shows a jacket tube reactor with an external circulation pump and, in addition, a heat exchanger arranged in a shunt circuit, a controllable bypass being connected in parallel to the heat exchanger.
- the aim is to ensure that the circulation quantity passing through the heat exchanger and through the reaction vessel are constant at all load ranges.
- the bypass appears to be dimensioned such that it is only able to accommodate the partial flow that otherwise passes through the heat exchanger.
- FIG. 1 is a schematic of a jacket tube reactor with external heat exchanger, external circulation pump and bypass according to the present invention
- FIG. 3 shows a diagram with regard to the size of the individual partial flows as a function of the relevant valve position in different operating states of the arrangement according to FIG. 2,
- FIG. 4 shows a diagram comparable to that of FIG. 1, but with a reactor with subdivided ring channels
- FIG. 5 is a diagram similar to that of FIG. 4, but with a different valve arrangement
- 6 is a diagram similar to that of FIG. 5, but with a practical implementation of the bypass within a valve arrangement
- FIG. 8 is a diagram similar to that of FIG. 4, but with a modified line routing and valve arrangement
- FIG. 9 is a diagram of a similar slide valve, as can be used according to FIG. 8,
- FIG. 10 is a diagram similar to that of FIG. 1, but with a suction pressure increasing pre-pressure pump in connection with the circulation pump,
- FIG. 11 is a diagram similar to that of FIG. 4, but with two circulation pumps on diametrically opposite sides of the reactor,
- FIG. 12 is a diagram similar to that of FIG. 11, but with a single heat exchanger
- FIG. 13 shows an application diagram of the invention with a multi-zone reactor
- 16 shows a further application diagram of the invention with a multi-zone reactor
- 17 shows an application diagram of the invention with a single-zone reactor with three ring channels
- FIG. 21a) and b) a schematic elevation or horizontal section similar to FIG. 20a) or b), but with the flow direction reversed and in connection with the lower reactor zone arranged circulation pump,
- a jacket tube reactor 2 with two ring channels 4 and 6 in the vicinity of the upper and lower end of the reaction vessel 8 is shown, the process gas mixture reacting therein - only exemplary - from top to bottom, from the heat transfer medium, however, viewed globally from bottom to top, ie in countercurrent to the process gas mixture, is flowed through.
- the heat transfer medium is fed from the upper, ie in this case the heat transfer outlet-side ring channel 4 via a line 10 to a circulating pump 12 which conveys the heat transfer medium via a line 14 to the lower ring channel 6 and thus back into the reaction container 8.
- a partial flow of the heat carrier conveyed by the circulation pump 12 passes via a heat exchanger 16, such as a cooler, within a valve-controlled shunt circuit 18 back to the inlet 20 of the circulation pump 12, through which it is admixed to the main stream supplied to the reactor 2 through line 14.
- the circulation pump 12 is also connected in parallel with a likewise valve-controlled bypass 22, which is likewise able to return a partial flow of the heat carrier conveyed by the circulation pump to its inlet 20.
- bypass 22 can also, as indicated by dashed lines in FIG. 1, lie in the shunt circuit 18 containing the heat exchanger 16. It can be seen that the valves 24 and 26 of the shunt circuit 18 or the bypass 22 can then also be replaced by a single multi-way valve, as is the case according to FIG. 2.
- an electric heater 30 is connected to them according to FIG. 1 in a further shunt circuit, 28, as is provided in many cases when the reactor is started up heat still cold heat transfer media to a temperature suitable for starting the reaction.
- the shunt circuit 28 is also shown valve-controlled, but it has been shown that the valve 32 in question can usually be omitted without damage.
- the partial flow passing through the heater is stopped by a stationary throttle element or the like. Expediently limited to ⁇ 5%, preferably ⁇ 3%, of the total amount of heat transfer medium circulated.
- An electric heater can also be replaced by a steam or flue gas heated or a fired heater.
- the throughput through the bypass 22 in the start-up phase of the reactor is controlled as a function of the heat transfer medium such that the reaction vessel 8 and, if appropriate, also the heat exchanger 16 (at least if the latter is a cooler) are still relatively cold and thus viscous heat transfer media are largely avoided, while the throughput is regulated by the bypass in stationary operation of the reactor so that the throughput through the reaction vessel 8 remains largely constant regardless of the heat output to be removed or supplied.
- This constant throughput can be achieved according to the invention with a constant pump output. It is of great importance for a constant flow against the reaction tubes present in the reaction container 8, since the local flow conditions within the reaction container also change as the flow rate of the heat transfer medium changes. For example, turbulent flow could change to laminar flow or take a different route at deflection points due to reduced centrifugal effects. Furthermore, a constant pump throughput under operating conditions is important for an optimal design of the circulating pump.
- the pump output can be changed if necessary, for example for a programmed change in output of the reactor. This can be done by changing the speed or changing the geometry of the pump, but these are relatively complex measures that one tries to avoid.
- FIG. 2 shows an arrangement as shown in principle in FIG. 1, more precisely with a bypass 22 arranged in the shunt circuit 18 with the heat exchanger 16 (as in FIG 1), an advantageous embodiment.
- the same reference numbers are used for this, as continues.
- the two valves 24 and 26 are replaced in series with the heat exchanger 16 or in the bypass 22 by a common multi-way valve, 34.
- mixers 38 and 40 are now provided at the inlet of the circulation pump 12 and at the junction of the bypass 22 with the return line 36 from the heat exchanger 16.
- a mixer could also occur at the outlet of the circulating pump 12 or in the ring channel, here ring channel 6, on the heat carrier inlet side.
- Mixers such as the mixers 38 and 40 from FIG. 2, can also be provided at all points that are suitable for this in the exemplary embodiments described below, even if not specifically shown.
- Fig. 3 the previously described Steuer point. Control process with reference to an arrangement illustrated in principle in FIG. 2 using a diagram.
- the valve path or stroke of the valve 34 is plotted on the abscissa thereof, while the ordinate indicates the throughput V B through the bypass 22 as well as that V c through the heat exchanger 16.
- I which is considered for starting the reactor, the bypass 22 is largely open, while the flow through the heat exchanger 16 is blocked, at least on the assumption that this is a cooler.
- FIG. 4 shows a jacket tube reactor 50 which is largely the same as the reactor 2 from FIG. 1, but in which the circulation pump 12 with its lines 10 and 14 on the one hand and the shunt circuit 18 containing the heat exchanger 16 together with the bypass 22 at various points on the ring channels 4 and 6 are connected. Contrary to the illustration, these locations can also occur, for example, on diametrically opposite sides of the reactor 50.
- the two ring channels 4 and 6 are each divided by a vertical partition 52 and 54, respectively, and the respective lines 14 and 56, respectively, are branched by the pump 12 and the heat exchanger 16, the two branches of line 56 are also provided with continuously adjustable valves 58 in order to be able to distribute the relevant inflow in the desired manner between the two ring channel ends 60 and 62 formed by the partition wall 52. It is understood that the valves 58 could also be replaced by a common multi-way valve, possibly in the form of a flap.
- FIG. 5 shows the same jacket tube reactor 50 with the same connected circulation pump 12 as in FIG.
- FIG. 6 shows an arrangement basically like that according to FIG. 4, but the multi-way valve 34 is combined with the bypass 22 in a single valve unit 68, as is shown schematically in FIG. 7. Thereafter, a line 70 coming from the ring channel 6 enters the valve unit 68, as does the discharge line 36 from the heat exchanger 16. On the other hand, the inlet line 64 to the heat exchanger 16 emerges from the valve unit 68, as does the line 56 to the ring channel 4.
- valve unit 68 The functioning of the valve unit 68 can be seen from FIGS. 7a) - c), which show the valve unit 68 in different phases.
- V R ⁇ , V Ro , V and V Co correspond to the designations also entered in FIG. 6.
- V B forms the bypass flow, as was the case with the previously described embodiments passes through the bypass channel 22.
- FIG. 7a corresponds to the start-up phase of the reactor, in which the heat transfer medium still has to be heated up, or the state in the event of an interruption in operation.
- the state according to Fig. 7b) corresponds to the "control phase" in the operation of the reactor.
- Fig. 7c) would correspond to the full load state, where the entire partial flow branched off at the circulation pump flows over the heat exchanger, the bypass is therefore deactivated. According to the invention, this state should only be reached in exceptional cases. Since the valve slide 76 is always pressurized on both sides, except in the case of FIG. 7 a), where the incoming heat transfer medium can flow freely, it is essentially relieved of pressure, so that it can be adjusted easily and sensitively. The valve 24 in the line 26 can also be omitted under certain circumstances, since the partial flow V C ⁇ conducted via the heat exchanger 16 is anyway controlled by the valve unit 68.
- FIG. 8 shows a jacket tube reactor 90 which is essentially the same as the reactor 50 from FIGS. 4 to 6, but in which the circulating pump 12 and the shunt circuit 18 containing the heat exchanger 16 and bypass 22 are connected to one another, ie along one and the same jacket line of the reactor lying Points are connected to the ring channels 4 and 6.
- two separate lines 96 and 98 enter a multi-way valve 100 from the two sections 92 and 94 of the ring channel 6, as is shown schematically in FIG. 9 with further elements.
- the line 64 to the heat exchanger 16 and the bypass 22 emerge from the valve 100, just as the outlet line 36 from the heat exchanger 16 merges with the bypass 22 before entering the annular channel 4.
- the subsequent return line 56 is branched from the outset, and throttle elements 102 are installed in both branches, in order to determine the distribution of the heat transfer medium between the two sections 60 and 62 of the ring channel 4.
- the throttle bodies 102 thus replace the two valves 58 from FIGS. 4 to 6, which generally only need to be set once.
- expansion tanks 104 and 106 above the circulating pump 12 and the heat exchanger 16 are shown, as are usually used to keep the entire heat transfer circuit completely filled with heat transfer medium and to maintain a certain minimum pressure therein and create a compensation volume.
- the multi-way valve 100 together with the bypass 22 and the throttle elements 102 is shown schematically as a common valve unit 108 similar to the previously described valve unit 68 in FIG. 9.
- the valve unit 108 has a valve housing 110 with a valve bore 112 and a plurality of channels 114-124 opening laterally therein, and a symmetrical valve slide 126. If we refer to FIG. 8, lines 96 and 98 open into channels 118 and 120 and line 36 into channel 122, while line 64 from channel 124 and two branches of line 56 from channels 114 and 116 out.
- the throttle bodies 102 are in the ca channels 114 and 116 installed.
- the bypass 22 is integrated in the valve unit 108.
- the slide rod 128 runs upwards through a further container 130 filled with heat transfer medium, next to the expansion container 106, to a cylinder-piston unit 132 for actuating the valve slide 126.
- Fig. 10 shows an arrangement similar to that of Fig. 1 with the bypass 22 in the position shown in dashed lines there, although the direction of flow of the heat transfer medium is reversed, i.e. the heat transfer medium, seen from top to bottom, passes through the reaction vessel 8.
- the connections on the ring channels 4 and 6 are simply interchanged.
- pre-pressure pump 136 in the case shown consisting of an injector, which is operated with a partial flow of the heat carrier conveyed by the circulating pump and branched off from the discharge line 138 of the circulating pump 12 and which feeds into the feed line 140 of the circulating pump, whereby Heat carrier is sucked out of an expansion tank 142 comparable to the expansion tank 106 from FIG. 7. 10 could of course also take the form of an additional pump impeller on the shaft of the circulation pump 12.
- Such a pre-pressure pump of any type is to avoid the pressure on the suction side of the circulating pump 12 dropping to a value that is so low that cavitation occurs, as is otherwise to be feared, particularly in the case of a relatively compact design of a powerful pump.
- a cavitation-protected circulation pump for a jacket bath-cooled jacket tube reactor is taken from FR 2 660 375 AI known.
- this pump which pumps from bottom to top, a partial flow of the heat transfer medium is returned from the pump outlet within the pump housing to the pump inlet, while at the same time a certain minimum level of the heat transfer medium above the pump outlet is maintained by the partial flow in the pump housing.
- cavitation alone cannot be prevented by such measures, regardless of whether the pump is pumping from bottom to top or from top to bottom.
- a compensating line 146 opens into a riser pipe 144 within the container 142, into which a degassing line 148 in turn opens out from the inside of the reaction container 8. Since there is generally a substantially higher pressure inside the reaction vessel 8 than in the expansion vessel 142, a throttle 149 is installed in the degassing line 148.
- FIG. 11 shows an arrangement similar to that according to FIG. 3 (apart from the mixers 38 and 40 shown there), but in a symmetrical arrangement on diametrically opposite sides of a jacket tube reactor 150 with correspondingly halves 154 on both sides by dividing walls 152 and 153 and 156 or 158 and 160 divided ring channels 4 and 6. Both sides are completely the same.
- the arrangement according to FIG. 11 essentially corresponds to that according to DE-34 09 159 AI with the exception that there is a common heat exchanger between the connection points of the circulation pumps connected to the ring channels and a bypass is missing.
- FIG. 12 shows a similar arrangement with a jacket tube reactor 162 with two diametrically opposite circulation pumps 12, but with a common one connected to the ring channels 4 and 6 at an intermediate point Heat exchanger 16 - so far more comparable with DE 34 09 159 AI -.
- the ring channel 4 in this example corresponds completely to the ring channel 4 according to FIG. 11, the ring channel 6 is divided by a helical partition 164 into two sections 166 and 168 tapering away from the feed point of the respective pumps 12, as seen in isolation , but for both ring channels, is known from DE 43 26 643 AI. It has been shown that such a subdivision, as shown in FIG. 12 for the ring channel 6, essentially brings advantages only for the ring channel on the heat carrier inlet side.
- a single multi-way valve 170 which in principle can be constructed similarly to the valve unit 68 from FIG. 7, is located at the feed point of the heat transfer medium subjected to the heat exchange in the ring channel 4 on the heat transfer outlet side instead of two separate valves.
- the valve 170 can be omitted without disadvantage in such a ring channel system without disadvantage, since the two heat transfer streams fed into the reaction vessel 8 via the ring channel sections 166 and 168 mix sufficiently.
- the helical partition 164 shown in FIG. 12 could also be replaced by an approximately Z-shaped angled section with a longer horizontal section, as in the parallel patent application PCT / EP02 / 14188 "ring channel for the supply and discharge of the heat transfer medium shown on a tubular reactor ".
- the overlap of the ring channel sections 166 and 168 expediently makes up between 1 and 100%, preferably between 20 and 100% and most suitably between 50 and 100% of the total length of the ring channel.
- FIG. 13 shows a multi-zone jacket tube reactor 180 with two reaction vessels 182 and 184 which adjoin one another at the end, similar to the reaction vessel 8 approximately from FIG. 1, each with two ring channels 4 and 6 at their two ends.
- Both like this Reactor zones formed, I and II, have the same heat transfer circuit systems with a circulation pump 12 connected on one side to the respective ring channels 4 and 6 and a bypass 22 containing a heat exchanger 16 and a bypass 22 on the diametrically opposite side connected to the same ring channels. That the two Circulation pumps 12 in FIG. 13, in contrast to the heat exchangers 16, are shown lying at the same height, to symbolize that, together with their drives, they are expediently arranged on one level for constructional reasons.
- a common expansion tank 104 is shown above both circulation pumps 12 only as an example. Of course, separate expansion tanks could also be provided. Furthermore, in contrast to FIG. 13, the global heat transfer streams in the two reactor zones I and II could also be in opposite directions, as well as in opposite directions to the reaction gas mixture passing through the reactor.
- a pre-pressure pump such as the pre-pressure pump 136 from FIG. 10, can again be added to one or both of the circulation pumps 12.
- both reaction vessels, 182 and 184 can have separate tubes with possibly different number and arrangement of tubes, which end in adjacent tube sheets, or can have a common, continuous tube and only through one around the tubes more or less sealing cutting disc to be separated from each other on the heat carrier side.
- 14 shows a similar multi-zone reactor 180, in which the two heat transfer circuits are, however, linked to one another and have their own heat exchanger 16, although they have separate circulating pumps 12 and bypasses 22.
- Another difference here is that the heat carrier flow through the reaction vessels 182 and 184 here - only by way of example - takes place in the opposite sense, ie in countercurrent to the reaction gas mixture.
- FIG. 15 again shows a similar multi-zone reactor 180 with two circulation pumps 12 and a common heat exchanger 16.
- this arrangement is essentially comparable to that according to FIG. 13.
- apart from the common heat exchanger 16 it differs from this in that the global directions of flow of the heat carrier through the reaction vessels 182 and 184 are opposite.
- the heat transfer medium passes through the reaction vessel 182 in countercurrent to the reaction gas mixture, it moves in the same way in the reaction vessel 184.
- the directions of passage could of course also be reversed.
- the expansion tank 16 of the heat exchanger 16 according to DE-A-2 207 166 can be dimensioned such that the heat exchanger tube bundle can be pulled out through it for repair or maintenance work without the heat transfer medium for this purpose must be drained.
- zone II schematically shows a multi-zone jacket tube reactor 190 with two successive zones I and II, only separated from one another by a separating disc 192, each with two ring channels 4 and 6 in connection with a single circulation pump 12, a single heat exchanger 16 and a single to bypass 22. While there are alternating annular and disk-shaped deflection plates 194 and 196 in reactor zone I, as are known, for example, from DE-A-2 201 528, zone II contains a single annular deflection plate 194. Both zones are in the form of a heat transfer circuit connected to one another, the heat transfer medium, viewed globally, passes through in countercurrent to the reaction gas mixture.
- heat medium which has passed through the heat exchanger 16 only enters directly into the lower zone, II, which, in the event that the heat exchanger 16 is a cooler, can also simply be an unreactive cooling zone.
- the upper zone I is cooled in this case only in that the cooled heat transfer medium from zone II returns via a return line 198 to the inlet of the circulating pump 12, from which the main stream then enters zone I through the lower ring channel 6.
- the reaction tubes in the zone II can be filled with an inert material instead of a catalyst.
- FIG. 17 shows a variant compared to FIG. 16 with a type of multi-zone reactor 200, in which two successive zones I and II with continuous tubing are separated from one another by an intermediate heat transfer inlet zone III instead of by a separating disk, and accordingly only a total of three ring channels, 202, 204 and 206.
- the heat transfer medium which is conveyed by a single circulation pump 12 and in part in a shunt circuit 18 via a heat exchanger 16, enters the heat transfer zone III through the central ring channel 204 in order to branch into a partial flow which flows from bottom to top the reactor zone I passes through and another partial stream which enters the reactor zone II from above and leaves it through the lowermost ring channel, 206.
- the subsequent return line 198 is drawn in a valve-controllable manner, but this is not mandatory.
- the process gas mix from bottom to top through reactor 200, but a top-to-bottom passage could also be used here. It is only essential that the two reactor zones I and II are flowed through in opposite directions by the heat transfer medium.
- FIG. 18 shows a variant compared to FIG. 17 with a multi-zone reactor with only two ring channels 202 and 204, while the ring channel 206 together with the line 198 in the interior of the reaction vessel 208 concerned is replaced by pipes 212 leading to the windows 210 of the ring channels 202.
- the tubes 212 as symbolized by the small arrows drawn on them, can each have a plurality of inlet and outlet openings in different planes.
- the height of a single reactor zone is advantageously between 10 and 80%, preferably between 20 and 80%, of the total height of all reactor zones.
- FIG. 19 shows a single-zone jacket tube reactor 220, in this respect similar to reactor 2, for example according to FIG. 1, but in contrast to this, in addition to the two terminal ring channels 4 and 6, a further ring channel, 222, is provided.
- the ring channel 222 is connected via a valve-controlled line 224 to the line 10 leading from the ring channel 4 to the circulating pump 12, which in this case is also valve-controlled.
- the main heat carrier flow supplied to the reaction vessel 226 through the ring channel 6 can be divided in any desirable manner into two partial streams, one of which already exits through the ring channel 222, while the other flows through the rest of the reaction vessel up to the ring channel 4.
- the valve le in lines 10 and 224 can be replaced by a multi-way valve.
- the reaction gas mixture passes through the reactor 220 from bottom to top. Assuming that the reaction taking place therein is an endothermic reaction and accordingly the heat exchanger 16 forms a heater, the reaction gas mixture entering can be preheated more or less intensively. In the same way, after-cooling could also take place in the case of an exothermic reaction and reverse flow.
- mixers can be provided at points that are suitable for this, in order to uniformly temper the respectively conducted heat carrier flows, as well as generally expansion tanks, degassing elements, admission pressure pumps and the like. Can find use.
- a multi-zone reactor such as the multi-zone reactor 180 shown in FIG. 14, can also be designed with more than two zones and with a corresponding number of pumps, although several zones can have one or more heat exchangers in common.
- a four-zone reactor with four pumps and two heat exchangers that are common to two zones can be built, just as a common heat exchanger is conceivable for all zones. All pumps or at least their drives are expediently arranged at the same height laterally above the reactor.
- Each pump and each heat exchanger can be equipped with an expansion tank 15, like the expansion tanks 104 or 106 shown in FIG. 15.
- the expansion tanks can communicate with one another, as is already apparent in principle from DE-A-2 207 166, or common expansion tanks can be used for several pumps and / or heat exchangers , In the latter cases, the expansion tanks can complement each other.
- the pumps are not arranged at the same height, there may be leakages between adjacent zones, especially when a pump is switched off, through the respective cutting disc. In this case, the excess resulting in the lowest zone can be discharged into a tank, from where it is returned to the top zone.
- the heat exchangers with the pumps are arranged essentially at the same level, there is the advantage that the heat exchanger tube bundle can be removed and installed without the heat transfer medium having to be drained off for this purpose. This also applies if, in the case of heat exchangers in the form of evaporative coolers, the bundle of cooler tubes with the steam drum is assembled with water and / or droplet separators and the like.
- the process used in such a multi-zone reactor can be a multi-stage, the number of process stages need not be the same as that of the reactor zones.
- acrolein is produced from propylene and in the other two stages from acrylic acid.
- the heat transfer medium in the individual stages can, depending on the requirements of each stage, be run globally in cocurrent or in countercurrent with respect to the process gas stream.
- a hot gaseous medium mostly air, which is not critical for the catalyst, is passed through the contact tubes of the reactor until they have warmed to a temperature above the melting point of the heat transfer medium.
- the gas throughput and the temperature rise for the preheating time are calculated.
- the heating rate is limited so that the reactor does not suffer any damage.
- Additional devices, such as pumps, heaters and pipes, can be preheated by trace heating.
- the already liquefied heat transfer medium is filled in. If the circulation pump is in operation, the liquid heat transfer medium, which is further heated, for example, by an electric heater such as heater 30 (FIG. 1), can be used to heat up to the operating temperature.
- the heating process can be carried out in stages. Initially, only the heat transfer circuit of the first zone with the heat transfer medium filled can be started up and heated with the heater switched on. To heat the second zone, hot gas is passed through the contact tubes, which is further heated in the first zone that has already been put into operation. The second zone is preheated until the heat transfer medium can also be filled in there. If this has happened, the second zone can be further heated via the heat transfer medium on the part of its own heater, or a bypass can be provided via which the second zone can be heated by the heater of the first zone. Such a bypass may also be useful for starting the reaction. A lot of heat is often required for this, since only one component of the process gas mixture is initially charged to the reactor.
- the reactor naturally does not generate any heat.
- the heater is usually not designed for start-up performance.
- the remaining heat is extracted from the heat transfer medium, which cools down accordingly.
- the amount of heat transfer medium from several zones can be used via the bypass mentioned.
- reactors If several reactors are arranged one behind the other, they can be heated and filled in succession in a similar manner.
- the catalyst in the reactor is to be conditioned, tempered or otherwise treated with a medium, such as a gas mixture, this depends on the nature of the catalyst.
- the treatment in question usually takes place after the heat transfer medium has been filled in at the appropriate temperature. Before filling, the heat transfer medium is usually preheated and melted in a separate tank.
- Corresponding suggestions can be found, for example, in the paper "Molten Salt for Heat Transfer" by H.P. Voznick and V.W. Uhl in Chemical Engineering, May 27, 1963, pages 129-135.
- FIGS. 20 to 23 show circulation pump arrangements of the kind that can be used in particular in connection with the invention on jacket tube reactors in which the inlet and outlet of the circulation pump are further apart than the connections of the relevant ring channels for the supply and discharge of the heat transfer medium.
- FIG. 20 shows in a partially sectioned elevation or a horizontal section a circulating pump 230 in the form of an axial pump on a two-zone jacket tube reactor 234 with the reactor zones 236 and 238 and accordingly four ring channels 240, 242, 244 and 246 Pump 230 connected to the upper reactor zone, 236. It contains a pump impeller 248 within a pump housing 250 and on a vertical shaft 252 which passes through an expansion tank 254 above the pump housing 250 and is directly driven by an electric motor (not shown) located thereover.
- the pump housing 250 contains a channel 256, which widens downward in the direction of flow, in the nozzle direction, in which, in the example shown, flow guide vanes 258 and 260 are located in front of and behind the pump impeller 248.
- the pump housing 250 connects with an inlet 262 and an outlet 264 directly to the two ring channels 240 and 242 of the upper reactor zone 236 of the reactor 234. Since their distance is less than that of the inlet and outlet of the pump 230, the outlet 264 is cranked sideways.
- the outlet 264 of the pump 230 branches off on both sides as it enters the annular channel 242, with additional baffles 266 and 268 ensuring an orderly flow guidance. Similar baffles, such as baffle 268 in particular, can also be provided at the inlet 262 of the pump housing, as shown in FIG. 20b).
- FIG. 21 shows a circulation pump 270 at the lower zone 238 of the two-zone reactor 234 on the assumption that the global axial flow direction of the heat carrier is reversed with respect to the upper zone 236.
- the inlet 272 of the pump 270 is connected to the lower ring channel 246, the reactor zone 238, while the outlet 274 coming from above opens into the ring channel 244, since it is often advisable for cavitation reasons to have the pump pumped from top to bottom ,
- the heat transfer medium is guided through a vertical section 276 to the entry of the pump.
- the pump 270 of the lower reactor zone 238 is expediently arranged at the same level as the pump 230 of the upper zone 236 from FIG. 20.
- the expansion tanks become correspondingly 254 all pumps can be arranged at the same height.
- the pump shaft 252 is mounted above the respective expansion tank 254 in order to be able to reliably protect its mounting and its drive from corrosion in a simple manner.
- the entry and exit of the ring channels 244 and 246 can also be equipped with baffles such as 266 and 268.
- bend of the outlet 264 of the pump 230 or of the inlet 272 of the pump 270 can also be provided on both sides of the respective pump housing.
- FIG. 22 shows how, in the case of a circulation pump 280 similar to the pump 230 from FIG. 20, inlet 282 and outlet 284 can surround the actual pump housing 286.
- FIG. 23 shows a circulation pump 290 in connection with the ring channels 244 and 246 of the lower reactor zone 238 similar to the circulation pump 270 of FIG. 21, but now the inlet 292 surrounds the actual pump housing 294. With 296 are arranged within the inlet 292 baffles, as they could also occur in the outlet 284 of the circulation pump 280 of FIG. 22 as well.
- FIG. 23a) shows schematically how, for example, a form pump 298 in the form of an injector similar to the form pump 136 from FIG. 10 can be connected to the circulating pump in question, in order to keep the expansion tank low and, accordingly, to keep the pump shaft 252 short, despite the risk of cavitation can .
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Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2004557842A JP2006508794A (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor for catalytic gas phase reactions. |
AU2002358695A AU2002358695A1 (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
PCT/EP2002/014189 WO2004052526A1 (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
EP02792994A EP1569744A1 (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
CN02830022.XA CN1708350A (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/EP2002/014189 WO2004052526A1 (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004052526A1 true WO2004052526A1 (en) | 2004-06-24 |
Family
ID=32479699
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2002/014189 WO2004052526A1 (en) | 2002-12-12 | 2002-12-12 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP1569744A1 (en) |
JP (1) | JP2006508794A (en) |
CN (1) | CN1708350A (en) |
AU (1) | AU2002358695A1 (en) |
WO (1) | WO2004052526A1 (en) |
Cited By (14)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2006120026A2 (en) * | 2005-05-13 | 2006-11-16 | Ashe Morris Ltd | Variable plate heat exchangers |
WO2006120028A1 (en) * | 2005-05-13 | 2006-11-16 | Ashe Morris Ltd | Variable heat flux heat exchangers |
WO2008076039A1 (en) * | 2006-12-19 | 2008-06-26 | Alfa Laval Corporate Ab | A sectioned flow device |
EP1946829A1 (en) * | 2007-01-05 | 2008-07-23 | Sterecycle Ltd. | Process and apparatus for waste treatment |
GB2448390A (en) * | 2007-01-05 | 2008-10-15 | Sterecycle Ltd | Process and apparatus for waste treatment |
SG146539A1 (en) * | 2007-03-09 | 2008-10-30 | Hitachi Plant Technologies Ltd | Temperature adjustment system and temperature adjustment method of product |
US8309067B2 (en) * | 2005-12-07 | 2012-11-13 | Conopco, Inc. | Hair straightening composition comprising a disaccharide |
WO2012084406A3 (en) * | 2010-12-22 | 2012-11-22 | Tridelta Hartferrite Gmbh | Device for cooling a pourable or liquid product |
EP2581132A2 (en) | 2011-10-13 | 2013-04-17 | MAN Diesel & Turbo SE | Tube bundle reactor |
DE102011121543A1 (en) | 2011-10-13 | 2013-04-18 | Man Diesel & Turbo Se | Tube bundle reactor useful for catalytic gas-phase reactions, comprises bundle of reaction tubes, heat carrier-annular flow channel, external pump comprising pump housing, main heat exchanger, second heat carrier-annular return channel |
ITMI20130857A1 (en) * | 2013-05-27 | 2014-11-28 | Versalis Spa | APPARATUS FOR RECOVERING THE ENTHALPY OF REACTION |
WO2014202503A1 (en) * | 2013-06-17 | 2014-12-24 | Basf Se | Method and system for carrying out an exothermic gas phase reaction on a heterogeneous particulate catalyst |
FR3027663A1 (en) * | 2014-10-27 | 2016-04-29 | Commissariat Energie Atomique | EXCHANGER REACTOR COMPRISING MEANS FOR MODIFYING THE DISTRIBUTION OF A HEAT TRANSFER FLUID |
WO2020247158A1 (en) * | 2019-06-03 | 2020-12-10 | John Bean Technologies Corporation | Fluid retort installation and methods for circulating process fluid |
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DE102010014642B4 (en) * | 2010-04-12 | 2014-08-07 | Man Diesel & Turbo Se | Temperature control device and method for controlling the temperature of a tube bundle reactor |
DE102018113735A1 (en) * | 2018-06-08 | 2019-12-12 | Man Energy Solutions Se | Process, tube bundle reactor and reactor system for carrying out catalytic gas phase reactions |
CN115888564A (en) * | 2022-10-31 | 2023-04-04 | 东方电气集团东方锅炉股份有限公司 | Double-pump circulation loop maleic anhydride reactor complete device and control method thereof |
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SE9502189D0 (en) * | 1995-06-16 | 1995-06-16 | Tetra Laval Holdings & Finance | plate heat exchangers |
JP3948798B2 (en) * | 1997-10-27 | 2007-07-25 | 株式会社日本触媒 | Acrylic acid production method |
AU2135099A (en) * | 1998-03-27 | 1999-10-07 | Karmazin Products Corporation | Aluminum header construction |
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2002
- 2002-12-12 CN CN02830022.XA patent/CN1708350A/en active Pending
- 2002-12-12 JP JP2004557842A patent/JP2006508794A/en active Pending
- 2002-12-12 WO PCT/EP2002/014189 patent/WO2004052526A1/en not_active Application Discontinuation
- 2002-12-12 EP EP02792994A patent/EP1569744A1/en not_active Withdrawn
- 2002-12-12 AU AU2002358695A patent/AU2002358695A1/en not_active Abandoned
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US3760870A (en) * | 1969-12-18 | 1973-09-25 | Deggendorfer Werft Eisenbau | Cooler construction for circulating controlled amounts of heat carrier from a reaction vessel |
US5759500A (en) * | 1996-01-16 | 1998-06-02 | E. I. Du Pont De Nemours And Company | Fluid reactor with catalyst on floating tubesheet |
DE19857842A1 (en) * | 1998-12-15 | 2000-06-21 | Basf Ag | Reactor module with a contact tube bundle |
DE10232967A1 (en) * | 2001-07-20 | 2002-12-05 | Basf Ag | Oxidation synthesizing reactor for e.g. synthesis of phthalic acid anhydride, comprises diagonal-action impeller wheel with heat medium throttle gap parallel to shaft |
Cited By (22)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2006120026A2 (en) * | 2005-05-13 | 2006-11-16 | Ashe Morris Ltd | Variable plate heat exchangers |
WO2006120028A1 (en) * | 2005-05-13 | 2006-11-16 | Ashe Morris Ltd | Variable heat flux heat exchangers |
WO2006120026A3 (en) * | 2005-05-13 | 2007-01-11 | Ashe Morris Ltd | Variable plate heat exchangers |
US8309067B2 (en) * | 2005-12-07 | 2012-11-13 | Conopco, Inc. | Hair straightening composition comprising a disaccharide |
WO2008076039A1 (en) * | 2006-12-19 | 2008-06-26 | Alfa Laval Corporate Ab | A sectioned flow device |
US8567487B2 (en) | 2006-12-19 | 2013-10-29 | Alfa Laval Corporate Ab | Sectioned flow device |
EP1946829A1 (en) * | 2007-01-05 | 2008-07-23 | Sterecycle Ltd. | Process and apparatus for waste treatment |
GB2448390A (en) * | 2007-01-05 | 2008-10-15 | Sterecycle Ltd | Process and apparatus for waste treatment |
SG146539A1 (en) * | 2007-03-09 | 2008-10-30 | Hitachi Plant Technologies Ltd | Temperature adjustment system and temperature adjustment method of product |
WO2012084406A3 (en) * | 2010-12-22 | 2012-11-22 | Tridelta Hartferrite Gmbh | Device for cooling a pourable or liquid product |
DE102011121543A1 (en) | 2011-10-13 | 2013-04-18 | Man Diesel & Turbo Se | Tube bundle reactor useful for catalytic gas-phase reactions, comprises bundle of reaction tubes, heat carrier-annular flow channel, external pump comprising pump housing, main heat exchanger, second heat carrier-annular return channel |
DE102011084476A1 (en) | 2011-10-13 | 2013-04-18 | Man Diesel & Turbo Se | Tube reactor |
CN103071432A (en) * | 2011-10-13 | 2013-05-01 | 曼柴油机和涡轮机欧洲股份公司 | Tube bundle reactor |
EP2581132A2 (en) | 2011-10-13 | 2013-04-17 | MAN Diesel & Turbo SE | Tube bundle reactor |
ITMI20130857A1 (en) * | 2013-05-27 | 2014-11-28 | Versalis Spa | APPARATUS FOR RECOVERING THE ENTHALPY OF REACTION |
WO2014191309A1 (en) * | 2013-05-27 | 2014-12-04 | Versalis S.P.A. | Apparatus for recovering reaction enthalpy |
WO2014202503A1 (en) * | 2013-06-17 | 2014-12-24 | Basf Se | Method and system for carrying out an exothermic gas phase reaction on a heterogeneous particulate catalyst |
CN105307765A (en) * | 2013-06-17 | 2016-02-03 | 巴斯夫欧洲公司 | Method and system for carrying out an exothermic gas phase reaction on a heterogeneous particulate catalyst |
FR3027663A1 (en) * | 2014-10-27 | 2016-04-29 | Commissariat Energie Atomique | EXCHANGER REACTOR COMPRISING MEANS FOR MODIFYING THE DISTRIBUTION OF A HEAT TRANSFER FLUID |
WO2016066560A1 (en) * | 2014-10-27 | 2016-05-06 | Commissariat à l'énergie atomique et aux énergies alternatives | Exchanger reactor including means for modifying the distribution of heat-transfer fluid |
WO2020247158A1 (en) * | 2019-06-03 | 2020-12-10 | John Bean Technologies Corporation | Fluid retort installation and methods for circulating process fluid |
US11582991B2 (en) | 2019-06-03 | 2023-02-21 | John Bean Technologies Corporation | Retort system |
Also Published As
Publication number | Publication date |
---|---|
CN1708350A (en) | 2005-12-14 |
AU2002358695A1 (en) | 2004-06-30 |
EP1569744A1 (en) | 2005-09-07 |
JP2006508794A (en) | 2006-03-16 |
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