JP4999248B2 - Chemical reactor with heat exchanger - Google Patents

Description

[0001]
Field of Invention
The present invention is applicable to the field of chemical engineering, and particularly relates to the improvement of chemical reactors. The present invention generally relates to control of reactant temperature during endothermic or exothermic reactions. Specifically, the present invention has a "flat" reactant temperature profile at the outlet of the heat exchanger panel, i.e., the reactant outlet temperature in the width direction of the heat exchanger panel is ideally uniform and possible. It relates to a printed circuit reactor (PCR) and a process control method that are as constant as possible.
[0002]
Background of the Invention
Controlling the reaction temperature to an acceptable range has been extensively studied, and several apparatuses have been devised in the chemical industry. Commonly used materials are described in standard reference books and textbooks. General knowledge can be found in, for example, Chapter 19 of “Chemical Reaction Engineering” by Octave LEVENSPIEL (Chemical Reaction Engineering, published by John Wiley & Sons). ) Can be referred to.
[0003]
Some of the prior art is a conventional reactor designed to allow even more control of the reactant temperature, which is called a staged adiabatic packed bed reactor. In the apparatus used in this system, during a number of spaced apart reaction zones, the temperature of the product leaving the first reaction zone is controlled before entering the next reaction zone. Means are provided. In this reaction zone, a heat exchanger for controlling the reaction temperature is not provided. That is, the reactant fluid entering the reactor at the desired temperature passes through a packed bed containing the catalyst. Upon exiting this first stage, the reactant gas and product will be at a temperature above or below the initial temperature, depending on the thermal characteristics of the reaction. Here, the reactant gas is heated or cooled to a second desired temperature by means of a heat exchanger before moving on to the next packed bed, ie the second stage. This procedure is repeated until the desired conversion is achieved. Therefore, the temperature profile of the reaction is stepped within the allowable temperature range and is not truly isothermal.
[0004]
The heat exchanger panel selected for the purposes of the present invention is a stack of plates stacked together and diffusion bonded to form a stack of plates, and fluid passages are defined in the stack by pretreatment of the plates. Each plate is processed into a channel processed surface according to a desired fluid path pattern by performing a process of removing the surface material to a desired depth by a method such as chemical etching or hydraulic mill, or a blank surface. Is selectively configured. Optionally, chemical processing may be enhanced by mechanochemical processing using appropriate tools.
[0005]
Such plate pre-treatment is performed in a manner somewhat similar to printed circuit board (PCB) manufacturing, and in this sense, the design of this heat exchanger is the Printed Circuit Heat Exchanger (PCHE). Can be called. Application of diffusion bonding technology to metal plates is well known in the technical field of metal processing, and is applied for various purposes such as the production of medical prostheses.
This PCHE design has been demonstrated by the proposed PCR designers since 1985 when these small heat exchangers were first introduced.
[0006]
An example of a PCR-type reactor designed by the applicant of the present invention has been filed separately from the present application (see: 32 46271 WO-01 / 54806). Such a reactor is configured to provide at least one reaction zone bounded by a heat exchanger in which a plurality of plates are overlaid and diffusion bonded to form a stack of plates. Are defined in the stack by pretreatment of the plates, and each plate is selectively selected according to the desired channel pattern by processing to a desired depth by a chemical treatment, such as chemical etching, that removes the surface material. It is configured. With the fluid channels defined in such a stack, various channels are provided in the channels arranged for heat exchange with the discrete channels containing at least one auxiliary fluid for controlling the temperature of the reactants. The reactant can be conveyed.
[0007]
In order to maintain reasonable control over the reaction, the reactants at the outlet of the heat exchanger panel have no opportunity to be mixed on a whole scale and go directly into the subsequent adiabatic reaction zone. The temperature profile is preferably flat. If the reactants are partially too hot or too cold, selectivity and conversion processes can also be hindered. This problem is particularly important in the case of a strongly exothermic reaction, because a heat spill can occur when some of the reactants are not sufficiently cooled between reaction stages, The higher the temperature, the higher the reaction rate, which further increases the temperature.
[0008]
The heat transfer medium that carries heat to or from the reactants may be a fluid such as water, steam, molten salt, liquid metal, combustion gas or pressurized closed loop gas. If the reaction is near atmospheric temperature, there appears to be little problem in providing a large amount of heat transfer medium flow, supplying heat to the medium, or extracting heat therefrom. In that case, simply using water, if the reaction is an exothermic reaction, the lower heat that is discarded in the cooling tower, and if the reaction is an endothermic reaction, the lower heat obtained from the exhaust steam. Can be used. Alternatively, boiling water or condensed water can be used at higher temperatures.
[0009]
However, many challenges arise when the temperature is extreme and it is more difficult to supply or extract heat. For example, when water exceeds the critical point, depending on the situation, isothermal heat supply using boiling and condensation cannot be performed, the temperature limit of the structural material approaches, or the molten salt deteriorates.
A typical example is the styrene reaction, which is an endothermic reaction, in which the catalyst layer is ideally maintained near 600 ° C. This means that in PCR, the temperature of the reaction must be reduced to about 580 ° C. in each insulation layer and reheated to about 620 ° C. in each heat exchanger.
[0010]
A suitable heat exchange medium is steam superheated at 750 ° C. The steam outlet temperature from the heat exchanger is ideally designed to minimize the flow rate of the steam, minimize the size of the pipe that carries it, and minimize energy loss due to the fluid. It will approach the temperature.
However, this can cause serious problems. That is, if the heat exchange between the steam flowing in at 750 ° C. and being cooled to the reactant inlet temperature and the reactant flowing in at 580 ° C. is not carefully controlled, the average outlet temperature of the reactant will be the required 620 ° C. Even so, the temperature of the reactants leaving the heat exchanger will fluctuate significantly.
[0011]
This problem is illustrated in FIG. If there is a simple counter-flow contact between the steam and the reactants, it can be seen that the outlet temperature of the reactants is biased to higher temperatures towards the end of the plate where the steam exits.
Moreover, although the average temperature is adjusted to 620 ° C., the fluctuation of the outlet temperature of the reactant in the width direction of the heat exchanger panel is about 580 ° C. to 720 ° C., and has a range of ± 70 ° C. This is fatal to the yield of the reaction.
One object of the present invention is to eliminate or mitigate this type of property problem. In particular, it is an object of the present invention to provide an apparatus that includes a chemical reaction zone and a method for controlling the temperature of reactants that react within the zone.
[0012]
Summary of the Invention
Therefore, the present invention described more specifically here is a reactor of a staged adiabatic reactor type in a broad sense, comprising at least one heat exchanger panel inserted between adiabatic catalyst layers, The surface area and the corresponding superficial facial area of the catalyst are substantially equivalent, and the panel includes means for defining discrete passages for transporting the reactants and heat transfer medium, Means for defining a passage for the heat transfer medium provide the heat transfer medium with at least two different flow paths through the heat exchanger panel, thereby reducing the occurrence of temperature deviations or differences. The reactor.
[0013]
Preferably, the entire heat exchanger panel is a printed circuit heat exchanger type (PCHE), and at least two different plate designs can be used to construct the panel, thereby achieving significant changes in flow path design. Like that. First, the flow direction of the fluid in the PCHE is initially set by the supply and ventilation connections to the inlet and outlet, respectively, of the assembled PCHE plates that make up the panel. However, by changing the “printed circuit” scheme design of the flow path in the plate and providing different PCHE plates in the panel, both the flow path direction and the heat transfer influence can be controlled.
[0014]
Using plates with different designs is a preferred way of gaining design freedom, but in some cases, plates with substantially the same design can be used. In the special case where the same square plates are stacked side by side, each has a unique passage pattern etched on the surface, and the alternating plates are rotated in the plane of the plate. And optionally, if necessary to prevent intermixing of fluids, the passages in different directions are defined by inserting plates with non-etched surfaces (blanks). can do. In this way, continuous flow paths in different directions can be achieved.
[0015]
Plates with appropriate channels defined by etching or the like are stacked and diffusion bonded together to form a heat exchanger panel, and so formed panels are juxtaposed if necessary, It is also possible to provide a larger panel having the desired height and width that are joined, for example by welding, to meet the required cross-sectional area of the catalyst layer. In some cases, it is appropriate to use a blank plate (non-etched plate) to complete the panel and close the open side of the channel formed in the adjacent etched plate. Reference to this panel is for convenience only and is not intended to be a dimensional constraint. However, it can be seen that the dimensions of the heat exchanger unit will vary depending on the reactor design chosen and presently available manufacturing equipment may impose practical constraints on the panel dimensions that can be produced in one step. Will. When it is desirable to form a relatively large panel, such a practical constraint is that multiple panels of dimensions formed within the capability range of the available equipment can be placed side-by-side. It can be solved by joining by a method, for example, welding. In this manner, PCHE panels having various shapes and sizes can be constructed.
[0016]
Also preferably, the plate design allows the flow of the heat transfer medium to pass more than once in both directions along the length of the plate, with passages defined by printed circuit technology. The flow path may be a serpentine path, and optionally may be provided with a noticeable change in the direction of enhancing turbulence in the heat exchange medium flow.
In a preferred embodiment of the invention, the heat transfer medium is housed in a header external to the heat exchange panel and is optionally coupled thereto to allow fluid flow. The arrangement of the header on a panel, preferably a PCHE-type panel, is used to distribute the heat exchange medium in a discrete heat exchange panel passageway, in particular to separate inlets and outlets, at specific positions of the header. A septum may be included, or in an alternative arrangement, a manifold system may be provided, thereby forming openings in opposing plates so that inlet and outlet chambers are created, for example during diffusion bonding prior to panel assembly. Distributes the heat exchange medium to and from ports formed directly in the periphery of the panel.
[0017]
In accordance with one aspect of the present invention, a staged adiabatic reactor type apparatus, defined by at least one surface, comprising means for effecting heat exchange with a fluid passing through a chemical reaction zone to effect a reaction. Said chemical reaction zone, wherein said zone and said surface are at least partially defined by a printed circuit heat exchange (PCHE) panel, said panel allowing discrete flow of fluid reactant and heat transfer medium A mold passage is defined and at least two different flow paths are defined by a PCHE plate design that handles the heat transfer medium so that the heat transfer medium is in at least two different directions relative to the flow of fluid reactants. It is possible to pass through the PCHE panel, which in particular controls the temperature profile of the fluid flowing out of the PCHE panel. Goodness the apparatus is provided.
[0018]
Preferably, the entire means for achieving heat exchange is of the PCHE type as described herein. In such an arrangement, the size of the heat transfer is usually smaller than the size of the catalyst particles, so that the temperature profile specific to heat transfer to the fluid in the passages is not critical to the size of the catalyst particles. Also, the heat transfer dimensions are relatively small compared to the depth of the layers, so that the temperature profile of any passage scale is, for example, only the length of the individual catalyst layers, which are typically up to about 200 mm. Occupies only a small part. This is in sharp contrast to the prior art using, for example, a 25 mm outer diameter exchanger tube, which in this case results in a downstream wake in the temperature profile, which then inevitably becomes discrete. The scale is significantly larger than the catalyst particles of the catalyst layer and extends over at least a significant portion of each catalyst layer.
[0019]
The heat exchange medium is advantageously passed more than once in both directions along the length of the plate.
Also preferably, the passage through which the heat exchange medium includes a serpentine portion comprising a series of short and sharp turns.
[0020]
According to another aspect of the present invention, a method for carrying out a chemical reaction under controlled temperature conditions, preferably in a staged adiabatic reactor, which achieves a reaction between the fluid reactant and the heat exchange means. Continuously distributing through a chemical reaction zone for said zone, said zone being delimited by at least one surface comprising means for achieving heat exchange with said fluid, said surface being Defined at least in part by a printed circuit heat exchanger (PCHE) panel that provides a means for defining discrete passages that allow flow of the heat transfer medium therein, and separate passages of the reactant fluid flow. Enabling introduction of a heat transfer medium into the PCHE panel, and placing the heat transfer medium in at least two directions relative to a flow of fluid reactants in the PCHE panel. It was allowed to pass through, whereby the fluid flowing from the PCHE panel, the method comprising the step of improving the control of the reactant temperature profile is provided.
[0021]
In accordance with the present invention, several variations on the method of temperature control are possible, and this variation is selected according to the operator's choice to think about the chemical reaction system in the field. The main variants of the PCR system that should be considered for temperature control purposes include (a) the direction of flow of the heat exchange medium (HE) relative to the direction of flow of the chemical reactant (CR), essentially There are parallel flow (same main flow direction), cross flow (oblique or cross direction with respect to the axial direction of the CR main flow), counter flow (HE main flow opposite to the CR main flow axis), and (b) the number of passes to one of the other. (HE vs. CR), (c) the direction of HE flow in one PCHE plate exposed to the corresponding plate performing CR and the direction of HE flow in another PCHE exposed to that CR performing plate And (d) the number of different PCHE plate designs incorporated into the PCHE panel. Utilizing two or more heating or cooling fluids in a single panel can be used either in a separate circuit on one plate or in a separate plate.
[0022]
An excellent reactant outlet temperature profile across the heat exchanger is achieved when the HE flow in one PCHE juxtaposed to a plate having fluid transport passages in fluid communication with the CR reaction zone, for example, Complementarily corresponds to the HE flow in another PCHE plate arranged to have a heat transfer relationship with a plate in fluid communication with the CR reaction zone on the opposite side of the first PCHE plate, and generally the HE mainstream path Is a cross flow, that is, a tangent or oblique angle with respect to the CR mainstream path. An example of this is the two-way, three-pass parallel flow shown in FIGS. The arrangements shown in FIGS. 3 and 5 are also less suitable, but acceptable results are obtained with some reaction systems. Examples of systems with poor performance are the systems shown in FIGS.
[0023]
According to another aspect of the present invention, the PCHE plate design essentially follows a meandering path that exhibits a sharp turn in the meandering path, for example by having a zigzag pattern over substantially the entire length of each individual path. It consists of multiple flow passages parallel to. The number of meandering rotations in each path can vary, but at least two rotations are required to provide a return path and an exit path. The use of a zigzag design is an optional feature. In essence, the advantages of a convoluted flow passage arrangement provide fluid path flow lengths that are integer or non-integer multiples of the flow length, heat transfer and pressure drop requirements. It is to improve the compatibility with.
Such a plate is combined with a correspondingly designed complementary plate reflecting this plate, as a pair of plates, between which there is a plate designed to carry the reactant fluid. The Baffles may be provided at both ends of the pair of plates.
The present invention will now be described in more detail with reference to the accompanying drawings, given by way of example only and not by way of limitation.
[0024]
BEST MODE FOR CARRYING OUT THE INVENTION
In accordance with the present invention using a PCHE panel, it is possible to obtain an improved catalytic reactor system, which, as described below with particular reference to the preferred embodiment of FIG. In comparison, the arrangement is such that a substantially flat reactant temperature profile is obtained upon exit from the PCHE.
In this description, for convenience, a design in which the heat transfer medium enters both sides of the PCHE panel is referred to as a “two-way” design, and a design in which the heat exchange medium enters from only one side of the PCHE is referred to as “one-way”.
[0025]
FIG. 6 (bottom) illustrates the arrangement of a PCHE panel 4 comprised of a heat exchange medium, here a plate that receives steam, the plates comprising different designs 1 and 2, each of which is a reactant flow plate. For ease of understanding, the plate is initially shown as in use, and below it is shown separately for clarity of the respective flow paths. On both sides, there is a semi-cylindrical header 20 with a partition wall 21 for separating the steam inlet and outlet at each plate end. Arrows indicate the direction of steam or intended reactant flow.
The plate is provided with serpentine paths 15, 25, allowing steam to pass multiple times across the plate, thereby increasing the flow path length relative to the plate width, Designed to improve heat transfer with reactants passing between them.
[0026]
In use, the fluid reactant to be heated or reheated is introduced into the PCHE panel, where steam enters from the left end of the lower steam plate 2 and exits from the right end and flows through the plate in the direction of the arrow. In the upper plate 1, there is a steam inlet on the right side, which is complementary to the flow in the lower plate, and flows in the left end direction. Since the reaction in the adjacent reaction zone is an endothermic reaction, the flowing reactant fluid enters the PCHE panel and cools the vapor as it passes through the plate 1. The temperature profile of the exiting reactant fluid is substantially symmetrical because the reactant fluid interacts with the heated fluid (vapor) in both directions on both sides of the plate, which is compared to the one-way contact PCHE in FIG. It is preferable.
[0027]
This process is thus improved by passing the vapor "multi-pass" across the reactant path, i.e., passing the vapor back and forth more than once on the same plate. . In the PCHE panel, a complicated channel arrangement can be easily manufactured by a photochemical processing method, and thus it is possible to easily use multiple passes on the plate.
FIG. 6 shows an arrangement in which steam passes through each steam plate three times. The vapor of the upper plate 1 passes twice from right to left and once from left to right, during which time it is reversed in the complementary lower plate 2 so that, as shown in the temperature profile plot, The outlet temperature profile of the reactant in the transverse direction of the PCHE is substantially uniform. Thus, the combined effect of both plates results in a substantially flat and target temperature profile of the reactants as they flow out of the PCHE panel, with temperature fluctuations of negligible ± 1.6 ° C. width.
[0028]
A variation of this arrangement is shown in FIG. 5, in which the steam passes three times on each steam plate. Here, the vapor on the upper plate 11 enters the plate adjacent to the outlet side of the reactant flow plate 13 and passes twice from the left to the right and once from the right to the left to reach the inlet side of the reaction flow plate. Spill adjacent. Similarly, on the lower plate 12, the vapor flow path enters the plate 12 adjacent to the outlet side of the reactant flow plate, passes three times through the plate, and is adjacent to the inlet side of the reactant flow plate 13. leak. Similarly, on the lower plate 12, the steam channel enters the plate adjacent to the outlet side of the reactant flow plate and passes across the plate 12 three times to the inlet side of the reactant flow plate 13. Spill adjacent. Accordingly, as shown in FIG. 5, an outlet temperature profile of the reactant fluid having a symmetrical curve with respect to the transverse direction of the PCHE panel can also be obtained here. However, the multiple passes in this diagonally opposite direction (vs. steam inflow) gave a profile with a temperature range of only ± 5 ° C.
[0029]
A simpler arrangement is shown in FIG. 4, where the steam passes only once on each steam plate. In such a single-pass design, the steam flow is separated by turning the flow of one steam plate 90 degrees at both ends of the plate. In order to keep all the passages the same length, the passages are bent upward at one end and downward at multiple ends.
From the temperature plot in the upper diagram of FIG. 4, it is possible to reduce the temperature range from the inlet to the outlet from ± 70 ° C. (as shown in FIG. 1) to ± 29 ° C. even by such an arrangement. It can be seen that a significant improvement over the arrangement of FIG.
[0030]
FIGS. 8 and 9 show alternative embodiments, each improved in some respect. FIG. 8 shows a port-type plate configuration that allows an opening 7 to be formed in the plate to create an inlet 8 and an outlet 9 within the panel when the plates are diffusion bonded. Yes.
Another improvement is the application of the zigzag passage 10 shown in FIG. 9, which has the advantage of improving heat transfer by introducing turbulence. In addition, the passage may be an integral multiple or a fractional multiple of the plate length, and steam may flow from one end and flow out from the other end, and have the same length.
[0031]
A new adiabatic catalytic bed reactor system (shown in FIG. 10) for carrying out a chemical reaction process comprises a series of catalytic reaction zones 80, which comprise a reactor vessel upper and lower wall 82 and a mesh. It consists of a catalyst packed bed 81 enclosed in a catalytic reaction zone end wall 83 of the form. This mesh acts as a resistance to the catalyst moving from the bed by a large flow of fluid, otherwise this flow will carry the catalyst particles downstream of the catalytic reaction system. Such catalytic reactor zones are arranged in series, and between these reactor zones, the catalyst layer is used for the purpose of adjusting its thermal conditions before the mixed reactant enters the next process stage. A PCHE panel 90 is provided in fluid communication therewith. Each PCHE panel is composed of a plurality of PCHE plates that are appropriately perforated and provided with meandering paths that allow heat exchange in two directions and three times in contact with the reactants to be conditioned. The The PCHE panel is connected to an external steam manifold for suitably supplying or exhausting steam as a heat exchange medium (HE).
[0032]
Although not specifically shown as in FIG. 10, the panel may have a different design, changing the inner diameter of the meander path for HE throughput, or process needs when the reaction develops throughout the catalytic reactor. The surface area of the heat transfer surface may be changed, particularly to adjust for changes required for the catalyst layer.
In use, for example, a reactant for producing styrene (endothermic reaction) is introduced into the first catalyst layer 81, ideally at a temperature of about 600 ° C. or higher, and this catalyst layer is brought to a desired flow rate. Fit and dimensioned to ensure proper overall throughput flow. Depending on the specific heat requirements for the reaction, the reactants and partial product mixture may exit the first catalyst layer below the optimum temperature, for example at about 580 ° C. Thus, the first PCHE panel 90 is a steam that has been superheated to a temperature of about 800 ° C. for the purpose of reheating the partial mixture of reactants and products to about 800 ° C. before entering the next catalyst layer. Designed to accept.
[0033]
Industrial application fields
The PCHE plate design, PCHE panel, PCR catalyst system and method for performing chemical reactions under controlled temperature conditions disclosed in this application are applicable in the field of chemical engineering and are used in a wide range of industrial scale chemical reactions. Although useful, it is also adaptable to small scale, eg small scale, eg small scale laboratories or pilot plant operations.
[Brief description of the drawings]
BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 shows a prior art one-pass counter-flow heat exchange system in a superposed plan view and a disassembled state (also a plan view) for easy identification of discrete flow paths. The upper figure is a graph showing a typical outlet temperature profile in the width direction of the heat exchange system shown in the lower figure.
FIG. 2 is a schematic diagram showing a superposed plan view and a disassembled state (also a plan view) of the improved heat exchange system in order to facilitate identification of discrete flow paths. The upper figure is a graph showing a typical outlet temperature profile in the width direction of the heat exchange system shown in the lower figure.
FIG. 3 shows an overlaid plan view and an exploded view (also a plan view) of an alternative improved heat exchange system in use to facilitate identification of discrete flow paths. It is a schematic diagram and the upper figure is a graph showing a typical outlet temperature profile in the width direction of the heat exchange system shown in the lower figure.
FIG. 4 shows a one-way two-way heat exchange system with a superposed plan view and a disassembled state (also a plan view) in order to make it easy to identify discrete flow paths. The upper figure is a graph showing a typical outlet temperature profile in the width direction of the heat exchange system shown in the lower figure.
FIG. 5 is a schematic diagram showing an overlaid plan view and an exploded view (also a plan view) of the improved heat exchange system in order to facilitate identification of discrete flow paths. The upper figure is a graph showing a typical outlet temperature profile in the width direction of the heat exchange system shown in the lower figure.
FIG. 6 shows a preferred heat exchange system with further improvements in a superposed plan view and a disassembled state (also a plan view) in order to make it easier to identify discrete flow paths. The upper figure is a graph showing a typical outlet temperature profile in the width direction of the heat exchange system shown in the lower figure.
FIG. 7 is a schematic diagram showing, for comparison purposes, different reactant outlet temperature profiles that can be achieved by changing the heat exchange passage flow relative to the reactant flow.
FIG. 8 is a schematic diagram illustrating a preferred arrangement of a plate design that implements inlet and outlet ports at the periphery of the plate.
FIG. 9 shows a preferred heat exchange medium flow path arrangement including two optional characteristics of non-odd total path length using serpentine parallel flow paths and turbulence inducing zigzag changes in discrete flow path directions. It is.
FIG. 10 includes a series of temperature control zones and a series of chemical reactions suitable for use, for example, in a styrene production process, by providing a continuous packed catalyst layer with a continuous heat exchanger (PCHE) panel interposed therebetween. FIG. 2 is a plan view of a preferred printed circuit reactor (PCR) system that provides alternating zones.

Claims (10)

Comprising at least one heat exchanger panel is inserted into the adiabatic catalyst layers, a reactor staged adiabatic reactor type, before Symbol panel is formed as a stack of plates, each plate, a reaction product a plurality of passages for transferring or by at least one passage for transporting the heat transfer medium and image constant, varying the flow path direction of the heat transfer medium you pass the plate for each plate, the The reactor , wherein the occurrence of temperature deviation or temperature difference of the reactants at the outlet of the heat exchanger panel is reduced.   The entire heat exchanger panel is a printed circuit heat exchanger type (PCHE), in which a plurality of plates are stacked and diffusion bonded to form a stack of plates, by pre-treating the plates in the stack The reaction of claim 1 wherein fluid passages are defined and each plate is selectively configured to provide a channeled or blank surface by a process of removing surface material according to a desired fluid passage pattern. vessel. The reactor of claim 2, wherein the panel is constructed using at least two passage patterns . Plates of the same rectangular shape are juxtaposed in a stack, each plate, to sequence the surface thereof on has a unique path patterns etched into, to the respective plate rotating in the stack The reactor of claim 2, wherein the reactor defines passages in different directions. To prevent intermixing of fluids, without the channel on the front surface (the blank) plate was incorporated in the panel, the reactor according to claim 2 or 3. Means for achieving heat exchange with a fluid flowing through the chemical reaction zone to effect a reaction, the chemical reaction zone defined by at least one surface, the zone and the surface comprising: defined by at least partially printed circuit heat exchanger (PCHE) panel, said panel defining a plurality of passages Ru with the flow of fluid reactants and a heat transfer medium, at least two different flow paths, the heat transfer medium defined by PCHE plate design for handling, whereby said heat transfer medium, at least two different directions relative to the flow of fluid reactants, it is possible to pass through the PCHE panel, P CHE This ensures that The reactor of claim 1 having improved control of a reactant temperature profile of fluid exiting the panel.   The reactor according to claim 6, wherein the fluid passage is configured so that the heat transfer medium passes twice or more along the length direction of the plate. Fluid passageway comprises a series of sharp meandering portion, the reactor of claim 7.   The reactor of claim 6, wherein the fluid passage comprises a zigzag pattern imposed on substantially the entire length of each individual passage. Reactor of the staged adiabatic, under controlled temperature conditions provides a method of conducting a chemical reaction,
Continuously allocating a fluid reactant through a chemical reaction zone to achieve a reaction and heat exchange means, the zone comprising means for achieving heat exchange with the fluid One of which is defined by a surface, said surface is at least partially, printed circuit heat exchanger (PCHE comprising a stack of plates to provide a means for defining a plurality of passages flow that enables heat transfer medium therein A) defined by the panel, and further passages providing for the flow of reactant fluid;
Introducing a heat transfer medium into the PCHE panel, and passing the heat transfer medium through the PCHE in at least two different directions relative to a flow of fluid reactants, and fluid exiting the PCHE panel. Improving the control of the reactant temperature profile.

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