CN218642475U

CN218642475U - Steam reforming hydrogen production conversion pipe and conversion furnace comprising same

Info

Publication number: CN218642475U
Application number: CN202223038772.3U
Authority: CN
Inventors: 杨帆; 张维; 郑蕾
Original assignee: Sichuan Chuangda Xinneng Technology Co ltd
Current assignee: Sichuan Chuangda Xinneng Technology Co ltd
Priority date: 2022-11-15
Filing date: 2022-11-15
Publication date: 2023-03-17
Anticipated expiration: 2032-11-15

Abstract

The utility model provides a steam reforming hydrogen production reformer tube and a reformer comprising the same. The conversion pipe comprises a pipe body, a catalyst bed layer, a core pipe, a heat exchange device and a sieve hole pipe. The catalyst bed layer is arranged in the pipe body and divides the inside of the pipe body into an upper cavity and a lower cavity; the core tube penetrates the catalyst bed. The heat exchange device is arranged on the upper cavity, the upper end of the heat exchange device is provided with a raw material gas heat exchange inlet and a converted gas heat exchange outlet, and the lower end of the heat exchange device is provided with a raw material gas heat exchange outlet and a converted gas heat exchange inlet; wherein, the raw gas heat exchange outlet is communicated with the upper end of the core tube, and the reformed gas heat exchange inlet is communicated with the upper cavity. The screen hole pipe is sleeved outside the core pipe, and a transverse gap is formed between the screen hole pipe and the core pipe. The utility model discloses a reformer and reborner, the maintenance of equipment personnel of being convenient for withdraws the core pipe when changing the catalyst, avoids appearing bending or damaging the condition of core pipe.

Description

Steam reforming hydrogen production conversion pipe and conversion furnace comprising same

Technical Field

The utility model relates to a natural gas steam reforming hydrogen manufacturing technical field, concretely relates to steam reforming hydrogen manufacturing reformer tube and contain its reborner.

Background

In recent years, the market demand for small-scale hydrogen production is gradually increased, and the small-scale natural gas steam reforming hydrogen production reformer is more important. In order to make the device small, most of the conversion tubes adopt a flow channel design mode that the upper end of raw material gas enters and the upper end of converted gas exits. In such a top-up design, a core tube is typically inserted through the catalyst bed to guide the feed gas from the bottom of the catalyst bed into the catalytic reforming reaction zone.

Since the catalyst life is much less than the reformer life, equipment maintenance personnel are required to go to the site to replace the catalyst during the life cycle of the reformer after the catalyst in the reformer tubes has failed. However, when the equipment maintenance personnel replace the catalyst, the core tube is often bent or damaged in the process of withdrawing the core tube from the catalyst bed layer.

SUMMERY OF THE UTILITY MODEL

In order to solve the technical problem, the utility model provides a steam reforming hydrogen production reformer tube and a reformer comprising the steam reforming hydrogen production reformer tube.

On the one hand, the utility model provides a steam reforming hydrogen production converting pipe, including body, catalyst bed, core pipe, heat exchange device and sieve mesh pipe. The catalyst bed layer is arranged in the pipe body and divides the inside of the pipe body into an upper cavity and a lower cavity; the core tube penetrates the catalyst bed. The heat exchange device is arranged on the upper cavity, the upper end of the heat exchange device is provided with a raw material gas heat exchange inlet and a converted gas heat exchange outlet, and the lower end of the heat exchange device is provided with a raw material gas heat exchange outlet and a converted gas heat exchange inlet; wherein, the raw gas heat exchange outlet is communicated with the upper end of the core tube, and the reformed gas heat exchange inlet is communicated with the upper cavity. The screen hole pipe is sleeved outside the core pipe, and a transverse gap is formed between the screen hole pipe and the core pipe. Preferably, the size of the transverse gap is 1 to 3mm.

Preferably, the heat exchange device includes a first heat exchange portion, a second heat exchange portion, and an air flow reversing portion. The top of the first heat exchange part is provided with the raw material gas heat exchange inlet and the reformed gas heat exchange outlet, the first heat exchange part comprises an inner reformed gas cooling channel and an outer raw material gas heating channel, the outer raw material gas heating channel is communicated to the raw material gas heat exchange inlet, and the inner reformed gas cooling channel is communicated to the reformed gas heat exchange outlet. The bottom of the second heat exchange part is provided with a reformed gas heat exchange inlet and a raw material gas heat exchange outlet, the second heat exchange part comprises a reformed gas heat dissipation gas circuit and a raw material gas heat absorption gas circuit, the reformed gas heat dissipation gas circuit is communicated to the reformed gas heat exchange inlet, and the raw material gas heat absorption gas circuit is communicated to the raw material gas heat exchange outlet. The air flow diversion part enables the outer raw material gas temperature-rising flow passage to be communicated with the raw material gas heat-absorbing gas passage and enables the converted gas heat-dissipating gas passage to be communicated with the inner converted gas temperature-reducing flow passage.

Specifically, the first heat exchange part is configured to comprise an inner barrel and an outer barrel surrounding the inner barrel, an inner reforming gas cooling flow passage is limited by the inner barrel, an outer raw material gas heating flow passage is limited by a flow passage between the outer barrel and the inner barrel, a raw material gas heat exchange inlet is arranged at the top of the outer barrel, and a reforming gas heat exchange outlet is arranged at the top of the inner barrel. Specifically, the air flow diversion part comprises a first cavity, a second cavity and a partition positioned between the first cavity and the second cavity, and the partition is provided with a raw material air flow interface and a conversion air flow interface. The conversion gas heat dissipation channel is communicated with the inner conversion gas cooling channel through the second cavity and the conversion gas communication interface. The outer raw material gas temperature-rising flow channel is communicated with the raw material gas heat-absorbing gas channel through the first cavity and the raw material gas circulation interface.

Specifically, the second heat exchange portion comprises a shell, a first interface and a second interface are arranged at the upper end of the shell, the first interface is communicated with the raw gas flowing interface, the second interface is communicated with the second cavity, and a raw gas heat exchange outlet and a converted gas heat exchange inlet are arranged at the lower end of the shell. Further, the second heat exchange portion further comprises a plurality of heat exchange tubes which are longitudinally arranged, the upper end of each heat exchange tube is communicated with the second interface, and the lower end of each heat exchange tube is communicated with the reformed gas heat exchange inlet. Furthermore, the second heat exchange part also comprises a drainage tube, the drainage tube is surrounded by a plurality of heat exchange tubes, the upper end of the drainage tube is communicated with the first interface, and the lower end of the drainage tube is communicated with the raw material gas heat exchange outlet; wherein, the upper end of the drainage tube in the shell is provided with a raw material gas inflow diversion hole, and the lower end of the drainage tube in the shell is provided with a raw material gas outflow diversion hole. The second heat exchange part further comprises a blocking member which is arranged between the raw material gas inflow diversion hole and the raw material gas outflow diversion hole so as to block the circulation of the raw material gas in the drainage tube. Furthermore, the second heat exchange part also comprises a plurality of first baffling pieces and a plurality of second baffling pieces which are arranged in the shell, and the first baffling pieces and the second baffling pieces are alternately arranged along the length direction of the drainage tube; the distance between the position of the first baffle for deflecting the feed gas and the central longitudinal axis of the drainage tube is larger than the distance between the position of the second baffle for deflecting the feed gas and the central longitudinal axis of the drainage tube. Wherein the plurality of heat exchange tubes define a reformed gas heat dissipation gas path; the outer wall of the drainage tube, the inner wall of the shell, the first deflection piece and the second deflection piece jointly limit a raw material gas heat absorption gas path.

In particular, the first baffle is configured as a disk-shaped baffle, and the second baffle is configured as a ring-shaped baffle. Wherein, the outer diameter of the disc-shaped baffle plate is larger than the inner diameter of the ring-shaped baffle plate, and the feed gas is baffled by the outer edge of the disc-shaped baffle plate and the inner edge of the ring-shaped baffle plate.

On the other hand, the utility model provides a reformer, this reformer includes the reformer tube of above-mentioned first aspect.

The utility model discloses a characteristics and advantage include:

(1) Because the sieve hole pipe is arranged between the catalyst bed layer and the core pipe, and the transverse gap is formed between the sieve hole pipe and the core pipe, equipment maintenance personnel can evacuate the core pipe when replacing the catalyst, and the condition that the core pipe is bent or damaged is avoided.

(2) Because the raw material gas entering the transverse gap between the sieve hole pipe and the core pipe can enter the catalyst bed layer through the holes on the sieve hole pipe to react, the raw material gas can be prevented from directly flowing upwards through the gap channel between the sieve hole pipe and the core pipe and mixing into the converted gas flow, and the conversion rate of the raw material gas is improved.

(3) The converted gas generated by the reaction in the catalyst bed layer can enter the channel where the gap is positioned through the pores on the sieve tube, and the converted gas flowing in the gap can transfer heat to the raw material gas in the core tube, thereby being more beneficial to the temperature rise of the raw material gas in the core tube.

Drawings

In order to more clearly illustrate the technical solutions in the embodiments of the present disclosure, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present disclosure, and it is obvious for those skilled in the art to obtain other drawings based on the drawings without creative efforts.

FIG. 1 is a schematic diagram of a steam reforming hydrogen production reformer to which the present invention relates;

FIG. 2 is a schematic diagram of a steam reforming hydrogen production reformer according to the present invention;

FIG. 3 is an enlarged view of a portion of the screen pipe and core pipe of FIG. 2;

FIG. 4 is an enlarged perspective view of a portion of the screen pipe;

fig. 5 is a schematic view of a heat exchange device according to an embodiment of the present invention;

FIG. 6 is a schematic view of an embodiment of the second heat exchange portion of FIG. 5;

FIG. 7A is a schematic view of the first baffle of FIG. 6;

fig. 7B is a schematic view of the second baffle of fig. 6.

Detailed Description

The technical solutions in the embodiments of the present disclosure will be clearly and completely described below with reference to the drawings in the embodiments of the present disclosure, and it is obvious that the described embodiments are only a part of the embodiments of the present disclosure, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments disclosed herein without making any creative effort, shall fall within the protection scope of the present disclosure.

Referring to fig. 1, the present invention discloses a steam reforming hydrogen production reformer 200, such as a natural gas reforming hydrogen production reformer, which performs reforming conversion reaction on a raw material gas (a mixture of natural gas and steam) to generate reformed gas (a mixture of methane, hydrogen, CO2, and H2O). A plurality of burners 23 and reformer tubes 100 are provided within the reformer 200, with the reformer tubes 100 extending longitudinally down from the furnace top region 21 into the reformer body 22. The high temperature flue gas generated by the combustion of the burner 23 provides the heat required for the reforming conversion reaction in the reformer tubes 100.

In some embodiments, referring to FIG. 2, the reformer tube 100 includes a tube body 11, a porous support plate 17, a catalyst bed 12, and a heat exchange device 60. Wherein, a porous support plate 17 is provided at the lower end of the inner side of the tube body 11 for providing support for the catalyst bed 12. The heat exchange device 60 is used for exchanging heat between the raw gas to be heated and the reformed gas to be cooled.

With continued reference to FIG. 2, a catalyst bed 12 is disposed within the tubular body 11, the catalyst bed 12 dividing the tubular body 11 into an upper chamber 11a and a lower chamber 11b. The core tube 13 extends through the catalyst bed 12, the bottom end of the core tube 13 slightly exceeds the bottom of the catalyst bed 12 or is substantially flush with the bottom of the catalyst bed 12, and the top end of the core tube 13 exceeds the top of the catalyst bed 12 or is substantially flush with the top of the catalyst bed 12.

Specifically, the heat exchanger 60 is disposed in the upper chamber 11a, an upper end of the heat exchanger 60 has a raw gas heat exchange inlet 60a and a reformed gas heat exchange outlet 60b, and a lower end of the heat exchanger 60 has a raw gas heat exchange outlet 60c and a reformed gas heat exchange inlet 60d. Wherein, the raw gas heat exchange outlet 60c is communicated with the upper end of the core tube 13, and the reformed gas heat exchange inlet 60d is communicated with the upper chamber 11 a.

With continued reference to fig. 2 and 3, according to some embodiments of the present disclosure, the core tube 13 is sleeved with a perforated tube 15, and there is a transverse gap 16 between the core tube 13 and the perforated tube 15. Preferably, the transverse dimension L of the gap 16 is between 1 and 3mm. Wherein the length of the perforated pipes 15 substantially corresponds to the height of the catalyst bed 12 or the top of the perforated pipes 15 is slightly higher than the top of the catalyst bed 12.

There is a need to replace the spent catalyst bed 12 during use and maintenance of the plant. Specifically, when the catalyst bed 12 is replaced, the heat exchange device 60 and the core pipe 13 connected thereto are removed. Because the sieve pore tube 15 separates the catalyst bed layer 12 from the core tube 13 and the gap 16 is arranged between the sieve pore tube 15 and the core tube 13, the core tube is convenient for equipment maintenance personnel to remove, and the condition of bending or damaging the core tube is avoided.

The heat exchanging device 60 is used for exchanging heat between the raw material gas and the reformed gas, so as to lower the temperature of the reformed gas and raise the temperature of the raw material gas. Specifically, feed gas stream 18a flows into heat exchange device 60 from feed gas heat exchange inlet 60a and out of heat exchange device 60 from feed gas heat exchange outlet 60 c; reformed gas stream 18b flows into heat exchange apparatus 60 from reformed gas heat exchange inlet 60d and flows out of heat exchange apparatus 60 from reformed gas heat exchange outlet 60b.

The raw material gas flow 18a after heat exchange by the heat exchange device 60 flows out of the raw material gas heat exchange outlet 60c and then enters the core tube 13, and the raw material gas flow 18a enters the lower cavity 11b downwards along the core tube 13 and then enters the catalyst bed layer 12 through the pores on the porous support plate 17 for reaction. The reaction produces a reformed gas stream 18b which enters upper chamber 11a from the top of catalyst bed 12 and flows into heat exchange means 60 through reformed gas heat exchange inlet 60d.

Feed gas stream 18a flows upwardly from lower chamber 11b, and a small amount of feed gas enters the channels in gap 16. Because the perforated pipes 15 are provided with pores, the raw material gas in the gap 16 can enter the catalyst bed layer 12 through the pores on the perforated pipes 15 to carry out reforming reaction, so that the raw material gas can be prevented from directly flowing upwards and mixing into the converted gas flow in the upper cavity 11a, and the conversion rate of the raw material gas is improved. Meanwhile, the converted gas generated by the reaction in the catalyst bed layer 12 can also enter the channel where the gap 16 is located through the pores on the sieve tube 15, and the converted gas flowing in the gap 16 can transfer heat to the raw gas in the core tube 13, which is beneficial to the temperature rise of the raw gas in the core tube 13; that is, the core tube 13, the gap 16 and the mesh tube 15 constitute one heat exchange assembly. The feed gas is further subjected to a temperature increase by the heat exchange assembly after being subjected to a temperature increase by the heat exchange device 60.

According to some preferred embodiments of the present invention, referring to fig. 5, the heat exchanging device 60 includes a first heat exchanging part 61, a second heat exchanging part 62, and an air flow reversing part 63.

The top of the first heat exchange part 61 is provided with a raw gas heat exchange inlet 60a and a reformed gas heat exchange outlet 60b. The first heat exchange portion 61 has an inner reformed gas cooling flow passage 61a and an outer raw material gas heating flow passage 61b, the outer raw material gas heating flow passage 61b is communicated to the raw material gas heat exchange inlet 60a, and the inner reformed gas cooling flow passage 61a is communicated to the reformed gas heat exchange outlet 60b.

The second heat exchange portion 62 has a reformed gas heat exchange inlet 60d and a raw gas heat exchange outlet 60c at the bottom thereof. The second heat exchange portion 62 has a reformed gas heat-dissipating gas path 62a and a raw material gas heat-absorbing gas path 62b, the reformed gas heat-dissipating gas path 62a is communicated to the reformed gas heat exchange inlet 60d, and the raw material gas heat-absorbing gas path 62b is communicated to the raw material gas heat exchange outlet 60c. Alternatively, in some embodiments, only one reformed gas heat exchange inlet 60d is provided at the bottom of the second heat exchange portion 62; in other embodiments, the bottom of the second heat exchange portion 62 may be provided with a plurality of reformed gas heat exchange inlets 60d.

The airflow diverting part 63 fluidly connects the outer raw material gas temperature increasing flow passage 61b of the first heat exchange part 61 to the raw material gas heat absorbing flow passage 62b of the second heat exchange part 62, and fluidly connects the reformed gas heat dissipating flow passage 62a of the second heat exchange part 62 to the inner reformed gas temperature decreasing flow passage 61a of the first heat exchange part 61.

Specifically, the first heat exchange portion 61 is configured to include an inner tube 611 and an outer tube 612 surrounding the inner tube 611, the inner reformed gas temperature decreasing flow passage 61a is defined by the inner tube 611, and the outer raw material gas temperature increasing flow passage 61b is defined by a flow passage between the outer tube 612 and the inner tube 611. The raw gas heat exchange inlet 60a is disposed at the top of the outer tube 612, and the reformed gas heat exchange outlet 60b is disposed at the top of the inner tube 611.

Specifically, the air flow guide 63 includes a first chamber 631c, a second chamber 631d, and a partition 631 located between the first chamber 631c and the second chamber 631d, and the partition 631 is provided with a raw material air flow interface 631a and a conversion air flow interface 631b.

Specifically, the reformed gas heat-dissipating air passage 62a of the second heat exchange portion 62 is fluidly connected to the inner reformed gas temperature-reducing flow passage 61a of the first heat exchange portion 61 through the second chamber 631d and the reformed gas flow-through interface 631b provided on the partition 631. Specifically, the outer raw material gas temperature increasing flow passage 61b of the first heat exchange portion 61 is fluidly connected to the raw material gas heat absorbing gas passage 62b of the second heat exchange portion through the first chamber 631c and the raw material gas flow interface 631a provided in the partition 631.

The utility model discloses a set up the interior hot first heat exchange portion 61 of outer cold, can reduce the heat loss of converter 100 upper end, improve heat utilization rate, make the heat be used for the intensification heating of feed gas more effectively. Further, by providing the first heat exchange unit 61, the second heat exchange unit 62, and the air flow diversion unit 63, the air flow diversion unit 63 causes the raw material gas outside the first heat exchange unit 61 to be subjected to a one-stage temperature rise and then to be guided into the appropriate second heat exchange unit 62 to continue the temperature rise. Since the first heat exchange portion 61 and the second heat exchange portion 62 provide effective heat exchange for the source gases, respectively, the amount of heat required for the source gases thereafter decreases; therefore, the design of the heat exchange path or the heat exchange device after the second heat exchange part 62 for raising the temperature of the raw material gas can be simplified, so that the length of the reforming pipe 100 can be made short and the reformer 200 device can be made small.

According to some preferred embodiments of the present invention, referring to fig. 6, the second heat exchange portion 62 comprises a housing 620, the upper end of the housing 620 has a first interface 620a and a plurality of second interfaces 620b, and the lower end of the housing 620 has a raw gas heat exchange outlet 60c and a plurality of reformed gas heat exchange inlets 60d of the whole heat exchange device 60. The first connection port 620a communicates with a raw gas flow connection port 631a of the partition 631 in the gas flow reversing unit 63, and the second connection port 620b communicates with the second chamber 631 of the gas flow reversing unit 63.

With continued reference to fig. 6, the second heat exchange portion 62 further includes a plurality of heat exchange tubes 623 arranged longitudinally, and an upper end of each heat exchange tube 623 is communicated to the second connector 620b, and thus communicated with the second chamber 631 of the airflow reversing portion 63. The lower end of each heat exchange tube 623 is communicated to the reformed gas heat exchange inlet 60d, and particularly, the lower end of each heat exchange tube 623 is the reformed gas heat exchange inlet 60d.

Further, the second heat exchange portion 62 further includes a guide tube 625 surrounded by the plurality of heat exchange tubes 623. The upper end of the draft tube 625 communicates with the first port 620a, and thus further communicates with the raw gas flow port 631a on the partition 631 in the gas flow reversing part 63. The lower end of the draft tube 625 is communicated with the feed gas heat exchange outlet 60c, and particularly, the lower end of the draft tube 625 is the feed gas heat exchange outlet 60c. Wherein, the upper end of the draft tube 625 in the case 620 is provided with a raw gas inflow guide hole 625a, the lower end of the draft tube 625 in the case 620 is provided with a raw gas outflow guide hole 625c, and a blocking member 625b is provided between the raw gas inflow guide hole 625a and the raw gas outflow guide hole 625c to block the flow of the raw gas in the draft tube 625. Specifically, the source gas inflow guide holes 625a are arranged in three rows in the longitudinal direction, with 4 holes per row; the source gas outflow guide holes 625c are arranged in a similar manner to the source gas inflow guide holes 625 a. The guide holes 625a and 625b are respectively provided at the upper and lower ends close to the guide tube 625, so that the movement distance of the raw material gas heat-exchanged with the reformed gas in the heat exchange tube 623 in the second heat exchange part 62 can be increased, and the heat exchange time can be increased to thereby improve the heat exchange effect.

Preferably, the second heat exchange portion 62 further includes a plurality of first baffle 621 and a plurality of second baffle 622 alternately arranged along the length direction of the drainage tube 625, wherein the first baffle 621 and the second baffle 622 are both disposed inside the housing 620. In particular, a distance W1 (first deflection position distance) between the position of the first deflection member 621 deflecting the source gas and the central longitudinal axis of the draft tube 625 is greater than a distance W2 (second deflection position distance) between the position of the second deflection member 622 deflecting the source gas and the central longitudinal axis of the draft tube 625. In other words, the first baffling location is distal to the draft tubes 625 and adjacent to the sidewalls of the housing 620 and the second baffling location is distal to the sidewalls of the housing 620 and adjacent to the draft tubes 625.

In the preferred second heat exchange portion 62 as shown in fig. 6, a plurality of heat exchange tubes 623 define the reformed gas heat dissipation gas path 62a; the outer wall of the draft tube 625, the inner wall of the housing 620, the first baffle 621, and the second baffle 622 collectively define the feed gas heat absorption gas path 62b.

In some embodiments, the first baffle 621 is configured as a disc-shaped baffle (refer to fig. 7A), and the second baffle 622 is configured as an annular baffle (refer to fig. 7B). Wherein, the inner diameter of the disc-shaped baffle plate is matched with the outer diameter of the drainage tube, and the outer diameter of the disc-shaped baffle plate is smaller than the inner diameter of the shell; the outer diameter of the circular baffle plate is matched with the inner diameter of the shell, and the inner diameter of the circular baffle plate is larger than the outer diameter of the drainage tube. And the outer diameter D1 of the disc-shaped baffle plate is larger than the inner diameter D2 of the ring-shaped baffle plate, so that the feed gas is baffled by the outer peripheral edge OE of the disc-shaped baffle plate and the inner peripheral edge IE of the ring-shaped baffle plate.

By arranging the bent raw material gas heat absorption gas circuit 62b, the path of the raw material gas from the raw material gas inflow guide hole 625a to the raw material gas outflow guide hole 625c is prolonged, so that the heat exchange time can be prolonged, and the heat exchange is more sufficient.

Specifically, referring to fig. 5, the raw material gas enters the heat exchange device 60 from the raw material gas heat exchange inlet 60a at the top of the outer cylinder 612 of the first heat exchange portion 61, and enters the first cavity 631c of the gas flow reversing portion 63 along the outer raw material gas temperature increasing flow channel 61 b. The raw material gas then enters the first connection port 620a of the second heat exchange unit 62 through the raw material gas flow connection port 631a of the gas flow reversing unit 63.

Referring to fig. 6, after the raw material gas enters the second heat exchange portion 62, the flow path direction is first guided by three rows of raw material gas inflow guide holes 625a at the upper end of the draft tube 625 so that the raw material gas enters the cavity defined by the outer wall of the draft tube 625 and the inner wall of the housing 620, and finally, the flow path direction is guided by three rows of raw material gas outflow guide holes 625c at the lower end of the draft tube 625 so that the raw material gas flows toward the raw material gas heat exchange outlet 60c. In the draft tube 625, a barrier 625b is provided between the raw material gas inflow guide hole 625a and the raw material gas outflow guide hole 625c, and the draft tube 625 is blocked by the barrier 625b, so that the raw material gas cannot vertically flow downward in the draft tube 625.

On the raw material gas flow path in the second heat exchange portion 62, the raw material gas flow 18a is alternately guided by the first and

second deflectors

621 and 622 in the flow path direction between the raw material gas inflow guide holes 625a and the raw material gas outflow guide holes 625 c. Wherein the first baffle 621 communicates with the raw material gas flow path at a position adjacent to the inner wall of the housing 620, and the second baffle 622 communicates with the raw material gas flow path at a position adjacent to the outer wall of the draft tube 625. Preferably, the baffles located uppermost and lowermost are the first baffles 621, so that the flow path of the source gas is longer. The raw gas flow 18a is guided through the flow path by the lowermost first baffle 621, and then passes through the raw gas outflow guide hole 625c to reach the raw gas heat exchange outlet 60c (the lower end of the draft tube 625) of the heat exchange device 60.

The reformed gas escapes from the top of the catalyst bed 12 to the upper chamber 11a and then enters the heat exchange tube 623 through the reformed gas heat exchange inlet 60d at the lower end of the second heat exchange portion 62. In the cavity defined by the outer wall of the draft tube 625 and the inner wall of the housing 620, the heat exchange tube 623 is filled with the baffled feed gas flow 18a, and the reformed gas flow 18b inside the heat exchange tube 623 radiates heat outwards, so that the feed gas flow 18a is heated. The reformed gas flow 18b flows upward from the second interface 620b at the upper end of the heat exchange tube 623 into the second chamber 631d of the gas flow reversing part 63, and further, the reformed gas flow 18b flows from the reformed gas flow interface 631b on the partition 631 of the gas flow reversing part 63 into the inner reformed gas cooling flow passage 61a defined by the inner tube 611 of the first heat exchange part 61, and finally flows out of the heat exchange device 60 from the reformed gas heat exchange outlet 60b at the top of the inner tube 611.

It is readily understood by a person skilled in the art that the above described preferred heat exchange device does not constitute a specific limitation of the core protective idea of the invention. Under the development of the general idea of the utility model, other heat exchange devices can be arranged on the upper cavity alternatively; the present invention does not preclude protection of the reformer tubes with these alternative heat exchange means.

The above description is only a few embodiments of the present disclosure, and those skilled in the art can make various changes or modifications to the embodiments of the present disclosure without departing from the spirit and scope of the present disclosure based on the disclosure of the application document.

Claims

1. A steam reforming hydrogen production reformer tube, comprising:

a pipe body;

the catalyst bed layer is arranged in the pipe body and divides the inside of the pipe body into an upper cavity and a lower cavity;

the core pipe penetrates through the catalyst bed layer;

the heat exchange device is arranged on the upper cavity, the upper end of the heat exchange device is provided with a raw material gas heat exchange inlet and a converted gas heat exchange outlet, and the lower end of the heat exchange device is provided with a raw material gas heat exchange outlet and a converted gas heat exchange inlet; wherein, the raw gas heat exchange outlet is communicated with the upper end of the core pipe, and the reformed gas heat exchange inlet is communicated with the upper cavity; and

the screen hole pipe, outside the screen hole pipe box was located the core pipe, and had horizontal clearance between screen hole pipe and the core pipe.

2. The reformer tube of claim 1, wherein the heat exchange means comprises:

the top of the first heat exchange part is provided with the feed gas heat exchange inlet and the reformed gas heat exchange outlet; the first heat exchange part comprises an inner reforming gas cooling channel and an outer raw material gas heating channel, the outer raw material gas heating channel is communicated to the raw material gas heat exchange inlet, and the inner reforming gas cooling channel is communicated to the reforming gas heat exchange outlet;

the bottom of the second heat exchange part is provided with the reforming gas heat exchange inlet and the feed gas heat exchange outlet; the second heat exchange part comprises a reformed gas heat dissipation gas path and a raw material gas heat absorption gas path, the reformed gas heat dissipation gas path is communicated to the reformed gas heat exchange inlet, and the raw material gas heat absorption gas path is communicated to the raw material gas heat exchange outlet; and

and the airflow diversion part enables the outer-side raw material gas heating channel to be communicated with the raw material gas heat absorption gas channel in a fluid mode, and enables the converted gas heat dissipation gas channel to be communicated with the inner-side converted gas cooling channel in a fluid mode.

3. The reformer tube of claim 2, wherein the first heat exchange section is configured to include an inner barrel and an outer barrel surrounding the inner barrel, the inner reformer gas cooling flow path is defined by the inner barrel, the outer feed gas warming flow path is defined by a flow path between the outer barrel and the inner barrel, the feed gas heat exchange inlet is provided at a top of the outer barrel, and the reformer gas heat exchange outlet is provided at a top of the inner barrel;

the airflow diversion part comprises a first cavity, a second cavity and a partition positioned between the first cavity and the second cavity, and the partition is provided with a raw material gas circulation interface and a conversion gas circulation interface;

the reformed gas cooling gas passage is communicated with the inner reformed gas cooling flow passage through the second cavity and the reformed gas circulation interface;

the outer-side raw material gas temperature-rising flow channel is communicated to the raw material gas heat-absorbing gas path through the first cavity and the raw material gas circulation interface.

4. The reformer tube of claim 3, wherein said second heat exchange portion comprises:

the upper end of the shell is provided with a first interface and a second interface, the first interface is communicated with the raw material gas circulation interface, the second interface is communicated with the second cavity, and the lower end of the shell is provided with the raw material gas heat exchange outlet and the converted gas heat exchange inlet;

the upper end of each heat exchange tube is communicated with the second interface, and the lower end of each heat exchange tube is communicated with the converted gas heat exchange inlet;

the drainage tube is surrounded by the plurality of heat exchange tubes, the upper end of the drainage tube is communicated with the first interface, and the lower end of the drainage tube is communicated with the feed gas heat exchange outlet; wherein, the upper end of the drainage tube in the shell is provided with a raw material gas inflow diversion hole, and the lower end of the drainage tube in the shell is provided with a raw material gas outflow diversion hole;

the blocking piece is arranged between the raw material gas inflow diversion hole and the raw material gas outflow diversion hole so as to block the circulation of the raw material gas in the drainage tube; and

the first baffling pieces and the second baffling pieces are arranged in the shell and are alternately arranged along the length direction of the drainage tube; the distance between the position of the first baffle for baffling the feed gas and the central longitudinal axis of the drainage tube is greater than the distance between the position of the second baffle for baffling the feed gas and the central longitudinal axis of the drainage tube;

wherein the plurality of heat exchange tubes define the reformed gas heat dissipation gas path; the outer wall of the draft tube, the inner wall of the housing, the first baffle and the second baffle jointly define the feed gas heat absorption gas path.

5. The reformer tube of claim 4, wherein the first baffle is configured as a disk-shaped baffle and the second baffle is configured as an annular baffle;

the outer diameter of the disc-shaped baffle plate is larger than the inner diameter of the annular baffle plate, and the feed gas is baffled by the outer edge of the disc-shaped baffle plate and the inner edge of the annular baffle plate.

6. The reformer tube of claim 1, wherein the transverse gap has a dimension of from 1 mm to 3mm.

7. A reformer comprising the reformer tube of any of claims 1 to 6.