RU148799U1 - HEAT EXCHANGE REACTOR - Google Patents

Abstract

1. A heat exchange reactor (100) for carrying out endothermic or exothermic reactions, including: - a casing (101), - wherein said casing defines the wall of the reactor (102), - a plurality of heat transfer tubes (103), placed inside the aforementioned casing for supply heat to the catalyst layers (104) located inside or outside the above heat transfer tubes or to remove heat from the above layers, the first tube head (105) located in the upper part of the housing to support the upper part of the heat transfer tubes, the second pipe the first head (106) located in the lower part of the housing to support the lower part of the heat transfer tubes is at least a first fluid chamber (107), a second fluid chamber (108) and a third fluid chamber (109) located inside the aforementioned housing, wherein the aforementioned first fluid chamber is located in the upper part of the housing above the first tube head, the second fluid chamber is located in the middle section of the housing between the first and second tube heads, and the third fluid chamber p located in the lower part of the housing under the second pipe head, at least four fluid holes in the above housing: at least one fluid hole (110) in the first fluid chamber, at least two fluid holes ( 111, 112) in the second fluid chamber and at least one fluid hole (113) in the third fluid chamber, the first and second tube heads have channels for each of the heat transfer tubes, in which the lower part of each heat transfer tube is supported

Description

The present technical solution relates to a heat exchange reactor for carrying out endothermic or exothermic catalytic reactions. In particular, the present technical solution relates to a heat exchange reactor with improved fluid seal suitable for high temperature reactions. A heat exchange reactor may form part of large equipment, such as manufacturing equipment.

Catalytic reactors for carrying out endothermic or exothermic reactions are well known in the art, with specific examples being reactors for endothermic steam reforming of hydrocarbons and reactors for exothermic reactions of methanol synthesis (without limiting the scope of these reactions). The reactions are usually carried out in tubes loaded with a suitable solid catalyst through which the process gas stream containing the reactants will pass at elevated pressure. A number of tubes are arranged vertically or horizontally in the reactor. The tubes run parallel along the main axis of the catalytic reactor, while the heat exchange medium outside the tubes heats or cools them. The solid catalyst inside the tubes forms a catalyst bed in which the required chemical reactions take place. The catalyst can be supplied in the form of solid particles or a coated structure, for example, in the form of a thin layer fixed on the inner wall of the tubes in steam reforming reactors.

In another configuration of the reactor, including a number of tubes, particles of solid catalyst can be located outside the tubes, hereinafter also referred to as heat transfer tubes, while the heat transfer medium passes inside. A solid catalyst outside the heat exchange tubes forms a catalyst bed in which the required chemical reactions take place.

Further types of heat exchange tubes and heat exchange reactors are also known in the art. In the future, the technical solution will be explained with reference to heat exchange reactors and heat transfer tubes with catalysts located inside the tubes, as well as to cases in which the tubes and the reactor are located mainly vertically. However, the utility model is not limited to these types of tubes and reactors. The terms “catalytic reactor”, “heat exchange reactor” and “reactor” are used interchangeably. By “catalyst bed” is meant the volume of the solid catalyst forming the above layer and located inside the heat exchange tubes. The terms “heat transfer tubes” and “tubes” are used interchangeably and encompass tubes that are in contact with the catalyst, as well as with the heat transfer medium, for carrying out catalytic reactions.

A process and a reactor in which the catalyst is in indirect contact with a heat exchange medium are known from EP 0271299. This reference describes a reactor and a process that combine steam reforming and autothermal reforming. The steam reforming zone formed at the bottom of the reactor includes a series of tubes with a catalyst located inside, while at the top of the reactor, an autothermal reforming catalyst is located outside of the steam reforming tubes. EP-A-1106570 describes a process for steam reforming in parallel-connected tubular reforming reactors, including a series of steam reforming tubes and heated by indirect heat transfer. The catalyst is located in one reactor outside the steam reforming tubes and inside the steam reforming tubes in another reactor.

WO 0156690 describes a heat exchange reactor including an outer shell equipped with nozzles for inlet and outlet of process gas, a number of reactor tubes supported at their upper ends, manifold equipment for supplying process gas from the inlet of the above manifold to the upper ends of the reactor tubes wherein the above collector equipment includes two or more primary input collectors located across the upper part of the above shell glasses, each primary input collector has a depth exceeding its width, so that the above tubes are supported directly or indirectly with respect to the shell by the above primary input collectors.

EP 1048343 A describes a heat exchanger type reactor that includes a number of tubes containing a catalyst, a sheath section through which a heat exchange medium is passed to effect heat transfer with the reaction medium in the above tubes, and upper and lower tube sheets; wherein the upper ends of the above tubes are attached to the above upper tube sheet by means of first expansion joints attached to the upper side of the above upper tube sheet, the lower ends of the above pipes are attached directly to the floating lower tube sheet; a floating space is formed, which is divided by the aforementioned lower tube sheet and the inner end plate (inner head) attached to its lower side, and has an opening in the lower part; wherein the aforementioned hole is connected by means of a second expansion joint to the outlet of the reactor from the side of the pipes.

In accordance with the conditions of the catalytic reaction process, the heat exchange reactor must have a structure capable of absorbing differential thermal expansion between the tubes and the casing due to the temperature difference between them. In addition, this design should be able to absorb differential thermal expansion between the tubes, which is caused by the temperature difference between the tubes, created by the difference in the reaction conditions and heat transfer between the tubes; the difference due to the tolerance of the inner diameter of the tubes in the reactor, the difference in the packing density of the catalyst in each tube, due to the tolerance of the inner diameter of the tubes in the reactor, the difference in the activity of the catalyst, the uneven distribution of the reaction gas flowing through the tubes, the uneven distribution of the heat transfer medium flowing through the shell section and etc.

Conventional heat exchange reactors with tubes and tube heads fixed to tube heads attached to the reactor vessel cannot meet these requirements because they cannot handle differential thermal expansion between the vessel and tubes or between tubes. In patent EP 1048343, thermal expansion can be absorbed by the first expansion joints for each tube and the second expansion joint in connection with the floating lower head of the tubes. Thus, the solution to expansion problems described in patent EP 1048343 requires that both the first and second expansion joints have sufficient strength to withstand the load from the weight of the tubes, catalysts and the lower tube head, as well as the pressure difference between the side of the tubes and side of the shell. Further, the second expansion joint described in patent EP 1048343, it is desirable to isolate from the reaction fluid or heat transfer fluid, if they have temperatures, for example, 500 ° C or higher, since the provision of gas-tight joints for such high temperatures is problematic. Another solution is to take a light gas leak at the expansion joint by providing, for example, a labyrinth seal. However, this is not acceptable for all applications.

The purpose of this technical solution is to provide a heat exchange reactor that allows to solve the above problems, in particular, problems with expansion. A further objective is to provide an improved heat exchange reactor that is capable of operating at high temperatures, but would still have gas-tight seals between the tubes and tube heads.

Utility Model Features

1. A heat exchange reactor (100) for carrying out endothermic or exothermic reactions, including:

- housing (101),

- while the above body determines the wall of the reactor (102),

- a plurality of heat transfer tubes (103) located inside the aforementioned housing for supplying heat to the catalyst layers (104) located inside or outside the above heat transfer tubes, or for removing heat from the above layers,

- the first tube head (105) located in the upper part of the housing to support the upper part of the heat transfer tubes,

- a second tube head (106) located in the lower part of the housing to support the lower part of the heat transfer tubes,

- at least a first fluid chamber (107), a second fluid chamber (108) and a third fluid chamber (109) located inside the aforementioned housing, wherein the aforementioned first fluid chamber is located in an upper part of the housing above the first tube head, the second fluid chamber is located in the middle section of the housing between the first and second tube heads, and the third fluid chamber is located in the lower part of the housing under the second tube head,

at least four fluid openings in the aforementioned housing: at least one fluid opening (110) in the first fluid chamber, at least two fluid openings (111, 112) in the second fluid chamber and at least one fluid hole (113) in the third fluid chamber,

the first and second tube heads have channels for each of the heat transfer tubes, in which the lower part of each heat transfer tube is supported in a fixed state both laterally and in the upper direction by the second tube head, and the upper part of each heat transfer tube is maintained in the movable state of the first the tube head, whereby the second tube head receives a load from the plurality of heat exchange tubes and prevents them from shifting with respect to the second tube head, and the first tube head supports a plurality of heat transfer tubes in the lateral direction, which allows the heat transfer tubes to move up and down with respect to the first tube head, and the sliding support of the upper part of the heat transfer tubes includes a fluid tight seal (118).

2. A heat exchange reactor according to feature 1, in which the aforementioned lower part of the heat transfer tubes includes a restriction (114), due to which the cross-sectional area of the lower end of the heat transfer tubes and the cross-sectional area of each channel in the second tube head is smaller than the cross-sectional area of the heat transfer tubes over the narrowing.

3. A heat transfer reactor according to feature 2, wherein the catalyst layers are located inside the heat transfer tubes, and each of the above heat transfer tubes includes a support (115) located at the bottom of each of the heat transfer tubes above the restriction to support the catalyst layers.

4. A heat exchange reactor according to feature 3, further comprising a spacer ring (116) located between the constriction and the support, for adjusting the height of the support.

5. The heat exchange reactor according to feature 4, in which the aforementioned support and the aforementioned spacer ring comprise one single unit.

6. A heat exchange reactor according to any one of the preceding features, in which at least one of the first and second tube heads has a concave shape.

7. A heat exchange reactor according to any one of the preceding features, in which the second tube head is ellipsoidal in shape, whereby the load of the heat exchange tubes is distributed at the edge of the above second tube head.

8. A heat exchange reactor according to any one of the preceding features, in which at least one of the first and second pipe heads has insulation (117) on at least one side of the pipe head.

9. A heat exchange reactor according to feature 8, in which the insulation (117) is located on the side of at least one of the first and second tube heads, which faces the second fluid chamber, and the thickness of the insulation is selected so that the insulation is substantially flat a surface on the side that faces the second fluid chamber.

10. The heat exchange reactor according to any one of the features of 8-9, wherein the portion of each of the heat exchange tubes, which is located in the second fluid chamber between the first and second tube heads and the insulation, is substantially equal in length.

11. A heat exchange reactor according to any one of the preceding features, in which the aforementioned seal includes, for each heat transfer tube, a stuffing box (119) with a bundle packing (120) that is compressed around the heat transfer tube by a compression tool (121).

12. A heat exchange reactor according to any one of the preceding features, in which at least one of the heat transfer tubes is equipped with fastening means (122, 130) in the upper part, which makes it possible to lift at least all the heat transfer tubes and the second tube head.

13. A heat exchange reactor to any of the preceding features, in which the aforementioned wall of the reactor forms at least a first tubular section (124) in the upper part of the second fluid chamber, a second tubular section (125) in the middle of the second fluid chamber, and a third a tubular section (126) in the lower part of the second fluid chamber, wherein the aforementioned first and third tubular sections have a larger diameter than the second tubular section, which allows at least two annular chambers to evenly distribute fluid to at least two fluid openings in the second fluid chamber and from the two openings, as well as to the lower and upper parts of the surface of the heat transfer tubes and from these parts.

14. A heat exchange reactor according to any one of the preceding features, further comprising a liner (127) arranged around the heat exchanger tubes in the second fluid chamber, wherein said liner has perforations (129) for uniformly distributing the fluid to at least two openings for the fluid in the second fluid chamber and from the two openings, as well as to the lower and upper parts of the surface of the heat transfer tubes and from these parts.

15. A heat exchange reactor according to feature 14, wherein at least a portion of the area of the above cladding facing at least one of the at least two fluid openings in the second fluid chamber does not have these perforations, resulting in the above area can act as a fluid chipper.

In implementing this utility model, a heat exchange reactor for conducting an endothermic or exothermic reaction includes a vessel with a reactor wall, heat transfer tubes, tube heads, fluid chambers, and fluid openings. The casing and heat transfer tubes are located mainly in an upright position, which is favorable for ensuring the structural strength of the components, especially when operating at elevated temperature and elevated pressure. The reactor is divided by tube heads into at least three fluid chambers. In the first fluid chamber located in the upper part of the housing above the first tube head, the first fluid is passed inwardly through the fluid opening and distributed to the heat exchange tubes. The first fluid flows inside the tubes down into the third fluid chamber located in the lower part of the housing under the second tube head, where the flow from each tube is collected and discharged from the fluid opening. In the second fluid chamber located in the middle section of the reactor vessel, the second fluid is passed inward through one fluid hole located in the lower part of the middle section. The second fluid flows upward in the middle section, while exchanging heat with the first fluid through the walls of the heat exchange tubes. In the upper part of the middle section, a second fluid is discharged through another fluid opening. The catalyst beds may be placed inside the tubes or outside the tubes in a second fluid chamber. Heat transfer tubes are supported by two tube heads. The tubes are supported to slide in the channels in the first upper tube head, therefore, while the upper part of each tube is supported and fixed with the inability to move in horizontal directions, they can freely move in vertical directions, independently of each other. A feature of this utility model is that the tubes are fixed in the second lower tube head and cannot move in any direction with respect to the second tube head. The lower part of each tube is attached to the second tube head at the location of the corresponding channel in the above tube head; however, it can be fixed with the lower end of each tube, located directly above the corresponding channel; with the end of the tube inside the channel, or with the end of the tube inside the channel, and the end of the tube under the tube head. The attachment of the tube to the second tube head can be carried out in any known manner, such as, for example, welding, which is preferred because it provides gas impermeability. It is important that the fixing method withstands operating temperatures. It is understood that since the tubes are slidably attached to the first tube head only in vertical directions, it is the second tube head that receives the load from a plurality of heat exchange tubes.

The first fluid may flow from top to bottom: through the fluid hole in the first fluid chamber, it flows from the first fluid chamber through heat exchange tubes to the third fluid chamber and out through the fluid hole; or, in another embodiment, it may flow in the opposite direction. In one embodiment, the second fluid may flow upward from the fluid hole at the bottom of the second fluid chamber, upwardly through the second fluid chamber around the tubes and out of the second fluid chamber through the fluid port into the top of the second fluid chamber. In an embodiment where the first fluid flows down, the second fluid flows up, the catalyst bed is placed inside the heat exchanger tubes, and the reaction is endothermic, the second fluid must transfer heat to the first fluid. Therefore, it is preferable to attach the pipes, for example, by welding, to the second pipe head, where the temperature is the highest.

In one embodiment of the utility model, the heat transfer tubes have a narrowing in their lower part, so that the outer and inner diameters of the tubes are reduced. Accordingly, the lower end part of the tubes, which is attached to the second tube head, requires a corresponding channel in the second tube head, which would be sufficient only to correspond to a reduced diameter of the tubes, which, in turn, increases the strength of the second tube head in comparison with a pipe head perforated with larger diameter channels.

In a further embodiment, in which the catalyst layers are located inside the heat exchange tubes, the support for the catalyst layer is located inside the tubes in the lower part of the tubes above the restriction. The support may be of any suitable design, for example a wire mesh at the top of the support mesh supported by the support ring. The narrowing serves as a lower stop for supporting the catalyst, and a distance ring can be placed between the narrowing and the supporting of the catalyst to adjust the height of the catalyst layer in each tube. The support and the spacer ring can also be combined into one single unit, the height of which can subsequently be changed to adjust the height of the catalyst layer in each tube, as described above.

In yet another further embodiment, at least one of the two tube heads — the first or second — is concave. The concave shape, for example, ellipsoidal, is especially favorable for the second tube head, which receives the load from the heat exchange tubes and the catalyst layer, since it transfers the load from the central part of the tube head outward to the periphery of the tube head, where the tube head can be supported by the reactor wall. The distance rings used to adjust the height of the catalyst supports in each tube can be adapted to compensate for the concave shape of the second tube head, so that the bottom of the catalyst layer in each tube has the same height in the reactor. This is beneficial when uniform catalytic activity in all tubes is desired.

In one embodiment, at least one of the two tube heads — the first or second — is isolated from the side surface of the tube head facing the second fluid chamber. In cases where the temperature in the second fluid chamber is higher than the temperature in the first and third fluid chambers and inside the tubes, the insulation protects the insulated tube head from high temperatures, and the thickness of the tube head can thus be reduced to meet the specified requirements strength. This is especially favorable for a second pipe head bearing a load. Further, the thickness of the insulation can be, like the height of the catalyst support, adapted to compensate for this concave shape of the first and / or second pipe head, whereby the insulation surface is substantially flat and the length of the tubes between opposite insulation surfaces or between the insulation surface and the opposite pipe head can be basically the same for all handsets. In a further embodiment, the upper and lower parts of the catalyst layers in each heat transfer tube are located at the same or almost the same height as the insulation surface.

In one embodiment, the top of each heat transfer tube has a seal on the top of the tube head. The seal provides lateral support for the tubes in the channels of the tube head and a substantially fluid tight connection, but allows the tubes in the channels to perform the sliding movement described above with respect to the first tube head. In one embodiment, the seal includes a stuffing box for each tube. A stuffing box can be attached (for example, by welding or other known means) to the first tube head around each channel. The seal may be a ceramic bundle packing that is compressed between the packing gland and the outer wall of each tube around the tube by means of a nut or any other known compression means. The stuffing box may further include locking means, such as a locking bolt, to prevent the compression means from slipping.

A particular advantage of the claimed technical solution is that in an embodiment where a relatively hot fluid enters the second fluid chamber through a hole for the fluid in the lower part of the second fluid chamber, and a relatively cold fluid (which should be heated relatively hot fluid) flows through heat transfer tubes, the seal located in the stuffing box in the first fluid chamber is exposed to temperatures significantly greater e lower than the highest temperature is relatively hot fluid. This means that a substantially fluid tight seal can be achieved even for processes in which the hottest inlet gas has a temperature well above the maximum allowed for a given sealant.

In a further embodiment, at least one of the heat exchange tubes is equipped with fastening means at the top of the tubes. This makes it possible to install mechanical stops that prevent the heat exchanger tubes from slipping out of the first tube head when it is installed, for example, in lifting eyes attached to the first tube head. The fastening means may be any of the known, such as threads, channels passing through the tube, snap locks, teeth, couplings, fittings, connectors, or means similar to them; they can be mounted on the outer or inner surface of the tubes, or simultaneously on the outer and inner surface of the tube. The fastening means provide easy installation of heat exchange tubes and tube heads in the reactor: A series of mechanical stops capable of supporting the full weight of the tubes and tube heads is mounted on the fastening means in the upper part of the corresponding row of tubes, where, after all, all tubes, as well as the first and second the pipe head can rise. After mounting the tube head and the tubes themselves in the reactor, the mechanical stops are removed.

In one embodiment, two annular fluid distribution chambers are provided associated with two fluid openings in a second fluid chamber. The annular chambers provide a uniform distribution of fluid from the fluid inlet to the area surrounding all heat transfer tubes close to one end, and a uniform distribution of the fluid from the area surrounding all heat transfer tubes close to the other end, to the fluid outlet. The above annular chambers are designed in the form of sections of the wall of the reactor around the second fluid chamber with an increased diameter, which allows fluid to flow around the tube bundle. These sections of the enlarged diameter reactor wall are located in the upper and lower parts of the second fluid chamber; the middle part of the fluid chamber has a reactor wall diameter that is only slightly larger than the outer diameter of the tube bundle, thereby reducing material consumption. In one embodiment, the fluid inlet to the second fluid chamber is located at the bottom of the second fluid chamber, and the fluid outlet from the second fluid chamber is at the top of the second fluid chamber. The uniform distribution of the fluid in the second fluid chamber around all the heat transfer tubes, as well as the uniform distribution of the catalyst layers along the same lengths of the heat transfer tubes, as described above, provide all conditions for a uniform reaction level and uniform heat transfer between the fluid inside the heat transfer tubes, and fluid outside these tubes.

In one embodiment, the uniform distribution of fluid around all the heat transfer tubes is further provided by a liner located inside the wall of the reactor in the second fluid chamber and surrounding all heat transfer tubes (tube bundle). At least in some areas of the annular chambers, the aforementioned cladding has openings distributed around the cladding, which would otherwise be in the form of a sheet containing a tube bundle. Through the through holes in the liner at the portion of the annular fluid inlet chamber, the fluid in the second fluid chamber flows from the fluid inlet to the corresponding annular chamber and into the space surrounding the heat exchange tubes near one end of the tubes. Similarly, through the openings in the liner in the portion of the annular fluid exit chamber, fluid in the second fluid chamber flows from the space surrounding the heat exchange tubes near the other end of the tubes, through the openings in the liner in the portion of the annular fluid exit chamber, to the corresponding annular chamber and out through the fluid outlet of the second fluid chamber. The liner may be hermetically attached to the wall of the reactor to prevent a fluid path between the tube bundle and the reactor wall, since the fluid passing between the reactor wall and the tube bundle from the inlet of the second fluid chamber to the outlet of the second fluid chamber would reduce the efficiency heat transfer.

In a further embodiment, the openings in the aforementioned cladding are evenly distributed around the circumference at each end of the cladding, with the exception of sections of the cladding directly facing the fluid openings of the second fluid chamber. In these areas, at least part of the lining has no openings, as a result of which this part of the lining acts as a fluid chipper, which further ensures uniform distribution of the fluid around the heat transfer tubes.

As is well known in the art, the tube bundle may be equipped with baffles, for example, disk or toroidal type, to further improve heat transfer between the fluid outside the tubes and the fluid inside them.

The present technical solution will be discussed in more detail with reference to some embodiments, as shown in the drawings, in which:

FIG. 1 is a longitudinal section of one embodiment of a heat exchange reactor,

FIG. 2 is a cross section of a fluid inlet and outlet of a second fluid chamber,

FIG. 3 is a longitudinal section of a heat exchange reactor before assembly,

FIG. 4 is a detailed view of an insulated first tube head,

FIG. 5 is a detailed view of an insulated second tube head,

FIG. 6 is a detailed image of the cladding and the first pipe head with partitions and connecting rods,

FIG. 7 is a detailed view of the bottom of a heat transfer tube,

FIG. 8 is a detailed view of an embodiment of a stuffing box at the top of a heat transfer tube,

FIG. 9 is a detailed view of an upper portion of a tube including attachment means,

FIG. 10 is a detailed view of an insulated second tube head and a third fluid chamber,

FIG. 11 is a detailed view of sections of a heat transfer tube.

FIG. 12 is a detailed view of an embodiment of a stuffing box.

Item Number Overview

100. heat exchange reactor

101. building

102. reactor wall

103. heat transfer tubes

104. catalyst layer

105. first pipe head

106. second tube head

107. first fluid chamber

108. second fluid chamber

109. third fluid chamber

110. hole for the fluid, the first chamber for the fluid

111. a hole for the fluid, the upper part of the second chamber for the fluid

112. hole for the fluid, the lower part of the second chamber for the fluid

113. fluid hole, third fluid chamber

114. narrowing

115. support grid

116. distance ring

117. isolation

118. seal

119. stuffing box

120. harness packing

121. compression tool

121a. fixative

122. fastening means (thread)

123. lifting eyes

124. first upper tubular section of the wall of the reactor

125. second middle tubular section of the wall of the reactor

126. third lower tubular section of the wall of the reactor

127. facing

128. partition

129. perforation cladding

130. locknut

It should be understood that the following are only some specific embodiments. One of the advantages of the claimed technical solution is that it is scalable, therefore, other sizes and quantities of tubes are included in the scope of this utility model.

HTER, as shown in FIG. 1, is a tubular reforming heat exchange reactor. It is a heat exchange reactor 100, which includes a housing 101 with the walls of the reactor 102 and with a catalyst 104 inside the heat exchange tubes 103. It has two separate streams; process gas (TG), which flows from the side of the tubes (inside the tubes) and off-gas (exhaust), which flows from the side of the shell (outside the tubes). There are 1300 handsets. In this embodiment, the catalytic reaction is an endothermic reaction. Therefore, the process gas inside the tubes requires heat transferred from the exhaust gas from the side of the tube sheath.

Process gas flow

A relatively cold process gas (cold with respect to the off-gas) enters the first fluid chamber 107 at the very top of the reactor through the fluid hole 110 in the first fluid chamber and is distributed through the first pipe head 105 to the heat transfer tubes. TG flows through tubes filled with catalyst, and the reforming reaction occurs when heat is received from the shell. The TG leaves the tube through the second tube head 106, flows to the third chamber for the fluid 109 and exits through the hole for the fluid 113.

Flue gas flow

Relatively hot exhaust gas (hot with respect to the process gas) enters the second fluid chamber 108 from the tube sheath side through the fluid hole 112 at the bottom of the second fluid chamber. The stream is passed along the tubes through a system of partitions, supplying heat for the reaction inside the tubes. The exhaust gas exits through a fluid opening 111 at the top of the second fluid chamber. The baffles 128 are configured as disks and toroids, and result in a significant degree of cross-flow after the tubes. The exhaust gas is distributed to / from the tube bundle by means of an annular chamber in the first upper tubular section of the wall of the reactor 124 and the third lower tubular section of the wall of the reactor 126 and lining 127, giving the desired radial entry into the tube bundle and the radial exit from the tube bundle, as can be seen in Fig. 2. When the exhaust gas enters the reactor, it is distributed around the circumference in an annular chamber around the lining. Then the exhaust gas flows through perforations 129 made in the lining. There are fewer perforations in the nozzle position. Thus, the cladding acts as a chipper. The lining, which extends from the lower to the upper part of the reactor, is also perforated in the upper part to obtain a radial flow when the exhaust gas leaves the partition system. The liner is welded to the wall of the reactor 102 to prevent exhaust gas bypass. In the second middle tubular section of the wall of the reactor 125, the lining is located near the tube bundle, since no medium tends to bypass in this section.

A reactor shell including a liner and tube bundle is shown in FIG. 3 separately, as it is visible before the beam is mounted inside the reactor. A load of 1300 tubes is perceived by an ellipsoidal tube head at the bottom of the reactor. The tube head has an insulation 117 located above the tube head, so that the temperature of the tube head corresponds to the temperature of the process gas exiting the tubes. The load from the upper ellipsoidal tube head, partitions and connecting rods takes on the upper flange of the shell. The upper tube head is insulated under the head, which gives it temperatures corresponding to the inlet temperatures of the TG. The load from the cladding is absorbed by the shell at the conical joint.

Thermal expansion

The tubes are attached to the lower tube head. Thermal extensions of the tubes are absorbed by one mechanism — a stuffing box 119 on each tube at the top of the tube head. This allows for individual differences in tube elongation, as shown in FIG. 4. The partition system hangs from the upper pipe head using connecting rods and moves down when heated.

The lining is welded to the shell. The two ends of the cladding will expand from this point up and down, respectively.

Upper Tube Head Layout

The upper tube head has a series of eyelets 123 for lifting when performing beam mounting. Bottom of the head is insulated with fibrous ceramic material, which is held in place by the cladding plate. The tube head is perforated for 1300 tubes. Each perforation has a stuffing box assembly over the head.

The layout of the lower tube head

The head is insulated from above by a fibrous ceramic material that is held in place by the cladding metal plate, see FIG. 5.

Laying of cladding and partitions

The lining is welded to the cone on the shell. It is perforated above and below.

Partitions are held in place by connecting rods. Connecting rods are attached to the upper tube head, as can be seen in FIG. 6.

Tube layout

The tubes have different lengths due to ellipsoidal tube heads.

At the top of some tubes, there is a fastener 122, such as a threaded section. It is used to install the lock nuts 130 when lifting the beam by the lifting eyes.

Wire mesh.

As seen in FIG. 7, the catalyst rests on the support lattice 115. The distance rings 116, such as thin-walled cylindrical tubes, hold the catalyst support lattice at the correct height. The diameter of the tubes decreases at a restriction of 114 at the bottom of the tubes. This is done to obtain a larger bundle and, therefore, a thinner tube head. In FIG. 11 shows another embodiment in which there is no need for a spacer ring due to a change in the length of the lower part of the heat exchange tubes with a reduced diameter, and also because instead of narrowing, the diameter of the lower part of the tubes is reduced by flanging.

Stuffing box layout

1300 packing glands 119 are a stuffing box in which a seal 118 is located including a pack of packing 120. As can be seen in FIG. 8, there are compression means 121, such as an oil seal ring, which works like a hollow bolt that rotates around the tube when the packing harnesses are compressed. Between the harnesses and the stuffing box ring there is a follower ring that protects the harness packing from friction when tightening the stuffing box. The stuffing box assembly is welded to the tube head from the inside. A further implementation of the stuffing box is shown in FIG. 12. Here, the compression ring of the stuffing box is fixed by another ring, 121a.

On-site assembly

To assemble the tube bundle in the shell, it is necessary to use lifting eyes at the top of the tube head for lifting. The lower pipe head is lifted by tubes that are held in place by a lock nut at the upper head. FIG. 9: The stuffing box is shown with lock nut 130 (top left). Lock nuts act as connecting elements between the upper pipe head to which the valve is attached and the pipes and lower pipe head. When the beam is in place, a sealed weld is made between the lower tube head and the sheath joint.

Fig. 10: Final assembly steps for the bottom of the reactor. The beam is lowered, after which the ellipsoidal tube head and the connection to the shell are hermetically sealed.

Example

Cold process gas with a temperature of ~ 410 ° C enters the very top of the reactor and is distributed to the tubes. TG flows through tubes filled with catalyst, and the reforming reaction occurs when heat is received from the shell. TG leaves the tube at a temperature of ~ 750 ° C and exits through the lower outlet.

Hot flue gas with a temperature of ~ 1005 ° C enters from the shell through the lower nozzle. The flow is passed through the tubes in the partition system, supplying heat for the reaction inside the tube. Exhaust gas leaves through the upper nozzle from the shell side at a temperature of ~ 600 ° C.

The upper head has an inner diameter of 4250 mm, a thickness of 85 mm and is made of SA-387 alloy, grade 22, class 2. The head is insulated from below with a fibrous ceramic material that is held in place by a 3 mm thick cladding plate made of inconel 693.

The lower head has a thickness of 50 mm and an inner diameter of 3600 mm. The head is made of Inconel 625 or Haines 230. The head is insulated from above with a fibrous ceramic material that is held in place by a 3 mm thick cladding plate made of Inconel 693.

Facing, partitions and connecting rods are made of Inconel 693.

The tubes have a length of approx. 11 meters, inner diameter 50 mm and outer diameter 60 mm. All parts of the tube layout are made of Inconel 693.

Claims (15)

1. A heat exchange reactor (100) for carrying out endothermic or exothermic reactions, including: - housing (101), - while this body determines the wall of the reactor (102), - a plurality of heat transfer tubes (103) located inside the aforementioned housing for supplying heat to the catalyst beds (104) located inside or outside the above heat transfer tubes or for removing heat from the above layers, - the first tube head (105) located in the upper part of the housing to support the upper part of the heat transfer tubes, - a second tube head (106) located in the lower part of the housing to support the lower part of the heat transfer tubes, - at least a first fluid chamber (107), a second fluid chamber (108) and a third fluid chamber (109) located inside the aforementioned housing, wherein the aforementioned first fluid chamber is located in an upper part of the housing above the first tube head, the second fluid chamber is located in the middle section of the housing between the first and second tube heads, and the third fluid chamber is located in the lower part of the housing under the second tube head, at least four fluid openings in the aforementioned housing: at least one fluid opening (110) in the first fluid chamber, at least two fluid openings (111, 112) in the second fluid chamber and at least one fluid hole (113) in the third fluid chamber, the first and second tube heads have channels for each of the heat transfer tubes, in which the lower part of each heat transfer tube is held in a fixed state both in the lateral and in the upper m direction by the second tube head, and the upper part of each heat exchanger tube is kept movable by the first tube head, whereby the second tube head receives a load from the plurality of heat transfer tubes and prevents them from displacing with respect to the second tube head, and the first tube head supports the plurality of heat transfer tubes in the lateral direction, which allows the heat exchange tubes to move up and down with respect to the first tube head, and the sliding support of the upper part of the heat ennyh tubes includes a tight seal for the fluid (118). 2. The heat exchange reactor according to claim 1, wherein said lower part of the heat exchange tubes includes a restriction (114), due to which the cross-sectional area of the lower end of the heat transfer tubes and the cross-sectional area of each channel in the second tube head is smaller than the cross-sectional area of the heat exchange tubes over the narrowing. 3. The heat transfer reactor according to claim 2, wherein the catalyst layers are located inside the heat transfer tubes, and each of the above heat transfer tubes includes a support (115) located at the bottom of each of the heat transfer tubes above the restriction to support the catalyst layers. 4. The heat exchange reactor according to claim 3, further comprising a spacer ring (116) located between the constriction and the support to control the height of the support. 5. The heat exchange reactor according to claim 4, in which the aforementioned support and the aforementioned spacer ring comprise one single unit. 6. The heat exchange reactor according to claim 1, in which at least one of the first and second tube heads has a concave shape. 7. The heat exchange reactor according to claim 1, wherein the second tube head has an ellipsoidal shape, whereby the load of the heat exchange tubes is distributed along the edge of said second tube head. 8. The heat exchange reactor according to claim 1, in which at least one of the first and second pipe heads has an insulation (117) on at least one side of the pipe head. 9. The heat exchange reactor according to claim 8, in which the insulation (117) is located on the side of at least one of the first and second pipe heads, which faces the second fluid chamber, and the thickness of the insulation is selected so that the insulation has mainly a flat surface on the side that faces the second fluid chamber. 10. The heat exchange reactor according to any one of paragraphs. 8 and 9, in which a portion of each of the heat transfer tubes, which is located in the second fluid chamber between the first and second tube heads and the insulation, is substantially equal in length. 11. The heat exchange reactor according to claim 1, wherein the aforementioned seal includes, for each heat exchange tube, a stuffing box (119) with a bundle packing (120) that is compressed around the heat exchanger tube by a compression tool (121). 12. The heat transfer reactor according to claim 1, wherein at least one of the heat transfer tubes is equipped with fastening means (122, 130) in the upper part, which allows at least all heat transfer tubes and the second tube head to be lifted. 13. The heat exchange reactor according to claim 1, in which the aforementioned wall of the reactor forms at least a first tubular section (124) located in the upper part of the second fluid chamber, a second tubular section (125) located in the middle of the second fluid chamber medium, and a third tubular section (126) located at the bottom of the second fluid chamber, wherein the above first and third tubular sections have a larger diameter than the second tubular section, which allows at least two annular chambers to be uniform to distribute fluid to at least two holes for the fluid in the second fluid chamber and out of the two holes, as well as to the lower and upper portions of heat exchange tubes and surfaces of these parts. 14. The heat exchange reactor according to claim 1, further comprising a liner (127) placed around the heat exchange tubes in the second fluid chamber, the aforementioned liner having perforations (129) for uniform distribution of the fluid to at least two openings for fluid in the second chamber for the fluid and from these two holes, as well as to the lower and upper parts of the surface of the heat transfer tubes and from these parts. 15. The heat exchange reactor according to claim 14, in which at least part of the area of the above cladding, facing at least one of the at least two openings for the fluid in the second chamber for the fluid, does not have these perforations, resulting in the above the area may act as a fluid chipper.

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