A methanol reforming hydrogen production reactor

Abstract

The invention discloses a methanol reforming hydrogen production reactor, which relates to the technical field of reforming hydrogen production, and comprises a shell, a partition, a catalytic component, an inner tank, etc. Under the same volume, the total area of ​​the outer facade and the inner facade of the foam metal catalyst bed of the invention is increased by 10% to 15% compared with the hollow cylindrical shape, and has a larger contact area, which is conducive to the reaction; the heat exchange tube group adopts a skeleton-type integrated structure, has a more uniform heat transfer characteristic, and relative to the columnar structure, when the foam metal catalyst bed occupies the same size of external space, the volume of the foam metal catalyst bed can be increased by 10% to 15%, has a larger contact volume, and is conducive to the reaction; the wave-type structure of the outer facade and the inner facade on the foam metal catalyst bed has better fluid mechanics characteristics, can increase the disturbance of reactants in the flow channel, and is conducive to the reaction; the shell and the inner tank are insulated by vacuuming or heat-insulating by passing a heat transfer fluid to ensure that the temperature in the reaction space is uniform and stable, which is more conducive to the thermal reaction.

Description

Technical Field

[0001] The invention relates to the technical field of reforming hydrogen production, and in particular to a methanol reforming hydrogen production reactor. Background Art

[0002] At present, in the field of green hydrogen, photovoltaic or solar thermal hydrogen production is usually adopted. Among them, photovoltaic hydrogen production directly uses photovoltaic panels to generate electricity, and uses electricity to directly electrolyze water to produce hydrogen. This method has problems such as high energy consumption, low hydrogen production rate, difficulty in hydrogen storage and transportation, and high cost. Therefore, solar thermal hydrogen production technology has made great progress, especially the "solar thermal + valley electricity + energy storage" methanol reforming hydrogen production technology, which has the advantages of a wide source of raw materials, low price, convenient storage and transportation, and the ability to reuse existing infrastructure. In the field of methanol reforming hydrogen production, there is a core process component, namely the hydrogen production reactor.

[0003] At present, hydrogen production reactors mainly include four types: tubular reactors, plate reactors, membrane reactors and microchannel reactors. Among them, tubular reactors are widely used, but there are problems such as uneven internal heat transfer, insufficient chemical reaction rate, and insufficient methanol conversion rate. In addition, the equipment occupies a large space and is only suitable for large-scale hydrogen production industry scenarios. At the same time, as natural gas, which is closely related to methanol production, its source, namely natural gas fields and gas stations, especially scattered gas, has the characteristics of decentralization and miniaturization, and urgently needs corresponding miniaturized hydrogen production reactors. Summary of the invention

[0004] The purpose of the present invention is to provide a baffled methanol reforming hydrogen production reactor with uniform internal temperature, good heat and mass transfer performance, fast chemical reaction rate, high methanol conversion rate and compact size.

[0005] In view of the above technical problems, the technical solution adopted by the present invention is: a methanol reforming hydrogen production reactor, comprising a shell, a first pipe joint, a partition, a catalytic component, a second pipe joint, and an inner liner; there are two shells, which are fixedly installed on the upper and lower parts of the partition respectively; an inner liner is fixedly installed between each shell and the partition; a group of catalytic components is fixedly installed between each inner liner and the partition; the catalytic component is composed of a foam metal catalytic bed and a heat exchange tube group, and adopts an integrated molding process, and the foam metal catalytic bed is attached to the heat exchange tube group; each shell is provided with two first pipe joints arranged oppositely, and the first pipe joints connect the space between the inner liner and the partition; each shell is also provided with two second pipe joints arranged oppositely, and the second pipe joints connect the space between the shell and the inner liner.

[0006] Preferably, the foam metal catalyst bed comprises an outer facade, an inner facade, and a receiving hole system; the outer side surface of the foam metal catalyst bed is the outer facade; the inner side surface of the foam metal catalyst bed is the inner facade; the receiving hole system is used to receive the heat exchanger group; the outer facade and the inner facade are both curved surfaces with periodic fluctuations in the circumferential direction and the axial direction, and the curved surface is o - xyz The parametric equation in the space rectangular coordinate system is:

[0007] ;

[0008] In the formula, R is the radius of the base circle, mm; A is the amplitude of fluctuation, mm; K is the frequency of fluctuation; T is the number of z Change period in the axial direction; H-height boundary value, mm; t -Angular position parameter, rad.

[0009] Preferably, the heat exchange tube group includes an outer tube joint, a corrugated tube, and an inner tube joint; the corrugated tube is wavy in the circumferential direction, and has a plurality of wave crests and wave troughs, an outer tube joint is arranged on each wave crest, and an inner tube joint is arranged on each wave trough.

[0010] Preferably, the center line of the corrugated tube is a tube curve. o - xyz The parametric equation in the space rectangular coordinate system is:

[0011] ;

[0012] Where, r-radial distribution radius, mm; h-axial amplitude, mm; s-wave number; u -Angular position parameter, rad.

[0013] Preferably, a buffer cavity is respectively provided at the upper and lower parts of the partition, and the buffer cavity is closed by an inner liner for storing air to realize thermal insulation function; a flow hole is provided at the center of the partition for connecting the interiors of the two foam metal catalyst beds; a circle of docking holes evenly distributed around the flow hole is provided; the number of docking holes is the same as the number of internal pipe joints in the heat exchange tube group; the docking holes are used to accommodate and dock the internal pipe joints in the two heat exchange tube groups.

[0014] Preferably, a circle of sleeves evenly distributed around the circumference is provided on the shell; the number of sleeves is the same as the number of external pipe joints in the heat exchange tube group; the sleeves are used to wrap the external pipe joints; a circle of first welds evenly distributed around the circumference is provided on the inner liner; the number of first welds is the same as the number of sleeves; each sleeve is inserted into a first weld and sealed and welded thereto; two second welds arranged oppositely are also provided on the inner liner; the second welds are used to wrap the first pipe joints and seal and weld them thereto.

[0015] Preferably, the foam metal catalyst bed is a foam-like porous structure, and a catalyst for producing hydrogen by reforming methanol is attached to the porous matrix.

[0016] Preferably, the reactant raw materials flow into the reaction product from the two first pipe joints in either the upper or lower part of the partition, and flow out of the reaction product from the two first pipe joints in the other part; the heat transfer fluid flows into the outer pipe joint in either the upper or lower part of the partition, and flows out from the outer pipe joint in the other part; the flow direction of the reactant raw materials to the reaction product is opposite to the flow direction of the heat transfer fluid.

[0017] Preferably, the second pipe joint is used to evacuate and seal the space between the shell and the liner for thermal insulation, or the second pipe joint is used to pass a continuously circulating heat-conducting fluid between the shell and the liner for continuous thermal insulation.

[0018] Preferably, the two shells are fixedly connected to the partition plate by a group of bolts and nuts evenly distributed around the circumference.

[0019] Preferably, a compression sleeve is provided between each shell and the partition, and the compression sleeve is compressed by the connection pre-tightening force between the shell and the partition, so that the space surrounded by the compression sleeve, the shell and the partition is filled with air to achieve thermal insulation function.

[0020] Compared with the prior art, the present invention has the following beneficial effects: (1) Under the same volume, the total area of ​​the outer and inner facades of the foam metal catalyst bed of the present invention is increased by 10% to 15% compared with the foam metal catalyst bed of a hollow cylindrical shape, and has a larger contact area, which is conducive to the reaction; (2) The heat exchange tube group adopts a skeleton-type integrated structure, which has more uniform heat transfer characteristics, and compared with the column-type structure, when the foam metal catalyst bed occupies the same size of external space, the volume of the foam metal catalyst bed can be increased by 10% to 15%, and has a larger contact volume, which is conducive to the reaction; (3) The wavy structure of the outer and inner facades on the foam metal catalyst bed of the present invention has better fluid mechanics characteristics, which can increase the disturbance of the reactants in the flow channel, which is conducive to the reaction; (4) The shell and the inner tank are insulated by vacuuming or heat-transfer fluid, so as to ensure that the temperature in the reaction space is uniform and stable, which is more conducive to the thermal reaction. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] Figure 1 It is a schematic diagram of the overall appearance structure of the present invention.

[0022] Figure 2 It is a front view full cross-sectional view of the overall structure of the present invention.

[0023] Figure 3 It is a side full cross-sectional view of the overall structure of the present invention.

[0024] Figure 4It is a structural cross-sectional view of the shell and the inner container of the present invention.

[0025] Figure 5 It is a component structure diagram of the partition of the present invention.

[0026] Figure 6 This is a component structure diagram of the foam metal catalyst bed of the present invention.

[0027] Figure 7 It is a cross-sectional view of the parts of the foam metal catalyst bed of the present invention.

[0028] Figure 8 It is a top view of the parts of the foam metal catalyst bed of the present invention.

[0029] Fig. 9 It is a schematic diagram of the curved surface structure of the outer facade and the inner facade of the present invention.

[0030] Fig.10 It is a parts structure diagram of the heat exchange tube group of the present invention.

[0031] Fig.11 It is a cross-sectional view of the parts of the heat exchange tube group of the present invention.

[0032] Fig.12 It is a structural cross-sectional view of the catalytic component of the present invention.

[0033] In the figure: 1-shell; 2-first pipe joint; 3-partition; 4-compression sleeve; 5-foam metal catalyst bed; 6-second pipe joint; 7-nut; 8-bolt; 9-heat exchange tube group; 10-inner liner; 101-sleeve; 301-buffer cavity; 302-docking hole; 303-flow hole; 501-external facade; 502-inner facade; 503-accommodating hole system; 901-external pipe joint; 902-wave tube; 903-inner pipe joint; 904-tube curve; 1001-first weld; 1002-second weld. DETAILED DESCRIPTION

[0034] The technical solution of the present invention will be further described below in conjunction with the accompanying drawings and through specific implementation methods, wherein the accompanying drawings are only used for exemplary descriptions and represent only schematic diagrams rather than actual drawings, and should not be understood as limiting the present invention; in order to better illustrate the embodiments of the present invention, some parts of the accompanying drawings may be omitted, enlarged or reduced, and do not represent the size of the actual product; for those skilled in the art, it is understandable that some well-known structures and their descriptions in the accompanying drawings may be omitted.

[0035] Figures 1 to 12This is a preferred embodiment of the present invention. In this embodiment, the maximum outer diameter of the device body is 230 mm, and the maximum height of the device body is 155 mm; the bolt 8 is of M12×70; the first pipe joint 2 adopts a four-way pipe diameter; the second pipe joint 6, the outer pipe joint 901 and the inner pipe joint 903 all adopt a two-way pipe diameter.

[0036] like Figure 1 , Figure 2 and Figure 3 As shown, the two shells 1 are fixedly mounted on the upper and lower parts of the partition 3 respectively; the two shells 1 are fixedly connected to the partition 3 by 8 groups of bolts 8 and nuts 7 evenly distributed around the circumference; an inner liner 10 is fixedly mounted between each shell 1 and the partition 3; a group of catalytic components is fixedly mounted between each inner liner 10 and the partition 3; the catalytic component is composed of a foam metal catalytic bed 5 and a heat exchange tube group 9, and adopts an integrated molding process, and the foam metal catalytic bed 5 is attached to the heat exchange tube group 9; the foam metal catalytic bed 5 is a foam-like porous structure, and a catalyst for methanol reforming hydrogen production is attached to its porous matrix. In this embodiment, the catalyst adopts a Cu-Zn-AI-B methanol reforming hydrogen production catalyst; each shell 1 is provided with two oppositely arranged first pipe joints 2, and the first pipe joint 2 connects the space between the inner liner 10 and the partition 3; each shell 1 is also provided with two oppositely arranged second pipe joints 6, and the second pipe joints The head 6 is connected to the space between the shell 1 and the inner liner 10; the second pipe joint 6 is used to evacuate the space between the shell 1 and the inner liner 10 and seal it for thermal insulation, or the second pipe joint 6 is used to pass a continuously circulating heat-conducting fluid between the shell 1 and the inner liner 10 for continuous insulation; the hydrogen production reactant raw materials flow into the reaction product from the two first pipe joints 2 at any part of the upper or lower part of the partition 3, and flow out from the two first pipe joints 2 at the other part; the heat-conducting fluid flows into the outer pipe joint 901 at any part of the upper or lower part of the partition 3, and flows out from the outer pipe joint 901 at the other part; the flow direction of the reactant raw materials to the reaction product is opposite to the flow direction of the heat-conducting fluid; a compression sleeve 4 is provided between each shell 1 and the partition 3, and the compression sleeve 4 is pressed by the connection pre-tightening force between the shell 1 and the partition 3, so that the space surrounded by the compression sleeve 4, the shell 1 and the partition 3 is filled with air to achieve thermal insulation function.

[0037] like Figure 2 , Figure 3 and Figure 4As shown, a circle of sleeves 101 evenly distributed around the circumference is provided on the shell 1; there are 8 sleeves 101; the sleeves 101 are used to wrap the outer pipe joint 901; a circle of first welds 1001 evenly distributed around the circumference is provided on the inner liner 10; the number of first welds 1001 is the same as the number of sleeves 101; each sleeve 101 is inserted into a first weld 1001 and sealed and welded therewith; two second welds 1002 arranged opposite to each other are also provided on the inner liner 10; the second welds 1002 are used to wrap the first pipe joint 2 and seal and weld therewith.

[0038] like Figure 2 , Figure 3 and Figure 5 As shown, a buffer cavity 301 is respectively provided at the upper and lower parts of the partition 3, and the buffer cavity 301 is closed by the inner liner 10 for storing air to realize the function of heat preservation and heat insulation; a flow hole 303 is provided at the center of the partition 3 for connecting the interiors of the two foam metal catalyst beds 5; a circle of docking holes 302 evenly distributed around the circumference is provided around the flow hole 303; there are 8 docking holes 302, and the docking holes 302 are used to accommodate and dock the inner pipe joints 903 in the two heat exchange tube groups 9.

[0039] like Figure 6 , Figure 7 and Figure 8 As shown, the outer side of the foam metal catalyst bed 5 is the outer facade 501; the inner side of the foam metal catalyst bed 5 is the inner facade 502; the accommodating hole system 503 is used to accommodate the heat exchange pipe group 9, such as Fig.12 As shown; both the outer facade 501 and the inner facade 502 are curved surfaces with periodic fluctuations in the circumferential direction and the axial direction; in this embodiment, the outer facade 501 is o - xyz The parametric equation in the space rectangular coordinate system is:

[0040] ;

[0041] Inner facade 502 o - xyz The parametric equation in the space rectangular coordinate system is:

[0042] ;

[0043] In the above formulas, t - angular position parameter, rad; Specifically, the shape structure of the outer facade 501 and the inner facade 502 of this embodiment is as follows Fig. 9 shown.

[0044] like Fig.10 and Fig.11As shown, the wave tube 902 is wavy in the circumferential direction, with 8 wave crests and 8 wave troughs, each wave crest is provided with an outer pipe joint 901, and each wave trough is provided with an inner pipe joint 903; the center line of the wave tube 902 is the tube curve 904, and the tube curve 904 is o - xyz The parametric equation in the space rectangular coordinate system is:

[0045] ;

[0046] In the formula, u - Angular position parameter, rad; in this embodiment, the outer diameter of the wave tube 902 is 6.86 mm.

[0047] Working principle of the present invention: Figure 2 , Figure 2 The dashed arrow in the figure indicates the flow direction of the fluid; Figure 2 The upper outer pipe joint 901 (Inlet of HTF: heat transfer fluid inlet) flows in, Figure 2 The outer pipe joint 901 (Outlet of HTF: heat transfer fluid outlet) at the bottom flows out; the hydrogen production reactant raw materials (methanol and water) flow out from Figure 2 The first pipe joint 2 (Inlet of reactants: reactant raw material inlet) at the bottom flows in and passes through Figure 2 The outer facade 501 and the inner facade 502 of the lower foam metal catalyst bed 5 are Figure 2 The lower inner facade 502 rises internally, passes through the flow hole 303, and enters Figure 2 Inside the upper inner facade 502, and then through Figure 2 The inner facade 502 and the outer facade 501 of the upper foam metal catalyst bed 5 are Figure 2 The space between the upper metal foam catalyst bed 5 and the inner tank 10 is finally formed by Figure 2 The two first pipe joints 2 (Outlet of products) at the top flow out the reaction products (hydrogen and carbon dioxide); in this embodiment, the shell 1 and the inner tank 10 are evacuated and sealed through the second pipe joint 6 for heat insulation.

[0048] The foam metal catalytic bed 5 in the prior art mostly adopts a hollow cylindrical structure, similar to the honeycomb coal structure, and its heat exchange tube group 9 is a plurality of independent straight tubes evenly distributed around the circumference, and the straight tubes are directly inserted into the hollow cylindrical structure. Taking this as a comparative example, it is assumed that the inner diameter of the hollow cylinder is 30 mm and the outer diameter is 90 mm, which are respectively equal to the two base circle diameters of the present embodiment; it is assumed that the height of the hollow cylinder is 62.5 mm, which is the same as the height of the foam metal catalytic bed 5 of the present embodiment; at the same time, it is assumed that the number of straight tubes for accommodation in the hollow cylinder is 8 and the diameter is 2, which is consistent with the number and diameter of the appearance joints and the number and diameter of the inner pipe joints 903 of the present embodiment; further, the embodiment and the comparative example are compared. The total inner and outer surface area and total volume parameters of the foam metal catalyst bed 5 are calculated and compared (accurate to two decimal places): the total inner and outer surface area of ​​the comparative example is about 235.62 cm², and the total volume of the comparative example is about 279.51 cm³; the total inner and outer surface area of ​​the present embodiment is about 260.55 cm², and the total volume of the present embodiment is about 310.17 cm³; compared with the comparative example, the total inner and outer surface area of ​​the present embodiment is increased by about 10.58%, and the total volume is increased by about 10.97%; it can be seen that when the total inner and outer surface area and the total volume are significantly improved, the present invention has a larger contact area and volume compared with the prior art, which is conducive to the reaction.

Claims

1. A methanol reforming hydrogen production reactor, comprising a shell (1), a first pipe joint (2), a partition (3), a catalytic component, a second pipe joint (6), and an inner tank (10), characterized in that: There are two shells (1), which are fixedly mounted on the upper and lower parts of the partition (3) respectively; an inner liner (10) is fixedly mounted between each shell (1) and the partition (3); a group of catalytic components is fixedly mounted between each inner liner (10) and the partition (3); the catalytic components are composed of a foam metal catalytic bed (5) and a heat exchange tube group (9), and adopt an integrated molding process, and the foam metal catalytic bed (5) is attached to the heat exchange tube group (9); each shell (1) is provided with two first pipe joints (2) arranged opposite to each other, and the first pipe joints (2) are connected to the space between the inner liner (10) and the partition (3); each shell (1) is also provided with two second pipe joints (6) arranged opposite to each other, the second pipe joints (6) communicating with the space between the shell (1) and the inner tank (10); the foam metal catalytic bed (5) comprises an outer facade (501), an inner facade (502), and a receiving hole system (503); the outer side surface of the foam metal catalytic bed (5) is the outer facade (501); the inner side surface of the foam metal catalytic bed (5) is the inner facade (502); the receiving hole system (503) is used to receive the heat exchange pipe group (9); the outer facade (501) and the inner facade (502) are both curved surfaces with periodic fluctuations in the circumferential direction and the axial direction, and the curved surfaces are o - xyz The parametric equation in the space rectangular coordinate system is: ； In the formula, R is the base circle radius, mm; A is the fluctuation amplitude, mm; K is the fluctuation frequency; T is the number of z Change period in the axial direction; H-height boundary value, mm; t -Angular position parameter, rad.

2. A methanol reforming hydrogen production reactor as claimed in claim 1, characterized in that: The heat exchange tube group (9) comprises an outer tube joint (901), a wave tube (902), and an inner tube joint (903); the wave tube (902) is wavy in the circumferential direction and has a plurality of wave crests and wave troughs; an outer tube joint (901) is provided on each wave crest, and an inner tube joint (903) is provided on each wave trough.

3. A methanol reforming hydrogen production reactor as claimed in claim 2, characterized in that: The center line of the corrugated tube (902) is the tube curve (904). o - xyz The parametric equation in the space rectangular coordinate system is: ； Where, r-radial distribution radius, mm; h-axial amplitude, mm; s-wave number; u -Angular position parameter, rad.

4. A methanol reforming hydrogen production reactor as claimed in any one of claims 2 to 3, characterized in that: A buffer cavity (301) is respectively arranged at the upper and lower parts of the partition (3); the buffer cavity (301) is closed by an inner liner (10) and is used to store air to achieve a heat preservation and heat insulation function; a flow hole (303) is arranged at the center of the partition (3) and is used to communicate the insides of the two foam metal catalytic beds (5); a circle of docking holes (302) evenly distributed around the circumference is arranged around the flow hole (303); the number of the docking holes (302) is the same as the number of the inner pipe joints (903) in the heat exchange tube group (9); and the docking holes (302) are used to accommodate and dock the inner pipe joints (903) in the two heat exchange tube groups (9).

5. A methanol reforming hydrogen production reactor as claimed in claim 4, characterized in that: The shell (1) is provided with a circle of sleeves (101) evenly distributed around the circumference; the number of the sleeves (101) is the same as the number of the outer pipe joints (901) in the heat exchange tube group (9); the sleeves (101) are used to wrap around the outer pipe joints (901); the inner liner (10) is provided with a circle of first welds (1001) evenly distributed around the circumference; the number of the first welds (1001) is the same as the number of the sleeves (101); each sleeve (101) is inserted into a first weld (1001) and is sealed and welded thereto; the inner liner (10) is also provided with two second welds (1002) arranged opposite to each other; the second welds (1002) are used to wrap around the first pipe joints (2) and are sealed and welded thereto.

6. A methanol reforming hydrogen production reactor as claimed in claim 5, characterized in that: The foam metal catalyst bed (5) is a foam-like porous structure, and a catalyst for producing hydrogen by reforming methanol is attached to the porous matrix.

7. A methanol reforming hydrogen production reactor as claimed in claim 6, characterized in that: The reactant raw materials flow into the reaction product from the two first pipe joints (2) at either the upper part or the lower part of the partition (3), and flow out from the two first pipe joints (2) at the other part; the heat transfer fluid flows into the outer pipe joint (901) at either the upper part or the lower part of the partition (3), and flows out from the outer pipe joint (901) at the other part; the flow direction of the reactant raw materials to the reaction product is opposite to the flow direction of the heat transfer fluid.

8. A methanol reforming hydrogen production reactor as claimed in claim 7, characterized in that: The second pipe joint (6) is used to evacuate and seal the space between the shell (1) and the inner liner (10) for thermal insulation, or the second pipe joint (6) is used to pass a continuously circulated heat-conducting fluid between the shell (1) and the inner liner (10) for continuous thermal insulation.

9. A methanol reforming hydrogen production reactor as claimed in claim 8, characterized in that: A compression sleeve (4) is sleeved between each shell (1) and the partition (3), and the compression sleeve (4) is compressed by a pre-tightening force of the connection between the shell (1) and the partition (3), so that the space surrounded by the compression sleeve (4), the shell (1) and the partition (3) is filled with air, thereby achieving a heat preservation and thermal insulation function.

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