CN205328607U - Be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter - Google Patents
Be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter Download PDFInfo
- Publication number
- CN205328607U CN205328607U CN201521068475.0U CN201521068475U CN205328607U CN 205328607 U CN205328607 U CN 205328607U CN 201521068475 U CN201521068475 U CN 201521068475U CN 205328607 U CN205328607 U CN 205328607U
- Authority
- CN
- China
- Prior art keywords
- converter
- heat
- methanol
- conducting medium
- steam reforming
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The utility model discloses a be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter relates to a MSR hydrogen plant, including the converter casing, be fixed with the conversion tube bank through the converter tube sheet in the converter casing, be equipped with a plurality of baffling boards along the conversion tube bank, and with the converter casing in the intercommunication heat -conducting medium advance, the export, advance with the reaction gas of conversion tube bank intercommunication, the export, still including the feed gas import draft tube of locating the import of reaction gas, be equipped with buffering granule accumulation horizon on the converter tube sheet of reaction gas entrance point, between buffering granule accumulation horizon and feed gas import draft tube, just locate still to be equipped with the scour protection baffle to feed gas import draft tube. The utility model relates to a be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter, especially separate unit productivity exceedes 20000Nm3h.
Description
Technical field
This utility model relates to a kind of MSR device for producing hydrogen, particularly relates to separate unit production capacity more than 20000Nm3The converter of/h。
Background technology
The reformation hydrogen production of hydrocarbon fuel is the main method of current domestic and international industrial hydrogen。Steam reformation is currently used most commonly used hydrogen manufacturing mode, more than half hydrogen of the current whole world is prepared by raw material and steam reformation, at this wherein, methanol-water steam reformation (hereinafter referred to as " MSR ") hydrogen manufacturing because reaction temperature is low, hydrogen product content is high, raw material sources extensively, the first-selection of advantage the becomes hydrogen manufacturing mode such as volumetric hydrogen cost is low。
MSR device for producing hydrogen is when uniform temperature, pressure, with methanol and desalted water for raw material, by the effect of methanol steam reforming catalyst in reactor, promote raw material and steam to carry out conversion reaction inside reformer tube, produce syngas for synthetic ammonia (i.e. hydrogen)。
The principal element affecting MSR hydrogen manufacturing effect has chemistry, two aspects of physics。Chemical factor and catalytic condition；Physical factor then relates to operating condition, and mass-and heat-transfer situation etc., both general performances are in the design quality of reactor。
MSR is highly endothermic process, and the restriction dynamic response of the conventional reactor beaded catalyst heat and mass transfer process because adopting is slow, and beds exists " cold spot ", it is difficult to realize isothermal operation。In order to improve hydrogen production efficiency, each state all goes into overdrive to carry out the research of hydrogen from methyl alcohol reactor。Additionally, along with the expansion of energy demand, Hydrogen Energy demand constantly expands, wherein with Nm up to ten thousand3The product hydrogen scale of/h is in the majority。Because of methanol production capacity surplus, methanol prices low level runs, and namely large-scale schizolysis hydrogen production plant with methanol arises at the historic moment。Converter is the nucleus equipment in schizolysis hydrogen production plant with methanol, and schizonychia larger-scale unit needs the large-scale converter with premium properties as support。
MSR reaction is that methanol completes with water vapor mixture pressurized catalysis cracking and conversion one step in converter, generates hydrogen and carbon dioxide, and its net reaction is as follows:
CH3OH+H2O=CO2+3H2-49.5kJ/mol
This reaction is the endothermic reaction, and reaction institute calorific requirement is provided by conduction oil。Reacting gas, conduction oil the import and export temperature difference, and the temperature difference of conduction oil and reaction gas controls within 15 DEG C, and thus prior art all selects fixed tube-sheet exchanger as overall structure form；Because the temperature difference is only small, it is not necessary to arrange expansion joint and can meet the requirement of thermal (temperature difference) stress。In converter, the required catalyst of reaction needs periodic replacement, and conversion reaction pressure is higher than conduction oil pressure, therefore considers that tube side is made in reaction leave with rage from the angle of heat exchanger technological design, and Catalyst packing is in conversion tube, and conduction oil walks shell side。
The reaction of methanol conversion is reversible reaction, and in course of reaction except primary response, also with the side reaction generating a small amount of hydrocarbon formic acid, dimethyl ether。In order to reduce the generation of side reaction, improve methanol conversion, be necessary for selecting suitable process conditions and optimizing reactor design so that temperature can effectively control, and makes reaction heat energy be rapidly provided, and makes the reaction of methanol conversion can carry out at constant, a controlled temperature。Therefore, methanol conversion is not only a heat exchanger, and the more important thing is that converts an endothermic reaction device, is have chemical kinetics and a thermodynamic (al) equipment。
Fig. 1 is shown in by the converter structure sketch for middle and small scale MSR device for producing hydrogen general at present, and this kind of structure cannot meet extensive MSR device for producing hydrogen needs, and reason is as follows:
1, the uniformity of extensive MSR reaction air inlet cannot be ensured by this structure, existing structure meets the air flow method within diameter 2m, but along with scale becomes big, converter diameter is along with becoming big, this structure air inlet can cause air inlet cannot be evenly distributed in every conversion tube, cause the decline of conversion ratio, have a strong impact on conversion results。
2, for middle and small scale device, converting tube bank adopts " arch " deflection plate can meet requirement, but for large-scale MSR device for producing hydrogen, " arch " deflection plate obviously cannot meet the conversion tube bank requirement such as substantial amounts, device interior flow regime complication。
3, for middle and small scale device, upper lower perforated plate can meet requirement, but reacting for large-scale MSR, device diameters becomes big, and conversion tube increases several times even tens times, hundreds of times, if also adopting the type of attachment of this vessel flange and tube sheet, the equipment tube plate thickness of will result in becomes the increase of geometry multiple, causes the waste of cost, additionally, connection needs also cannot be met。
Utility model content
The purpose of this utility model is in that: providing one for large-scale hydrogen production from methanol-steam reforming device methanol converter, particularly separate unit production capacity is more than 20000Nm3/h。
The purpose of this utility model is realized by following technical proposals:
A kind of for large-scale hydrogen production from methanol-steam reforming device methanol converter, including converter housing, it is fixed with conversion tube bank by converter tube sheet in converter housing, it is provided with some deflection plates along converting tube bank, and enter with the heat-conducting medium connected in converter housing, outlet, the reaction gas connected with conversion tube bank enters, outlet, it is characterized in that: also include being located at the raw material gas inlet guide shell of reaction gas inlet, the converter tube sheet of reaction gas inlet end is provided with buffering settled layer, between buffering settled layer and raw material gas inlet guide shell, just raw material gas inlet guide shell place is additionally provided with erosion control baffle plate。
As selection, raw material gas inlet guide shell is made up of cone cylinder nested inside and outside several, and the unstripped gas that reaction gas inlet enters is divided in some parts of importing converter housings, each cone cylinder is arranged in the same direction, and little and big towards other end opening in converter housing towards reaction gas inlet one end open。
As selection, deflection plate is alternately arranged is formed by circular ring type and the conversion tube bank of collar plate shape deflection plate edge, and wherein circular ring type deflection plate is close to converter inner walls layout, and collar plate shape arrangement of baffles is in the converter housing central authorities hollow position of circular ring type deflection plate relatively。
As selection, heat-conducting medium import and export coil pipe is further respectively had outside converter housing, heat-conducting medium import coil pipe is provided with at least two heat-conducting medium import, heat-conducting medium outlet coil pipe is provided with the outlet of at least two heat-conducting medium, and heat-conducting medium import and export coil pipe connects with in converter housing respectively through some fairleads。
As selection, ring converter inner walls further respectively has heat-conducting medium import and export coil pipe, heat-conducting medium import coil pipe is provided with the heat-conducting medium import outside at least two connection converter housing, heat-conducting medium import coil pipe is additionally provided with some heat-conducting medium intakes connect with in converter housing, heat-conducting medium outlet coil pipe is provided with some heat-conducting medium outlets and connects with in converter housing, and heat-conducting medium outlet coil pipe is additionally provided with the heat-conducting medium outlet outside at least two connection converter housing。
As selection, converter housing includes the fixing converter upper cover of non-dismountable connection from top to bottom, converter cylinder and converter low head, it is respectively fixed with converter tube sheet in the upper and lower end socket inwall of converter, conversion tube bank it is fixed with between the converter tube sheet of the upper and lower end socket of converter, converting the tube bank connection upper and lower end socket of converter, converter supports skirt and is fixed on converter low head lower support fixes whole converter by directly supporting。
As further selection, the upper and lower end socket of converter further respectively has manhole, converter upper cover is additionally provided with reaction gas gas outlet, converter low head is additionally provided with heat-conducting medium discharge port and catalyst discharge port。
As selection, buffering settled layer is made up of on converter tube sheet cushion particle packing。
As further selection, cushion granule is porcelain ball。
It is mean allocation as selection, several cone cylinder arranged concentric of raw material gas inlet guide shell, and the upper and lower opening area between each cone cylinder。
In such scheme, by cone cylinder arranged concentric, by uniform for feed throat area decile。
It is uniformly distributed on heat-conducting medium import and export coil pipe respectively as selection, heat-conducting medium import and export, and fairlead。
As selection, the external diameter of collar plate shape deflection plate is more than or equal to the internal diameter of circular ring type deflection plate。
In such scheme, heat-conducting medium is weave in and out between the circular ring type being alternately arranged and collar plate shape deflection plate, and between the external diameter and the internal diameter of circular ring type deflection plate of collar plate shape deflection plate, size difference is more big, and the flow process of heat-conducting medium is more tortuous, flow process is more long, and heat conduction is more uniform, abundant。
It is uniformly distributed on heat-conducting medium import and export coil pipe respectively as selection, heat-conducting medium import and export, and fairlead。
Aforementioned this utility model main formula case and each further selection scheme thereof can independent assortment to form multiple scheme; it is the scheme that this utility model can adopt and claim: such as this utility model; each selection can select combination in any with other; those skilled in the art can understand there is multiple combination according to prior art and known general knowledge after understanding the present invention program; it is the claimed technical scheme of this utility model, does not do exhaustive at this。
Workflow of the present utility model:
One, the raw material (methanol of technological temperature and pressure condition is met, desalted water) steam from reaction gas inlet through raw material gas inlet guide shell axially to flow in converter housing, in the process, arrange and just the erosion control baffle plate of raw material gas inlet guide shell is stopped, to prevent fluid washing away conversion tube beam tube end。Simultaneously, feed gas is divided into some parts by feed throat area by the cone cylinder of some nestings by raw material gas inlet guide shell, by the guide effect of cone, when water conservancy diversion cone cylinder upper and lower opening area mean allocation, gas flow rate is roughly equal, feeding gas becomes the coniform buffering settled layer surface flowed on converter tube sheet, simultaneously works as distribution of air flow and the effect of uniform gas distribution。Thus avoiding tube sheet surface buffer settled layer to be washed away formation pit, the uneven conversion tube bank catalyst layer that enters of air-flow causes conversion reaction uneven, affects transformation in planta efficiency。
Two, feedstock vapor is by, in restraining even into conversion after raw material gas inlet guide shell and buffering settled layer, converting placement catalyst in tube bank, and unstripped gas passes through to convert the beds in tube bank with certain speed, completes hydrogen production from methanol-steam reforming reaction。Convert tube bank and rely on the two pieces of converter tube sheet support location up and down in the upper and lower end socket of converter。Owing to catalyst amounts is big, converting tube bank quantity many, tube bank weight reaches more than hundreds of ton, shell side heat-conducting medium (conduction oil) weight about tens tons, and these weight undertake and are delivered to converter each through converter tube sheet and support on skirt。This structure vessel flange compared to existing technology and the type of attachment of converter tube sheet, connect more reliable, and converter tube plate thickness also can effectively be reduced。
Three, this converter shell side adopts disk-and-doughnut type deflection plate, and adopting one piece is circular ring type, one piece of deflection plate being alternately arranged for collar plate shape。Owing to converter is relatively large in diameter, adopting disk-and-doughnut type deflection plate more to can guarantee that the uniformity of circumference temperature than segmental baffle, creating good condition thus stably reacting for bed。
Four, MSR reaction is strong endothermic reaction, whole reaction institute calorific requirement all circulates by the heat-conducting medium (conduction oil) of uniform temperature and provides, owing to diameter is big, if conduction oil still adopts single mouth charging, whole heat-conduction oil heat field distribution will certainly be caused uneven, the conversion tube relatively remote apart from heat conductive oil inlet cannot react at optimum temperature, transformation efficiency can be caused substantially to reduce, in order to realize the homogeneous temperature in whole conduction oil temperature field, this patent creatively proposes the new model of a kind of conduction oil " ring-type " charging and discharging。In this equipment, heat-conducting medium import coil pipe around converter housing is positioned at converter top, the uniform a number of fairlead in inner side on heat-conducting medium import coil pipe, directly connect with equipment outer wall, conduction oil flows directly into equipment shell side by these fairleads, turns heat for large number of conversion tube with making the uniform temperature fields that the conduction oil of whole converter shell side sets up。Also have heat-conducting medium outlet coil pipe and fairlead device thereof that a structure is similar in bottom, principle is the same, in opposite direction。
The beneficial effects of the utility model: being that one can be applicable to large-scale hydrogen production from methanol-steam reforming device methanol converter, particularly separate unit production capacity is more than 20000Nm3/h。
Accompanying drawing explanation
The structural representation of the Methanol cluster hydrogen-manufacturing reactor that Fig. 1 commonly uses at present；
In Fig. 1,1 for convert gas outlet, 2 be converter low head, 3 for converter lower part equipment flange, 4 for conduction oil outlet, 5 for " arch " deflection plate, 6 for convert tube bank, 7 for converter cylinder, 8 for air vent, 9 for equipment upper perforated plate, 10 for converter top vessel flange, 11 for converter upper cover, 12 for raw material gas inlet, 13 be heat conductive oil inlet, 14 be converter lower perforated plate。
Fig. 2 is hydrogen production from methanol-steam reforming structure of reactor schematic diagram described in the utility model；
Fig. 3 is the conduction oil ring-type charging principle sketch described in this utility model embodiment 1；
Fig. 4 is the conduction oil equipment inner wall semicircular charging principle sketch described in this utility model embodiment 2；
Fig. 5 is the conduction oil equipment inner wall semicircular discharging principle sketch described in this utility model embodiment 2；
In Fig. 2-5, 1 supports skirt for converter, 2 for converting gas outlet device, 3 is converter low head, 4 export I for conduction oil, 5 for converting tube bank, 6 is deflection plate, 7 is converter cylinder, 8 is heat conductive oil inlet I, 9 is porcelain ball, 10 is converter upper cover, 11 is raw material gas inlet guide shell, 12 is manhole I, 13 is converter upper perforated plate, 14 is gas outlet, 15 is heat conductive oil inlet II, 16 export II for conduction oil, 17 is converter lower perforated plate, 18 is conduction oil unloading port, 19 is manhole II, 20 is catalyst discharge port, 21 is heat conductive oil inlet coil pipe, 22 is fairlead, 23 export coil pipe for conduction oil, 24 is conduction oil intake, 25 is conduction oil outlet。
Detailed description of the invention
Below in conjunction with specific embodiments and the drawings, this utility model is further described。
Comparative example 1:
With reference to shown in Fig. 1, unstripped gas enters converter from its upper side through raw material gas inlet 12, passes sequentially through the equipment conversion tube beds in conversion tube 5 from bottom to top, converts gas outlet 1 from equipment bottom and go out equipment after completing MSR reaction；Owing to MSR reaction is strong endothermic reaction, reaction institute calorific requirement is all circulated by conduction oil and provides, the conduction oil of uniform temperature is from the heat conductive oil inlet 13 access arrangement shell side of its upper side, and it is full of whole shell side, make conversion tube 5 " immersion " in conduction oil, and through " arch " deflection plate 5 (by the large semicircle deflection plate on the large semicircle deflection plate in left side and right side alternately, constitute " arch " runner) water conservancy diversion, in " arch " weave in and out between conversion tube 5, export 4 at conduction oil and be positioned at equipment bottom。
Embodiment 1:
With reference to Fig. 2, shown in 3, in figure, arrow represents heat-conducting medium (conduction oil) and reaction gas flow process, a kind of for large-scale hydrogen production from methanol-steam reforming device methanol converter, including converter housing, it is fixed with conversion tube bank by converter tube sheet in converter housing, be provided with some deflection plates along converting tube bank, and with heat-conducting medium import and export connect in converter housing, restrain, with converting, the reaction gas import and export connected。As shown in this embodiment, converter housing includes non-dismountable connection from top to bottom and fixes the converter upper cover 10 of (such as welding etc.), converter cylinder 7 and converter low head 3, it is fixed with converter upper perforated plate 13 in converter upper cover 7 inwall, it is fixed with converter lower perforated plate 17 in converter low head 3 inwall, conversion tube bank 5 it is fixed with between the upper and lower tube sheet 13,17 of converter, converting tube bank 5 connection converter upper and lower end socket 7,3 inner chamber body, converter supports skirt 1 and is fixed on converter low head 3 lower support fixes whole converter by directly supporting。The upper and lower end socket 7,3 of converter is additionally provided with manhole I 12, II 19, converter upper cover 7 is additionally provided with reaction gas gas outlet 14, converter low head 3 is additionally provided with heat-conducting medium discharge port (conduction oil unloading port 18) and catalyst discharge port 20。
Converter also includes the raw material gas inlet guide shell 11 being located at reaction gas inlet, raw material gas inlet guide shell 11 is made up of the cone cylinder of arranged concentric nested inside and outside several, and it is mean allocation between the upper open area of each cone cylinder and between lower open area, thus feed throat area is divided equally, in order to the unstripped gas that reaction gas inlet enters is divided in some parts of importing converter housings, now each part unstripped gas gas flow rate is roughly equal, each cone cylinder is arranged in the same direction, and it is little and big towards other end opening in converter housing towards reaction gas inlet one end open, flow in converter in order to make feeding gas become coniform；The converter tube sheet (converter upper perforated plate 13) of reaction gas inlet end is provided with buffering settled layer, as selection, as shown in this embodiment, buffering settled layer is deposited on converter tube sheet by porcelain ball 9 and constitutes, in order to buffering further, uniform unstripped gas。Between buffering settled layer and raw material gas inlet guide shell 11, just raw material gas inlet guide shell 11 place being additionally provided with erosion control baffle plate (not shown), the injection of erosion control baffle plate is directly just blocked, cushions and disperses by unstripped gas。
Unstripped gas is entered in converter upper cover 10 by the raw material gas inlet guide shell 11 of reaction gas inlet, then through the buffering further of the stop of erosion control baffle plate and porcelain ball 9, uniform, restrain pipe end on 5 by the conversion of converter upper perforated plate 13 and enter in conversion tube bank 5, react with beds converting in tube bank 5, the conversion 5 times pipe ends of tube bank then passing through converter lower perforated plate 17 go out to convert in tube bank 5 entrance converter low heads 3, and converter discharged by last inverted gas outlet device 2。
The heat conductive oil inlet coil pipe 21 on top and the conduction oil outlet coil pipe 23 of bottom is further respectively had around converter housing, heat conductive oil inlet coil pipe 21 is provided with at least two heat conductive oil inlet and is uniformly distributed (the present embodiment is illustrated as 2: heat conductive oil inlet I 8 and heat conductive oil inlet II 15), conduction oil outlet coil pipe 23 is provided with the outlet of at least two conduction oil and is uniformly distributed (the present embodiment is illustrated as 2: conduction oil outlet I 4 and conduction oil outlet II 16), conduction oil enters, outlet coil pipe 21, 23 connect with in converter housing respectively through some equally distributed fairleads 22。Deflection plate 6 is alternately arranged is formed by circular ring type and collar plate shape deflection plate edge conversion tube bank 5, wherein circular ring type deflection plate is close to converter inner walls layout (forming a ring along inwall), collar plate shape deflection plate and adjacent rings type deflection plate interval certain altitude, it is arranged in converter housing central authorities this hollow position of circular ring type deflection plate relatively, as preferably, the external diameter of collar plate shape deflection plate is more than or equal to the internal diameter of circular ring type deflection plate。
Conduction oil enters heat conductive oil inlet coil pipe 21 by the heat conductive oil inlet I 8 being arranged symmetrically with and heat conductive oil inlet II 15, enter the converter shell side converted between tube bank 5 from converter upper perforated plate 13 one end again through some uniform fairleads 22, then along converting tube bank 5 directions by deflection plate 6 water conservancy diversion, " 8 font " flow process is formed through the outer of the outer circular ring type deflection plate hollow area collar plate shape deflection plate of collar plate shape deflection plate, finally go out converter shell side from some fairleads 22 of converter lower perforated plate 17 one end and enter conduction oil outlet coil pipe 23, finally go out device from conduction oil outlet I 4 and conduction oil outlet II 16。
Embodiment 2:
With reference to Fig. 4, shown in 5, the present embodiment is substantially the same manner as Example 1, it is distinctive in that: ring converter inner walls is respectively equipped with conduction oil and enters, outlet coil pipe 21, 23 (being preferably a cross section is the loop pipe of semicircle), heat conductive oil inlet coil pipe 21 is provided with the heat conductive oil inlet (the present embodiment is illustrated as 2: heat conductive oil inlet I 8 and heat conductive oil inlet II 15) outside at least two connection converter housing, heat conductive oil inlet coil pipe 21 is additionally provided with some conduction oil intakes 24 connect with in converter housing, conduction oil outlet coil pipe 23 is provided with some conduction oil outlets 25 and connects with in converter housing, conduction oil outlet coil pipe 23 is additionally provided with the conduction oil outlet (the present embodiment is illustrated as 2: conduction oil outlet I 4 and conduction oil outlet II 16) outside at least two connection converter housing。
The foregoing is only preferred embodiment of the present utility model, not in order to limit this utility model, all any amendment, equivalent replacement and improvement etc. made within spirit of the present utility model and principle, should be included within protection domain of the present utility model。
Claims (10)
1. one kind is used for large-scale hydrogen production from methanol-steam reforming device methanol converter, including converter housing, it is fixed with conversion tube bank by converter tube sheet in converter housing, it is provided with some deflection plates along converting tube bank, and enter with the heat-conducting medium connected in converter housing, outlet, the reaction gas connected with conversion tube bank enters, outlet, it is characterized in that: also include being located at the raw material gas inlet guide shell of reaction gas inlet, the converter tube sheet of reaction gas inlet end is provided with buffering settled layer, between buffering settled layer and raw material gas inlet guide shell, just raw material gas inlet guide shell place is additionally provided with erosion control baffle plate。
2. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterized in that: raw material gas inlet guide shell is made up of cone cylinder nested inside and outside several, and the unstripped gas that reaction gas inlet enters is divided in some parts of importing converter housings, each cone cylinder is arranged in the same direction, and little and big towards other end opening in converter housing towards reaction gas inlet one end open。
3. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterized in that: deflection plate is alternately arranged is formed by circular ring type and the conversion tube bank of collar plate shape deflection plate edge, wherein circular ring type deflection plate is close to converter inner walls layout, and collar plate shape arrangement of baffles is in the converter housing central authorities hollow position of circular ring type deflection plate relatively。
4. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterized in that: outside converter housing, further respectively have heat-conducting medium import and export coil pipe, heat-conducting medium import coil pipe is provided with at least two heat-conducting medium import, heat-conducting medium outlet coil pipe is provided with the outlet of at least two heat-conducting medium, and heat-conducting medium import and export coil pipe connects with in converter housing respectively through some fairleads。
5. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterized in that: ring converter inner walls further respectively has heat-conducting medium and enters, outlet coil pipe, heat-conducting medium import coil pipe is provided with the heat-conducting medium import outside at least two connection converter housing, heat-conducting medium import coil pipe is additionally provided with some heat-conducting medium intakes connect with in converter housing, heat-conducting medium outlet coil pipe is provided with some heat-conducting medium outlets and connects with in converter housing, heat-conducting medium outlet coil pipe is additionally provided with the heat-conducting medium outlet outside at least two connection converter housing。
6. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterized in that: converter housing includes the fixing converter upper cover of non-dismountable connection from top to bottom, converter cylinder and converter low head, it is respectively fixed with converter tube sheet in the upper and lower end socket inwall of converter, conversion tube bank it is fixed with between the converter tube sheet of the upper and lower end socket of converter, converting the tube bank connection upper and lower end socket of converter, converter supports skirt and is fixed on converter low head lower support fixes whole converter by directly supporting。
7. as claimed in claim 6 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterized in that: the upper and lower end socket of converter further respectively has manhole, converter upper cover is additionally provided with reaction gas gas outlet, converter low head is additionally provided with heat-conducting medium discharge port and catalyst discharge port。
8. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterised in that: buffering settled layer is made up of on converter tube sheet cushion particle packing。
9. as claimed in claim 1 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterised in that: several cone cylinder arranged concentric of raw material gas inlet guide shell, and the upper and lower opening area between each cone cylinder is mean allocation。
10. as claimed in claim 3 for large-scale hydrogen production from methanol-steam reforming device methanol converter, it is characterised in that: the external diameter of collar plate shape deflection plate is more than or equal to the internal diameter of circular ring type deflection plate。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521068475.0U CN205328607U (en) | 2015-12-18 | 2015-12-18 | Be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521068475.0U CN205328607U (en) | 2015-12-18 | 2015-12-18 | Be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205328607U true CN205328607U (en) | 2016-06-22 |
Family
ID=56208356
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201521068475.0U Active CN205328607U (en) | 2015-12-18 | 2015-12-18 | Be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205328607U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111864240A (en) * | 2020-08-23 | 2020-10-30 | 浙江工业大学 | Small-size methanol reforming hydrogen plant |
| CN116832713A (en) * | 2023-09-02 | 2023-10-03 | 杭州普菲科空分设备有限公司 | Methanol hydrogen production converter convenient for replacing catalyst |
-
2015
- 2015-12-18 CN CN201521068475.0U patent/CN205328607U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111864240A (en) * | 2020-08-23 | 2020-10-30 | 浙江工业大学 | Small-size methanol reforming hydrogen plant |
| CN111864240B (en) * | 2020-08-23 | 2024-04-02 | 浙江工业大学 | Small-size methyl alcohol reforming hydrogen plant |
| CN116832713A (en) * | 2023-09-02 | 2023-10-03 | 杭州普菲科空分设备有限公司 | Methanol hydrogen production converter convenient for replacing catalyst |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108404821B (en) | Energy-saving efficient radial methanol reactor | |
| US8936656B2 (en) | Hydrogen generator using steam-reforming reaction | |
| CN104001457B (en) | A kind of methanation fluidized-bed reactor | |
| AU2018446829B2 (en) | Large-scale ethylene glycol reactor | |
| US4359448A (en) | Fluidized bed reactor for exothermic reactions | |
| CN205328607U (en) | Be used for large -scale for methanol steam reforming hydrogen plant methyl alcohol converter | |
| CN102274707A (en) | Slurry reactor used for producing liquid fuel | |
| CN100579643C (en) | By-product steam combined axial flow gas-solid phase fixed bed catalyst chamber | |
| JP5188895B2 (en) | Methanol synthesis reactor and methanol synthesis method | |
| CN203075923U (en) | Axial-radial constant-temperature conversion reactor | |
| CN104549063A (en) | Fluidized bed reactor | |
| CN105833804A (en) | Steam rising type radial-flow reactor | |
| CN108905906A (en) | A kind of axial-radial flow reactor | |
| CN109294627B (en) | Isothermal conversion device and synthesis gas complete conversion reaction system comprising same | |
| CN105413591A (en) | Multi-section type heat insulation fixed bed reactor for PX production | |
| CN103920429A (en) | Axial-radial fixed bed methanation reactor | |
| CN213254347U (en) | Tube array reactor with flow guide | |
| CN208810012U (en) | A kind of controllable heat tranferring radial direction isothermal reactor of ring pipe | |
| CN204469677U (en) | A kind of adopting heat pipes for heat transfer radial bed methanator | |
| CN208389980U (en) | Beam tube water bed type ethylene glycol hydrogenator | |
| CN208389982U (en) | A kind of energy-saving and high efficient radial direction methanol reactor | |
| CN202403563U (en) | Spiral tube heat exchanger | |
| CN202752008U (en) | Gas phase hydrogenation reactor | |
| CN201186210Y (en) | Vertical type water-cooling tube box type reactor | |
| CN106495098B (en) | A kind of catalytically reforming hydrogen producing apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: No. 5, gaon Boulevard, high tech Zone, Chengdu, Sichuan Province Patentee after: Sichuan Yalian Hydrogen Energy Technology Co.,Ltd. Address before: 4F, Block B, No. 5 Gaopeng Avenue, High tech Zone, Chengdu, Sichuan 610041 Patentee before: ALLY HI-TECH Co.,Ltd. |
|
| CP03 | Change of name, title or address |