CN219209879U

CN219209879U - Tube and shell side heat exchange natural gas steam conversion reactor

Info

Publication number: CN219209879U
Application number: CN202320714225.8U
Authority: CN
Inventors: 晁旭强; 郭朋飞; 盛刚; 张兴; 鲁路; 陈泓远; 陈平生
Original assignee: Shaanxi Rejude Engineering Technology Co ltd
Current assignee: Shaanxi Rejude Engineering Technology Co ltd
Priority date: 2023-04-04
Filing date: 2023-04-04
Publication date: 2023-06-20
Anticipated expiration: 2033-04-04

Abstract

The utility model relates to the technical field of natural gasification, in particular to a tube-shell side heat exchange natural gas steam conversion reactor, which comprises a reactor body and sliding lugs, wherein a conversion device is arranged in the reactor body, and a connecting device is arranged above and below the conversion device. The first-stage conversion gas can enter from the first-stage conversion gas inlet part at the bottom of the reactor body and uniformly enter into the cavity at the lower part of the reactor body, then the conversion raw material gas enters from the raw material gas inlet part at the top of the reactor body, and enters into the sleeve for preheating the raw material gas through the inner seal head part matched with the disc, the fan blade and the like to perform conversion reaction in a uniform distribution manner, the first-stage conversion gas also absorbs heat required by the reaction to perform conversion reaction, the two gases are heated, fully mixed and subjected to uniform temperature during the reaction, and finally the conversion raw material gas exits from the reactor body from the conversion gas outlet part to remove the waste heat boiler of the conversion gas.

Description

Tube and shell side heat exchange natural gas steam conversion reactor

Technical Field

The utility model relates to the technical field of natural gas engineering, in particular to a tube-shell side heat exchange natural gas steam conversion reactor.

Background

Large industrial plants, natural gas steam reforming to produce hydrogen or synthesis gas are relatively economical processes. Along with the large-scale of the device, various process flows are also layered endlessly, such as a single reformer, a pre-reforming and one-stage reformer, one-stage reformer and self-heating reformer, and the like, and the main purposes of the two latter flows are to reduce the load of one-stage reformer as much as possible. The operation temperature of the primary reformer is high, the temperature of the flue gas outlet of the reforming stage is basically above 1000 ℃, the temperature of the flue gas outlet of the reforming stage is above 750 ℃, and the maximum temperature can reach 930 ℃. This high temperature condition is necessary for the natural gas vapor conversion reaction (endothermic reaction). Therefore, the consumption of fuel gas in the primary reformer is relatively high. In the existing general process flow, after the converted gas exits the conversion section, the sensible heat in the converted gas is absorbed by steam generated by a waste heat boiler. For high-temperature flue gas, especially a hydrogen production device, most of sensible heat is absorbed in a steam production mode, and the convection section is huge. The utility model adopts a 'one-stage converter' + heat exchange type conversion process, and utilizes the converted gas converted from 'one-stage converter' (most, about 75-85% of raw material gas) — 'one-stage converted gas' (high temperature) to be mixed with the converted gas of the reactor (small part, about 15-25% of raw material gas), and the heat of conversion reaction (small part of raw material gas) is provided through the wall-to-wall countercurrent heat exchange of the inner wall and the outer wall of the sleeve. After two converted gases (mixed cooling) are discharged from the reaction section, the converted raw material gas (small part of raw material gas) is heated again, so that the raw material gas (small part of raw material gas) reaches the activation temperature of the conversion reaction, and the converted gas is cooled (about 610 ℃) and then enters the waste heat boiler to produce steam. The reactor of the utility model is a pressure vessel, has a compact structure and small equipment size. Meanwhile, the utility model can reduce the size of the primary reformer, reduce the fuel gas consumption of the primary reformer (the fuel gas is saved by 550-600 Nm3 (calculated by natural gas) per 10000Nm3/h of hydrogen produced), greatly improve the equipment investment and the economy of the device operation, and is particularly suitable for hydrogen production devices which do not need too much steam or have been balanced by other economic modes (such as coal-fired boilers).

Disclosure of Invention

The utility model aims to provide a novel natural gas steam reforming reactor which is assisted in a preface 'primary reformer', so that the fuel consumption of a hydrogen production device without too much steam is reduced, the size of the 'primary reformer' is reduced, and the investment economy of the whole hydrogen production device and the economy of the device operation are improved; meanwhile, conversely, the problem of large-scale device can be solved. The reactor is divided into a feed gas preheating section at the upper part and a conversion reaction section at the lower part, and a natural gas steam conversion catalyst is arranged in a shell side of the conversion reaction section and an inner pipe of a heat exchange sleeve. According to the utility model, the primary conversion gas (890-930 ℃) from the primary converter enters from the bottom of the reactor, is distributed in a cavity at the lower part of the reactor through refractory bricks and metal distributors, is mixed with the conversion gas after the conversion reaction of the reactor, flows at a high speed from a sleeve annular space, and is subjected to heat exchange with the raw material gas which flows through the inner pipe and the inter-pipe of the sleeve and is heated to the reaction temperature through the catalyst bed layer to provide the heat of the conversion reaction; the converted gas discharged from the catalyst bed of the reactor is mixed with the first-stage converted gas in the bottom cavity of the reactor and then enters the annular space of the sleeve; the converted gas from the reaction section enters a preheating section pipe, the raw material gas entering from the pipe is preheated to the activation temperature (more than 450 ℃) of the conversion reaction, and is cooled to about 610 ℃ at the same time, and the converted gas is discharged from the reactor to produce steam from a converted gas waste heat boiler and is continuously cooled; raw gas entering from a raw gas inlet at the top of the reactor is distributed into raw gas between an inner tube of a heat exchange sleeve and an outer tube of the heat exchange sleeve (shell pass) in proportion through a distributor at the end part of an inner seal head (distributor) and the heat exchange tube, then is uniformly distributed into the respective heat exchange tubes, exchanges heat with conversion gas exiting a reaction section, is heated to the activation temperature (more than 450 ℃) of conversion reaction, and is distributed into a conversion catalyst between the inner tube of the heat exchange sleeve and the outer tube of the heat exchange sleeve (shell pass) filled with the catalyst through an intermediate tube plate; the raw material gas heated to the activation temperature of the conversion reaction flows in the catalyst bed layer, and flows through the inner tube of the heat exchange sleeve and the outer tube wall of the heat exchange sleeve to exchange heat with the conversion gas flowing at high speed in the annular space of the heat exchange sleeve in a countercurrent way, so that sensible heat in the conversion gas is absorbed, the conversion reaction is completed, and meanwhile, the conversion gas is heated to 760-800 ℃ when the conversion gas is discharged from the bed layer; the converted gas from the catalyst bed layer is fully combined with the first-stage converted gas (890-930 ℃) from the first-stage converter at the bottom of the reactor, and then flows at a high speed in the annular space of the heat exchange sleeve to provide the heat required by the conversion reaction of the reactor.

In order to achieve the above purpose, the present utility model provides the following technical solutions:

the utility model provides a pipe, shell side heat transfer natural gas vapor conversion reactor, includes reactor body and slip journal stirrup, the middle outer wall rigid coupling of reactor body has the slip journal stirrup, the upper and lower side of slip journal stirrup is equipped with conversion gas outlet portion and manhole portion respectively, and the left side of conversion gas outlet portion and manhole portion all is rigid coupling mutually with the reactor body, the internally mounted of reactor body has conversion device, connecting device is installed to conversion device's upper and lower side.

Preferably, the conversion device comprises a support piece, the outer wall of the support piece is fixedly connected with the reactor body, a shell side conversion catalyst layer and an inner tube conversion catalyst layer are fixedly connected to the upper and lower sides of the inside of the support piece respectively, a plurality of sleeves are fixedly connected to the shell side conversion catalyst layer and the inner tube conversion catalyst layer, and a thermal expansion compensation structure is fixedly connected to the upper outer wall of the sleeve.

Preferably, the upper outer walls of the sleeves are fixedly connected with inner sealing heads, refractory brick distribution cones are arranged below the inner sealing heads, and the inner sealing heads and the outer walls of the refractory brick distribution cones are fixedly connected with the inner wall of the reactor body.

Preferably, the connecting device comprises a disc, the outer walls of the disc are fixedly connected with the inner wall of the reactor body, a plurality of net plates are fixedly connected in the disc, rectangular blocks are arranged on the inner sides of the disc, a plurality of cross bars are fixedly connected on the outer walls of the rectangular blocks, and the outer sides of the cross bars are fixedly connected with the inner wall of the reactor body.

Preferably, the outer sides of the upper rectangular block and the lower rectangular block are rotatably connected with fan blades.

Preferably, the upper and lower sides of the fan blade are respectively provided with a raw material gas inlet part and a section of conversion gas inlet part, and the inner sides of the raw material gas inlet part and the section of conversion gas inlet part are fixedly connected with the reactor body.

The utility model provides a tube-shell side heat exchange natural gas steam conversion reactor, which has the beneficial effects that: the device comprises a reactor body, a first section of conversion gas, a refractory brick distribution cone, a lower disc, a screen plate, a fan blade, a conversion raw gas inlet, a sleeve pipe, a shell side conversion catalyst layer, a sleeve pipe inner tube conversion catalyst layer, a conversion gas boiler, a conversion gas outlet and a conversion gas boiler.

Drawings

FIG. 1 is a schematic diagram of the structure of the present utility model;

FIG. 2 is a plan cross-sectional view of FIG. 1;

FIG. 3 is a schematic view of the structure of the sleeve, the conversion gas outlet portion, and the inner head portion of FIG. 2;

FIG. 4 is a schematic view of the fan blade, the screen and the disk of FIG. 2;

fig. 5 is a perspective view of the disk of fig. 2.

In the figure: 1. reactor body, 2, sliding lugs, 3, conversion device, 301, support, 302, shell side conversion catalyst layer between sleeve pipes, 303, conversion catalyst layer inside sleeve pipes, 304, sleeve pipes, 305, thermal expansion compensation structure, 4, connection device, 401, disk, 402, screen plate, 403, rectangular block, 404, cross bar, 4A1, first cross bar, 4A2, landing leg, 4A3, second cross bar, 5, conversion gas outlet portion, 6, manhole portion, 7, inner sealing portion, 8, refractory brick distribution cone, 9, fan blade, 10, raw gas inlet portion, 11, one-stage conversion gas inlet portion.

The specific embodiment is as follows:

the utility model is further described below with reference to the accompanying drawings:

example 1:

referring to fig. 1-5, in this embodiment, a tube-shell side heat exchange natural gas vapor conversion reactor includes a reactor body 1 and a sliding support lug 2, wherein the sliding support lug 2 is fixedly connected to the middle outer wall of the reactor body 1, a conversion gas outlet portion 5 and a manhole portion 6 are respectively arranged above and below the sliding support lug 2, gas in the reactor body 1 can be discharged through the conversion gas outlet portion 5, the left sides of the conversion gas outlet portion 5 and the manhole portion 6 are fixedly connected with the reactor body 1, a conversion device 3 is installed in the reactor body 1, and a connecting device 4 is installed above and below the conversion device 3.

Referring to fig. 1 to 3, the conversion device 3 comprises a supporting member 301, a shell-side conversion catalyst layer 302 between the tubes, a sleeve pipe inner tube conversion catalyst layer 303, a sleeve pipe 304 and a thermal expansion compensation structure 305, wherein the outer wall of the supporting member 301 is fixedly connected with a reactor body 1, the shell-side conversion catalyst layer 302 between the tubes and the sleeve pipe inner tube conversion catalyst layer 303 are fixedly connected with the upper and lower parts of the inside of the supporting member 301 respectively, the shell-side conversion catalyst layer 302 between the tubes and the sleeve pipe inner tube conversion catalyst layer 303 can be fixed through the supporting member 301, the shell-side conversion catalyst layer 302 between the sleeve pipe and the sleeve pipe inner tube conversion catalyst layer 303 are fixedly connected with a plurality of sleeve pipes 304, the gas in the sleeve pipe 304 can perform heat exchange reaction through the shell-side conversion catalyst layer 302 between the sleeve pipe inner tube and the sleeve pipe inner tube conversion catalyst layer 303, the upper outer wall of the sleeve pipe 304 is fixedly connected with the thermal expansion compensation structure 305, the stability after the thermal expansion of the internal structure is improved, the upper outer walls of the plurality of the sleeves 304 are fixedly connected with inner seal heads 7, the lower parts 7 of the inner seal heads 7 can be sealed through the inner seal heads can be realized, the lower parts of the inner seal heads 7 are provided with the inner seal heads 8 and the inner wall 8 of the refractory brick body can be distributed with the inner seal heads 8 of the reactor body 1, and the inner wall of the refractory brick body can be distributed with the inner seal heads 8 is fixedly connected with the inner seal heads 1;

the first-stage conversion gas enters from the first-stage conversion gas inlet 11 at the bottom of the reactor body 1, the first-stage conversion gas is scattered through the refractory brick distribution cone 8 and the disc 401 at the lower part, uniformly passes through the screen 402 on the disc 401 at the lower part, and simultaneously blows the fan blades 9 at the lower part to rotate, so that the first-stage conversion gas is further scattered through the fan blades 9, uniformly enters into the cavity at the lower part of the reactor body 1, then enters from the raw material gas inlet 10 at the top of the reactor body 1, uniformly distributes into the sleeve 304 for preheating the raw material gas through the inner seal head 7, and the like, and the raw material gas flow reaching the activation temperature exchanges heat through the sleeve tube shell side conversion catalyst layer 302 and the sleeve tube conversion catalyst layer 303 to absorb heat required by the reaction, so as to carry out conversion reaction.

Referring to fig. 1, 2, 4 and 5, the connecting device 4 comprises a disc 401, a screen plate 402, rectangular blocks 403 and cross bars 404, the outer walls of the upper disc 401 and the lower disc 401 are fixedly connected with the inner wall of the reactor body 1, 4 screen plates 402 are fixedly connected inside the disc 401, gas can be dispersed through the disc 401 and the screen plates 402, the rectangular blocks 403 are arranged inside the upper disc 401 and the lower disc 401, the 4 cross bars 404 are fixedly connected with the outer walls of the rectangular blocks 403, the outer sides of the cross bars 404 are fixedly connected with the inner wall of the reactor body 1, the outer sides of the upper rectangular blocks 403 and the lower rectangular blocks 403 are rotationally connected with fan blades 9, and the gas can blow the fan blades 9, so that the gas can be dispersed further, the gas flowing speed is improved, the upper part and the lower part of the fan blades 9 are respectively provided with a raw gas inlet 10 and a section of conversion gas inlet 11, and the inner sides of the raw gas inlet 10 and a section of conversion gas inlet 11 are fixedly connected with the reactor body 1;

the first section of conversion gas absorbs the heat required by the reaction, the conversion reaction is carried out, the two gases are heated, fully mixed and homogenized at the same time of the reaction, and finally the conversion gas exits the reactor body 1 from the conversion gas outlet part 5, and the conversion gas waste heat boiler is removed.

In this embodiment, when an operator needs to use the tube-shell side heat exchange natural gas steam reforming reactor, a section of reformed gas is first introduced from the inlet 11 of the first section of reformed gas at the bottom of the reactor body 1, the first section of reformed gas is dispersed by the refractory brick distribution cone 8 and the lower disc 401, then uniformly passes through the mesh plate 402 on the lower disc 401, and simultaneously blows the lower fan blade 9 to rotate, such that the section of reformed gas is further dispersed by the fan blade 9, uniformly introduced into the cavity at the lower part of the reactor body 1, then introduced from the inlet 10 of the raw gas at the top of the reactor body 1, uniformly distributed into the sleeve 304 for preheating the raw gas by the inner head 7, and then heat exchanged by the raw gas flow reaching the activation temperature through the shell side reforming catalyst layer 302 and the inner sleeve tube reforming catalyst layer 303, and simultaneously the first section of reformed gas absorbs the heat required by the reaction, and the two sections of reformed gas are further dispersed by the fan blade 9, and finally the reformed gas is mixed at the temperature of the boiler body 1, and the waste heat of the boiler can be fully discharged from the outlet 5.

Example 2:

referring to fig. 1-5, in this embodiment, the present utility model provides a technical solution: the connecting device 4 can also comprise a first transverse plate 4A1, supporting legs 4A2 and a second transverse plate 4A3, wherein the interior of the first transverse plate 4A1 is fixedly connected with the middle outer wall of the reactor body 1, 2 supporting legs 4A2 are fixedly connected below the first transverse plate 4A1, the interior of the supporting legs 4A2 is fixedly connected with the second transverse plate 4A3, and the interior of the second transverse plate 4A3 is fixedly connected with the outer wall of a section of conversion gas inlet part 11;

the first transverse plate 4A1 can be arranged on the outer wall of the reactor body 1, the supporting leg 4A2 is arranged below the first transverse plate 4A1, the second transverse plate 4A3 is arranged on the inner side of the supporting leg 4A2, and the first section of conversion gas inlet 11 is fixed through the second transverse plate 4A3, so that the stability of the device is improved.

In this embodiment, when an operator needs to use the tube-shell side heat exchange natural gas steam reforming reactor, a first transverse plate 4A1 may be disposed on the outer wall of the reactor body 1, a supporting leg 4A2 is disposed below the first transverse plate 4A1, and a second transverse plate 4A3 is disposed on the inner side of the supporting leg 4A2, and a section of reformed gas inlet 11 is fixed through the second transverse plate 4A3, so that stability of the apparatus is improved.

While the utility model has been shown and described with reference to a preferred embodiment, it will be understood by those of ordinary skill in the art that various changes in form and details may be made therein without departing from the scope of the utility model.

Claims

1. The utility model provides a pipe, shell side heat transfer natural gas steam reforming reactor, includes reactor body (1) and slip journal stirrup (2), the middle outer wall rigid coupling of reactor body (1) has slip journal stirrup (2), its characterized in that: the upper and lower side of slip journal stirrup (2) is equipped with conversion gas outlet portion (5) and manhole portion (6) respectively, and conversion gas outlet portion (5) and manhole portion (6) left side all with reactor body (1) looks rigid coupling, internally mounted of reactor body (1) has conversion device (3), connecting device (4) are installed to the upper and lower side of conversion device (3).

2. A tube-on-shell heat exchange natural gas vapor conversion reactor as defined in claim 1 wherein: the conversion device (3) comprises a supporting piece (301), the outer wall of the supporting piece (301) is fixedly connected with the reactor body (1), a shell side conversion catalyst layer (302) and a shell inner tube conversion catalyst layer (303) are fixedly connected to the upper and lower sides of the inside of the supporting piece (301), a plurality of sleeves (304) are fixedly connected to the inner parts of the shell side conversion catalyst layer (302) and the shell inner tube conversion catalyst layer (303), and a thermal expansion compensation structure (305) is fixedly connected to the outer wall of the upper part of the sleeve (304).

3. A tube-on-shell heat exchange natural gas vapor conversion reactor as defined in claim 2 wherein: an inner sealing head part (7) is fixedly connected to the outer wall above the plurality of sleeves (304), a refractory brick distribution cone (8) is arranged below the inner sealing head part (7), and the outer walls of the inner sealing head part (7) and the refractory brick distribution cone (8) are fixedly connected with the inner wall of the reactor body (1).

4. A tube-on-shell heat exchange natural gas vapor conversion reactor as defined in claim 1 wherein: the connecting device (4) comprises a disc (401), wherein the outer wall of the disc (401) is fixedly connected with the inner wall of the reactor body (1), a plurality of screen plates (402) are fixedly connected in the disc (401), rectangular blocks (403) are arranged on the inner sides of the disc (401), a plurality of cross bars (404) are fixedly connected on the outer walls of the rectangular blocks (403), and the outer sides of the cross bars (404) are fixedly connected with the inner wall of the reactor body (1).

5. A tube-on-shell heat exchange natural gas vapor conversion reactor as defined in claim 4 wherein: the outer sides of the upper rectangular block (403) and the lower rectangular block are rotatably connected with fan blades (9).

6. A tube-on-shell heat exchange natural gas vapor conversion reactor as defined in claim 5 wherein: the upper and lower sides of flabellum (9) are equipped with raw materials gas inlet (10) and one section conversion gas inlet (11) respectively, and the inboard of raw materials gas inlet (10) and one section conversion gas inlet (11) all is with reactor body (1) looks rigid coupling.