CN109694037A - The method of reforming hydrogen-preparation reactor, reformation hydrogen production reburner and reformation hydrogen production reaction - Google Patents
The method of reforming hydrogen-preparation reactor, reformation hydrogen production reburner and reformation hydrogen production reaction Download PDFInfo
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- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
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- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
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- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
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- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
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- C01B2203/14—Details of the flowsheet
- C01B2203/141—At least two reforming, decomposition or partial oxidation steps in parallel
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Abstract
This disclosure relates to a kind of method of reforming hydrogen-preparation reactor, reformation hydrogen production reburner and reformation hydrogen production reaction.The reforming hydrogen-preparation reactor and reformation hydrogen production reburner use micro- catalysis reaction plate, load has catalytic active component on reaction plate, reduce catalytically-active metals dosage and catalyst is not easy carbon distribution inactivation, shortens the distance that reaction gas diffuses to catalytic active center, resistance to mass tranfer and reactor pressure decrease are reduced, hydrogen production reaction conversion ratio is improved；Reaction gas is flowed by center outward in the reactor, and flow area, which is gradually increased, reacts plate temperature gradually rises, and is increased advantageous as volume and the promotion of the hydrogen production reaction conversion ratio of the endothermic reaction；The reactor use scope is wide, and the boiler tube as hydrogen manufacturing conversion furnace can be adapted for different types of reburner.Low using the hydrogen production process boiler tube pressure drop of the reformation hydrogen production reburner, per volume of catalyst in boiler tube product space-time yield height, unstripped gas processing capacity energy high conversion rate, can satisfy hydrogen production reaction requirement.
Description
Technical field
This disclosure relates to reformation hydrogen production field, and in particular, to a kind of reforming hydrogen-preparation reactor, reformation hydrogen production reburner and
The method of reformation hydrogen production reaction.
Background technique
Hydrogen is not only important industrial chemicals and a kind of clean fuel.Hydrogen is in modern industry, especially petroleum
It is played an increasingly important role in the national economy such as work industry, fuel cell.In the continuous heaviness of global crude oil, in poor quality
Trend is aggravated and people are continuously increased clear gusoline quantity demand, quality standard is constantly promoted, and environmental legislation is constantly stringent
Multiple pressure under, it is also increasing to hydrogen demand, and then higher requirements are also raised to device for producing hydrogen.
Process for making hydrogen mainly has water electrolysis method, light hydrocarbon steam conversion method, partial oxidation process and methanol decomposition method etc., at present
With being most widely light hydrocarbon steam conversion method.The raw material of light hydrocarbon steam conversion method hydrogen manufacturing is with natural gas, naphtha, refinery
Based on the carbon containing light hydrocarbons such as gas.Its conversion process are as follows: light hydrocarbons and water vapour are in certain temperature, pressure and catalyst
It reacts under effect, generates hydrogen and carbon monoxide, carbon monoxide further generate hydrogen using water gas shift reaction,
Further increase light hydrocarbons purpose product yield.
The main chemical reactions occurred in hydrogen-making reaction procedure have:
Conversion reaction CnHm+n H2O→n CO+(n+m/2)H2△ H=206kJ/mol
Conversion reaction CO+H2O→CO2+H2△ H=-36kJ/mol
Conversion reaction is a strong endothermic reaction, in traditional SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE, by fuel combustion, will be filled with conversion and urges
The reformer tube of agent is heated to 900~1000 DEG C of progress hydrogen production reactions.Common reformation hydrogen production active component have Pt, Pd, Ir,
Rh DengV Ш race transition elements limits industrial application due to its price height.Reformation hydrogen production industrial application is the most extensive at present
Active component be nickel.Catalyst activity height is directly related with catalyst specific surface axial extent, and in contrast, specific surface is got over
Greatly, the dispersion degree of active component is better, and activated centre number is more, to improve the catalytic activity of catalyst.
Existing hydrogen manufacturing conversion furnace loads the nickel-base catalyst of certain granules size, shape in boiler tube, often will appear
Filling is uneven, causes unstripped gas bias current, causes feed stock conversion low, and the easy carbon distribution inactivation of catalyst reduces the operation week of device
Phase.In addition, the lesser catalyst of loaded particles size in boiler tube increases catalyst although the loadings of catalyst can be improved
Activated centre number improves the processing capacity and conversion ratio of raw material to a certain extent, is disadvantageous in that catalyst size is got over
Small, boiler tube pressure drop is bigger, increases the energy consumption of feed gas compressor.
Summary of the invention
Purpose of this disclosure is to provide a kind of reforming hydrogen-preparation reactor, reformation hydrogen production reburner and reformation hydrogen production reaction sides
Method, the pressure drop of the reburner of the reforming hydrogen-preparation reactor and use reforming hydrogen-preparation reactor are low, existing without gas bias current and short circuit
As；Using the method high conversion rate of the reformation hydrogen production reburner.
To achieve the goals above, the first aspect of the disclosure provides a kind of reforming hydrogen-preparation reactor, which includes
Cylinder-shaped seal and pressure bearing shell, air inlet, gas outlet, the first straight tube for extending into from the case top enclosure interior, from institute
Housing bottom is stated to extend into the second straight tube of enclosure interior and be arranged in the shell described second below first straight tube
Radial catalytic reaction zone above straight tube；The air inlet is connected to first straight tube, and the gas outlet is straight with described second
Pipe connection；The radial direction catalytic reaction zone is sealed by top sealing plate and sealed bottom plate respectively up and down, the top sealing
The edge of plate and the inner walls are tightly connected, and the radial direction catalytic reaction zone includes central tube and is set in outside central tube
At least one sleeve；Central tube has central tube, and central tube passes through top sealing plate and the first straight tube is in fluid communication；Central tube
Cushion chamber is respectively formed between lateral wall and the inner sidewall of innermost layer sleeve and between the barrel of adjacent sleeve；It is outermost
Annular space is formed between the lateral wall of sleeve and the inner wall of shell；The side wall of the central tube, central tube and sleeve is respectively formed
There is aperture area, so that the central tube is connected to by the aperture area with the annular fluid；The radial direction catalytic reaction zone
Air collecting chamber is formed between sealed bottom plate and the inner wall of the lower part of the housing, the air collecting chamber is connected to the annular fluid；
Micro- catalysis reaction plate is respectively equipped in the central tube and the sleeve, the edge point of micro- catalysis reaction plate in the central tube
It is not tightly connected with the top sealing plate, sealed bottom plate, central tube tube wall and center medial wall of the tube, it is micro- in the sleeve
The edge of catalysis reaction plate is respectively between the inner sidewall and lateral wall of the top sealing plate, sealed bottom plate and the sleeve
It is tightly connected, the plate face load of micro- catalysis reaction plate has reforming hydrogen-production catalyst.
Optionally, micro- catalysis reaction plate in the central tube radially distributes around the central tube；The sleeve
Interior micro- catalysis reaction plate radially distributes around the central tube.
Optionally, micro- catalysis reaction plate is selected from least one of surface plate, castellated plates, corrugated plating and corrugated sheet.
Optionally, the micro- catalysis reaction plate of supplement is additionally provided in the central tube and/or in the sleeve, the supplement is micro- to urge
Change reaction plate and micro- catalysis reaction plate alternate intervals are arranged, the plate face load of the micro- catalysis reaction plate of supplement has reformation to make
Hydrogen catalyst；The ratio between the radial width of micro- catalysis reaction plate and the micro- catalysis reaction plate of the supplement is greater than 1.5；The supplement
The edge of micro- catalysis reaction plate is connect with the inner seal of the top sealing plate, sealed bottom plate, central tube barrel respectively；Or
The edge of person, the micro- catalysis reaction plate of supplement are close with the top sealing plate, sealed bottom plate, the inside of sleeve outer wall respectively
Envelope connection.
Optionally, the number of the sleeve is 1~500, and the sleeve, central tube, central tube and shell are in coaxial side
Formula arrangement.
The second aspect of the disclosure provides a kind of reformation hydrogen production reburner, including air inlet pipe, escape pipe, burner and burning
Room, the reburner further include the reforming hydrogen-preparation reactor of disclosure first aspect, and the reforming hydrogen-preparation reactor is located at the combustion
Interior is burnt, the air inlet of the reforming hydrogen-preparation reactor is connected to the air inlet pipe, the gas outlet of the reforming hydrogen-preparation reactor
It is connected to the escape pipe.
The third aspect of the disclosure provides anti-using the reformation hydrogen production reburner progress reformation hydrogen production of disclosure second aspect
The method answered is fired method includes the following steps: (1) makes fuel gas and air spray into the combustion chamber by the burner
It burns；(2) so that unstripped gas and vapor is entered the reforming hydrogen-preparation reactor through the air inlet pipe of the reburner, urged in the radial direction
Change and carry out reformation hydrogen production reaction in reaction zone, obtains the conversion gas rich in hydrogen.
Optionally, it is 700~1100 DEG C that the condition of the reformation hydrogen production reaction, which includes: reaction temperature, reaction pressure 1.8
~5.5MPaG, the H in vapor2The molar ratio of carbon atom in O and unstripped gas is (2.5~5): 1, air speed is 1000~
100000h-1。
Optionally, the unstripped gas passes through the mean flow rate at the central tube and the sleeve radial width half
For 0.3~90m/s.
Optionally, the unstripped gas is natural gas, liquefied petroleum gas, refinery gas, the resolution gas and stone for reforming hydrogen concentrate PSA
At least one of cerebrol；The reformation hydrogen production catalysts include reformation hydrogen production active component, the reformation hydrogen production activity
Component includes at least one of nickel, ruthenium, platinum, palladium, iridium and rhodium.
Compared with prior art, the invention has the benefit that
(1) catalytic reaction zone of reforming hydrogen-preparation reactor is the radial reaction zone being made of micro- catalysis reaction plate, reaction plate
It is upper to load the catalytic active component for having hydrogen production reaction, distance contracting of the reaction gas from gas phase main diffusion to catalytic active center
It is short, it greatly reduces resistance to mass tranfer (diffusional resistance is almost nil), while the product generated can be diffused into bodies of fluid quickly,
The residence time is shorter in the reactor for product, fundamentally improves the transformation efficiency of hydrogen production reaction, reaches and improves unit catalysis
The purpose of agent product space-time yield.
(2) reaction gas is uniformly distributed into radial reaction zone from central tube and flows from inside to outside, and flow area is gradually
Increase, it is mobile to product direction to be conducive to the increased hydrogen production reaction of volume.In addition, as reaction stream flows from inside to outside, outside
Layer it is micro- catalysis reaction plate temperature be higher than the micro- catalysis reaction plate of internal layer, the temperature highest of micro- catalysis reaction plate at annular space,
Since hydrogen production reaction is an endothermic reaction, be conducive to the progress of hydrogen production reaction.
(3) compared with the reforming hydrogen-preparation reactor of loaded particles shape, using micro- catalysis reaction plate, activity used in reactor
Total metal content significantly reduces, pressure drop is low.Under the conditions of same treatment scale, the reforming hydrogen-preparation reactor of the disclosure and it is made of it
Reburner equipment size it is more traditional small by 5%~30%, pressure drop low 3%~55%.
(4) compared with the reforming hydrogen-preparation reactor of loaded particles shape, micro- catalysis of the reforming hydrogen-preparation reactor of the disclosure is anti-
Plate is answered to be not easy carbon distribution inactivation, long service life, pressure drop is low, and bed pressure drop is low compared with the reactor of same treating capacity (15%~90%)；
(5) catalytic reaction zone is made of micro- catalysis reaction plate, is increased activated centre quantity, is improved reaction gas and urging
The uniformity for changing chain carrier, avoids the occurrence of reaction dead zone and gas Biased flow phenomenon, can fully ensure that whole service week
Even running in phase.
(6) different types of reburner can be suitable for as reformation hydrogen production reformer tube, use scope is wide, and can root
Control and tune are reached by the integration mode of the sleeve with functionalization and the increase and decrease of quantity according to actual demand of industrial production
Section production, is advantageously implemented the maximum utilization efficiency of equipment, without obvious enlarge-effect, while shortening the process time of equipment, into
One step reduces reactor production cost.
Other feature and advantage of the disclosure will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Attached drawing is and to constitute part of specification for providing further understanding of the disclosure, with following tool
Body embodiment is used to explain the disclosure together, but does not constitute the limitation to the disclosure.In the accompanying drawings:
Fig. 1 is a kind of structural schematic diagram of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Fig. 2 is a kind of cross-sectional view (the i.e. face A-A in Fig. 1 of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure
Cross-sectional view)；
Fig. 3 is the cross-sectional view of another specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Fig. 4 is the cross-sectional view of the third specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Fig. 5 is the cross-sectional view of the 4th kind of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Fig. 6 is the cross-sectional view of the 5th kind of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Fig. 7 is the structural schematic diagram of the 6th kind of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Fig. 8 is cross-sectional view (the i.e. face A-A in Fig. 7 of the 6th kind of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure
Cross-sectional view)；
Fig. 9 is a kind of structure of the micro- catalysis reaction plate of the tooth form of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure
Schematic diagram；
Figure 10 is a kind of knot of the micro- catalysis reaction plate of the ripple of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure
Structure schematic diagram；
Figure 11 is a kind of knot of the micro- catalysis reaction plate of the waveform of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure
Structure schematic diagram；
Figure 12 is a kind of structural schematic diagram of specific embodiment of the reformation hydrogen production reburner of the disclosure；
Figure 13 is the structural schematic diagram of another specific embodiment of the reformation hydrogen production reburner of the disclosure；
Figure 14 is a kind of central tube schematic diagram of specific embodiment of the reforming hydrogen-preparation reactor of the disclosure；
Figure 15 is the central tube schematic diagram of another specific embodiment of the reforming hydrogen-preparation reactor of the disclosure.
Description of symbols
1 air inlet, 2 gas outlet
3 upper cover, 4 lower head
5 top sealing plate, 6 central tube
7 annular space, 8 sealed bottom plate
The micro- catalysis reaction plate of 9 air collecting chamber 10
11 first straight tube, 12 shell
13 central tube, 14 second straight tube
15 sleeve, 16 cushion chamber
The 17 micro- 20 reformation hydrogen production reburners of catalysis reaction plate of supplement
21 reforming hydrogen-preparation reactor, 22 combustion chamber
23 burner, 24 air inlet pipe
25 escape pipes.
Specific embodiment
It is described in detail below in conjunction with specific embodiment of the attached drawing to the disclosure.It should be understood that this place is retouched
The specific embodiment stated is only used for describing and explaining the disclosure, is not limited to the disclosure.
In the disclosure, in the absence of explanation to the contrary, the noun of locality used such as " upper and lower, top, bottom " is usually
Refer to upper and lower, top and bottom of the device under normal operating condition, can specifically refer to the page of Fig. 1." inside and outside "
It is for the profile of device itself.In addition, term " first ", " second " are used for description purposes only, and should not be understood as
Indication or suggestion relative importance or the quantity for implicitly indicating indicated technical characteristic." first ", " are defined as a result,
Two " feature can explicitly or implicitly include one or more of the features.In the description of the disclosure, " multiples' "
It is meant that two or more, unless otherwise specifically defined.
As shown in Figure 1, the first aspect of the disclosure provides a kind of reforming hydrogen-preparation reactor, which includes cylinder-shaped close
Envelope pressure-bearing shell 12, air inlet 1, gas outlet 2, the first straight tube 11 for extending at the top of shell 12 enclosure interior, from shell 12
Bottom extend into the second straight tube 14 of enclosure interior and second straight tube, 14 top below first straight tube 11 is arranged in shell 12
Radial catalytic reaction zone；Air inlet is connected to the first straight tube 11, and gas outlet 2 is connected to the second straight tube 14；Radial catalytic reaction zone
Sealed respectively by top sealing plate 5 and sealed bottom plate 8 up and down, the edge of top sealing plate 5 and the sealing of 12 inner wall of shell connect
It connects, radial catalytic reaction zone includes central tube 13 and at least one sleeve 15 being set in outside central tube 13；Central tube 13 has
There is central tube 6, central tube 6 passes through top sealing plate 5 and the first straight tube 11 is in fluid communication；Central tube lateral wall and innermost layer sleeve
Inner sidewall between and the barrel of adjacent sleeve 15 between be respectively formed with cushion chamber 16；The lateral wall of outermost sleeve 15
Annular space 7 is formed between the inner wall of shell 12；The side wall of central tube 6, central tube 13 and sleeve 15 is respectively formed with aperture, with
Central tube 6 is in fluid communication by aperture and annular space 7；The sealed bottom plate 8 of radial catalytic reaction zone is interior with 12 lower part of shell
Air collecting chamber 9 is formed between wall, air collecting chamber 9 and annular space 7 are in fluid communication；It is anti-that micro- catalysis is respectively equipped in central tube 13 and sleeve 15
Answer plate 10, the edge of micro- catalysis reaction plate 10 in central tube 13 respectively with top sealing plate 5, sealed bottom plate 8, central tube 6
Tube wall and 13 inner sidewall of central tube are tightly connected, the edge of micro- catalysis reaction plate 10 in sleeve 15 respectively with top sealing plate 5,
It is tightly connected between sealed bottom plate 8 and the inner sidewall and lateral wall of sleeve 15, the plate face load of micro- catalysis reaction plate has reformation
Catalyst for preparing hydrogen.
The reforming hydrogen-preparation reactor of the disclosure uses micro- catalysis reaction plate, work needed for load has hydrogen production reaction on reaction plate
Property component, reduce catalytically-active metals dosage and catalyst be not easy carbon distribution inactivation, shorten reaction gas diffuse to catalysis live
The distance at property center, reduces resistance to mass tranfer and reactor pressure decrease, improves hydrogen production reaction conversion ratio；Reaction gas is in reactor
In flowed outward by center, flow area, which is gradually increased, reacts plate temperature gradually rises, and increases advantageous as volume and absorbs heat
The promotion of the hydrogen production reaction conversion ratio of reaction；The reforming hydrogen-preparation reactor use scope is wide, and the boiler tube as hydrogen manufacturing conversion furnace can
To be suitable for different types of reburner.
The reforming hydrogen-preparation reactor of disclosure meaning is usually also referred to as HK-40 Tube at Hydrogen Reformer or reburner in the industrial production
Pipe, in no special instruction, three of the above address indicates identical device.According to the disclosure, micro- catalysis reaction plate can
To have reforming hydrogen-production catalyst in optional plate face load, can also load in two plate faces of micro- catalysis reaction plate has
Reforming hydrogen-production catalyst, preferably two equal supported catalysts of plate face carry out turning for hydrogen production reaction to further increase reactor
Rate.Reforming hydrogen-production catalyst can use catalytic active component well-known to those skilled in the art, such as the activity of load
Component can be the metals such as nickel, ruthenium, platinum, palladium, iridium and rhodium with reformation hydrogen production reactivity；The load, which refers to, to lead to
The methods of dipping, ion sputtering, coating or filling is crossed to load to active component by the catalyst containing active component or directly
On micro- catalysis reaction plate.Wherein, active metal component coating loading process can use packet well-known to those skilled in the art
Include the coating method in two stages of pretreatment and catalyst deposit of metallic matrix.
According to the disclosure, micro- catalysis reaction plate 10 can be along reactor axis to being extended or micro- catalysis reaction plate 10
Extending direction and horizontal direction be in angle theta, θ can be greater than 0 ° and be not more than 90 ° in the range of, preferably 30 ° of θ≤90 ° <；
It is preferred that micro- catalysis reaction plate 10 along reactor axis to be extended.It may include one or more micro- in central tube 13 and sleeve 15
It is catalyzed reaction plate 10, multiple micro- catalysis reaction plates 10 can be arranged in central tube 13 or sleeve 15 by the usual manner of this field
Cloth, as long as guaranteeing reactor feed gas in central tube 13 and sleeve 15 respectively from center radial motion around.In order into
One step reduces reactor pressure decrease, adapts to the characteristics of hydrogen production reaction volume increases, in a kind of specific embodiment of the disclosure, such as
Shown in Fig. 2, Fig. 3, Fig. 4, micro- catalysis reaction plate 10 in central tube 13 can radially distribute around central tube 6；Sleeve 15
Interior micro- catalysis reaction plate 10 can radially distribute around central tube 13.It is further preferred that micro- catalysis reaction plate 10 can
With around central tube 13 or central tube 6 is radial is uniformly distributed.In other embodiments, micro- catalysis reaction plate 10 can be put down
Row interval distribution.
In order to further increase the catalytic active center quantity in reforming reactor, improve hydrogen production reaction conversion ratio, at this
In a kind of disclosed specific embodiment, as shown in Figure 5 and Figure 6, supplement is also provided in central tube 13 and/or in sleeve 15
Micro- catalysis reaction plate 17 supplements micro- catalysis reaction plate 17 and is arranged with micro- catalysis reaction plate 10 interval, supplements micro- catalysis reaction plate 17
Plate face load have reforming hydrogen-production catalyst；Micro- catalysis reaction plate 17 is supplemented to be preferably disposed in central tube 13 and/or sleeve 15
Close to the side of shell, there is enough catalytic active center density to guarantee flow of feed gas upwards；Supplement micro- catalysis reaction plate
17 size can change in a big way, it is preferable that micro- catalysis reaction plate 10 and the radial direction for supplementing micro- catalysis reaction plate 17
The ratio between width can be greater than 1.5, to guarantee the catalytic active center concentration for being suitable in catalytic reaction zone；Supplement in central tube 13
It is micro- catalysis reaction plate 17 edge can respectively with top sealing plate 5, sealed bottom plate 8,13 barrel of central tube inner seal
Connection；In sleeve 15 supplement it is micro- catalysis reaction plate 17 edge can respectively with top sealing plate 5, sealed bottom plate 8, sleeve
The inner seal of 15 outer walls connects.
According to the disclosure, reforming hydrogen-preparation reactor use loads the micro- catalysis reaction plate 10 for having reforming hydrogen-production catalyst and can
Selection of land supplements micro- catalysis reaction plate 17 and can reduce catalytically-active metals dosage, reduce reactor size, reduce reactor pressure decrease,
Wherein micro- catalysis reaction plate 10 can be this field conventional kind.Catalytic active center number in reactor in order to further increase
Mesh, it is preferable that micro- catalysis reaction plate 10 can be selected from least one of surface plate, castellated plates, corrugated plating and corrugated sheet, such as
Shown in Fig. 2, Fig. 9, Figure 10, Figure 11, more preferably in castellated plates (Fig. 9), corrugated plating (Figure 10) and corrugated sheet (Figure 11) at least
It is a kind of.Wherein the structure snd size of castellated plates, corrugated plating and corrugated sheet with no restrictions, as long as meet load active component, meet
The requirement of process for making hydrogen condition.Micro- catalysis reaction plate number is loaded in catalytic reaction zone in order to improve, in reactor preferably
The same micro- catalysis reaction plate of type.Further, for the ease of producing, installing micro- catalysis reaction plate, while original is uniformly distributed
Expect gas, each piece of micro- catalysis tooth waveform size of reaction plate, type, density degree etc. are answered completely the same, and the present invention is to tooth form
Size waveforms, type, density degree are not particularly limited, as long as meeting hydrogen production reaction process conditions.
According to the disclosure, under identical reaction condition and reactor diameter, the quantity for increasing sleeve 15 can increase instead
The contact probability for answering gas and catalyst improves the effect of conversion ratio.Sleeve 15 can be adjusted according to real reaction situation
Quantity, such as the quantity of sleeve 15 can be 1~500, preferably 1~150, further preferably 1~50.In order to mention
High reaction raw materials distribution consistency degree, it is preferable that sleeve 15, central tube 13, central tube 6 and shell 12 are arranged in coaxial manner.
According to the disclosure, the relative size of central tube 13, sleeve 15 and central tube 6 can change in a big way, in
The diameter of heart cylinder 13 and the diameter ratio and the diameter of central tube 13 and the diameter ratio of sleeve 15 of central tube 6 all can be fit
Any ratio closed；Sleeve 15 and central tube 13 can have identical height in the axial direction.Center in central tube 13
Pipe 6 can be open-celled structure, and the form of aperture can be circular hole as shown in figure 15 or groove profile as shown in figure 14, aperture
Shape, aperture size, aperture how many (percent openings) are of the invention with no restrictions, as long as meeting reforming hydrogen producing process condition.
According to the disclosure, in order to extend the service life of micro- catalysis reaction plate, central tube 6, micro- catalysis reaction plate can be adopted
With metal material, ceramic material, it is preferred to use the metal material not reacted with the gas in reaction system.
According to the disclosure, the material that the shell of reforming hydrogen-preparation reactor, upper lower head use can be with conventional reformation hydrogen manufacturing
The material of boiler tube selection is identical, such as: HP-40Nb, reforming hydrogen-preparation reactor shell material are well known to those skilled in the art
, the present invention repeats no more.The specific size of reforming hydrogen-preparation reactor can also change in a big way.Further, it is
Adapt to newly-built hydrogen manufacturing conversion furnace unit scale or the upgrading of existing hydrogen manufacturing conversion furnace plant modification, the reformation hydrogen production reaction of the disclosure
The reactor inside diameter of device can be 30~1000mm, preferably 50~300mm；Catalytic reaction zone length can be in reactor
1000mm~30000mm, preferably 3000mm~15000mm.
As shown in Figure 1, mobility status of the reactor feed gas in the reforming hydrogen-preparation reactor of the disclosure may include: reaction
Unstripped gas enters the central tube 6 of central tube 13 from reactor air inlet 1 through the first straight tube 11, is distributed in the gas of central tube aperture
It under effect, uniformly radially into central tube 13, and flows radially outward, reactor feed gas is while outside flowing in micro- catalysis
The catalyst active center of 10 area load of reaction plate reacts, and reaction stream flows to the lateral wall of central tube 13 simultaneously outward
Collect across side-wall hole in cushion chamber 16, cushion chamber 16 it is further buffering, reallocation effect under, reaction stream continue to
Outer flowing into sleeve 15, and flows radially outward, and reactor feed gas is while outside flowing in micro- 10 table of catalysis reaction plate
The catalyst active center of face load reacts, reaction stream continue to flow through outward the lateral wall of outermost sleeve 15 from
Catalytic reaction zone is opened, is collected in annular space 7, into air collecting chamber 9, reformation hydrogen production reaction is left by the second straight tube 14, gas outlet 2
Device.
As shown in figure 12, the second aspect of the disclosure provides a kind of reformation hydrogen production reburner, including air inlet pipe 24, escape pipe
25, burner 23 and combustion chamber 22, the reburner further include the reforming hydrogen-preparation reactor 21 of disclosure first aspect, and reformation hydrogen production is anti-
Device 21 is answered to be located in combustion chamber 22, the air inlet 1 of reforming hydrogen-preparation reactor 21 is connected to air inlet pipe 24, reforming hydrogen-preparation reactor
Gas outlet 2 is connected to escape pipe 25.
According to the disclosure, reformation hydrogen production reburner can be this field conventional kind, such as can burn for tipburn furnace, side
At least one of furnace, bottom fired heater and trapezoidal furnace, tipburn furnace preferably as shown in figure 12 and/or as shown in fig. 13 that side are burnt
Furnace.Burner, fuel type etc. are not done specifically limited in reburner, as long as can satisfy energy needed for reformation hydrogen production.In addition,
The disclosure is not particularly limited the reactor quantity being mounted between reburner air inlet pipe, escape pipe and arrangement mode etc.,
As long as meeting the requirement of reforming hydrogen producing process condition.
The reformation hydrogen production converting furnace pressure drop of the disclosure is low, in boiler tube per volume of catalyst product space-time yield
Height, and reburner overall dimensions are small, reduce equipment investment and energy consumption.
The third aspect of the disclosure provides a kind of method of reformation hydrogen production reaction, method includes the following steps: (1) makes to fire
Material gas and air spray into combustion chamber by burner and burn；(2) enter the air inlet pipe of unstripped gas and the inverted furnace of vapor
Reforming hydrogen-preparation reactor carries out reformation hydrogen production reaction in radial catalytic reaction zone, obtains the conversion gas rich in hydrogen.
The reformation hydrogen production reaction method reformer tube internal pressure reduction of the disclosure, unstripped gas high conversion rate, can satisfy hydrogen manufacturing
Reaction requires.
In the reformation hydrogen production reaction method according to the disclosure, the condition of reformation hydrogen production reaction can become in a big way
Change, it is preferable that the reaction temperature in reforming hydrogen-preparation reactor can be 700~1100 DEG C, preferably 800~950 DEG C；Reaction pressure
Power can be 1.8~5.5MPaG, preferably 1.8~3.5MPaG, the H in vapor2Mole of O and the carbon atom in unstripped gas
Than that can be (2.5~5): 1, preferably (2.5~4): 1.Under above-mentioned preferred reaction condition, the reformation hydrogen production of the disclosure reacts
Conversion ratio is higher.
Further, in order to improve unstripped gas conversion ratio, unstripped gas air speed can be 1000~100000h-1, further excellent
Select 3000~90000h-1, most preferably 8000~70000h-1。
Further, in order to improve unstripped gas conversion ratio, unstripped gas is divided by central tube 13 and 15 radial width two of sleeve
One of the mean flow rate at place can be 0.3~90m/s, preferably 0.8~55m/s, more preferably 1.0~45m/s.
In the reformation hydrogen production reaction method according to the disclosure, reactor feed gas can be natural gas, liquefied petroleum gas, refining
At least one of factory's gas, the resolution gas for reforming hydrogen concentrate PSA and naphtha.Further, natural gas mainly becomes methane, and
Containing the small molecules such as a small amount of ethane hydro carbons, carbon dioxide and nitrogen etc., the sulfur content in natural gas is low, and predominantly vulcanizes
Hydrogen, mercaptan, hydroxyl sulphur etc. are easy to be removed by simple hydrotreating；Refinery gas is primarily referred to as crude distillation
Fixed gas, catalysis drying gas, coking dry gas plus hydrogen dry gas and reformation dry gas of device etc.；Liquefied petroleum gas main component be propane,
Propylene, butane, butylene, can be the mixture of one or more of above-mentioned hydrocarbon, and contain a small amount of pentane, amylene and trace sulfide
Impurity, wherein carbonyl sulfide is removed with hydramine absorption tower, and removes sulphide removal with alkali wash；Reform the resolution gas of hydrogen concentrate PSA
In contain about a large amount of hydrogen and some small molecule hydro carbons；The preferentially sequence of naphtha are as follows: do 70 DEG C of perfectly straight light naphthar
(reforming topped oil), refinery's narrow fraction reforming raffinate oil, the perfectly straight gasoline of full fraction for doing 146 DEG C, one way are hydrocracked stone brain
Oil.
In the reformation hydrogen production reaction method according to the disclosure, steam can refer to middle pressure steam, and temperature can be 420 DEG C
Left and right, pressure can be 3.5Mpa or so, and the temperature, pressure of steam are it is possible that fluctuation, this public affairs during practical distribution
It opens and is not particularly limited, as long as meeting process for making hydrogen needs condition.
In the reformation hydrogen production reaction method according to the disclosure, reformation hydrogen production catalysts can be conventional kind of this field
Class, for example, reformation hydrogen production catalysts may include reformation hydrogen production active component, reformation hydrogen production active component may include
At least one of nickel, ruthenium, platinum, palladium, iridium and rhodium.
The present invention is further illustrated by embodiment below in conjunction with attached drawing, but therefore the disclosure is not taken office
What is limited.
Embodiment 1
As shown in Figure 1 and Figure 2, reforming hydrogen-preparation reactor used by the present embodiment includes being equipped with the first straight tube containing upper end
11, lower end is equipped with the pressure-bearing shell 12 of the second straight tube 14, sets that there are four sleeve 15 (being not entirely shown in figure) and one in shell
The radial catalytic reaction zone that central tube 13 is constituted, the top of the first straight tube 11 are provided with air inlet 1, the setting of 14 lower part of the second straight tube
There is gas outlet 2.Catalytic reaction zone is made of the micro- catalysis reaction plate 10 of plane, and micro- catalysis reaction plate 10 is with horizontal direction angle
90 °, micro- catalysis reaction plate 10 is uniformly distributed rotating around central tube or central tube are radial, central tube 6, central tube 13, sleeve
15 arrange with shell 12 in coaxial manner；Micro- catalysis reaction plate 10 of central tube 13 and top sealing plate 5, sealed bottom plate 8, in
Heart pipe 6 is connected and fixed；Micro- catalysis reaction plate 10 of sleeve 15 is connected and fixed with top sealing plate 5, sealed bottom plate 8；Micro- catalysis
Catalytic active component NiO needed for 10 liang of lateral loads of reaction plate have reformation hydrogen production to react.
The internal diameter of reforming hydrogen-preparation reactor is 120mm, tangential length 12000mm, inner diameter of centerpipe 35mm, catalysis reaction
Area height 10000mm, central tube use circular opening, and pore size isUniform pore openings, percent opening 17.5%,
Adjacent two micro- catalysis reaction plate average headway is 1mm, and annular space distance is 5mm, and the mean flow rate between micro- catalysis reaction plate is
1.04m/s。
Reactor shell material uses HP40-Nb (containing the elements such as Cr, Ni, Nb, W, Mo, Ti), micro- catalysis reaction plate 10
Using Fe-Cr-Al/Al2O3Material material is catalysis load substrate, and is planar substrates, and substrate two sides supported active metals are
NiO, content 13.5%.
The reformation hydrogen production reburner of the present embodiment is as shown in figure 12, including above-mentioned reforming hydrogen-preparation reactor 21, air inlet pipe 24,
Escape pipe 25, burner 23 and combustion chamber 22, reforming hydrogen-preparation reactor 21 are located in combustion chamber 22, reforming hydrogen-preparation reactor 21 into
Port 1 is connected to air inlet pipe 24, and the gas outlet 2 of reforming hydrogen-preparation reactor is connected to escape pipe 25.
The reforming hydrogen-preparation reactor of the present embodiment and reburner are reacted applied to natural gas steam reformation hydrogen production, it is main to walk
Suddenly include:
1) so that the burner 23 of fuel gas and the inverted furnace of air is sprayed into combustion chamber 22, make fuel in the combustion chamber of reburner
Burning provides hydrogen production reaction institute calorific requirement, and temperature of reactor is 940 DEG C；
2) water vapour and CH4The mixed gas (500 DEG C of temperature, pressure 3.1MPaG) that molar ratio is 2.9, flow is
38kmol/h, air speed 53501h-1, reburner air inlet pipe is entered after being sufficiently mixed, passes through the first straight tube of reactor 11, central tube 6
Into central tube 13, sleeve 15 micro- catalysis reaction plate 10 on carry out reformation hydrogen production reaction, the conversion gas after reacting passes through
Annular space 7, air collecting chamber 9, the second straight tube 14 leave reactor, and into conversion furnace outlet duct, the conversion gas that will be enriched in hydrogen is expelled to
Outside reburner.It is detected, outlet methane content (not moisture vapor) is 0.95%.
Provided in table 1 be the reforming hydrogen-preparation reactor and same reactor size in the prior art of the present embodiment and it is identical
The hydrogen-manufacturing reactor comparative situation of catalytic reaction zone size.
The reforming reactor and conventional hydrogen production reactor of 1 the present embodiment of table compare
| Type of reactor | Pressure drop, MPa | CH4Conversion ratio/(%) | Air speed, h-1 |
| Conventional reactor | 0.33 | 95 | 3400 |
| The reactor of the present embodiment | 0.1 | ≥96 | 53501 |
Embodiment 2
As shown in Fig. 1, Fig. 3, Fig. 9, the reforming hydrogen-preparation reactor and reburner of the present embodiment and the reactor ruler of embodiment 1
Very little, adjacent two micro- catalysis reaction plate spacing, annular space distance, micro- basic material and unit area active component for being catalyzed reaction plate
NiO load capacity parameter is identical.Difference from Example 1 is that micro- catalysis reaction plate is tooth form micro-reaction plate in the present embodiment,
Its waveform direction is along reactor axial direction.For castellated plates, peaks and troughs distance is 4mm, same micro- shape plate two
The distance between adjacent peaks or adjacent trough are 6.5mm.The reforming hydrogen-preparation reactor of the present embodiment and reburner are applied to
The reaction of natural gas steam reformation hydrogen production.Process for making hydrogen condition is same as Example 1, is detected, and methane content (not aqueous steaming is exported
Vapour) it is 0.87%.
Provided in table 2 be the reforming hydrogen-preparation reactor and same reactor size in the prior art of the present embodiment and it is identical
The hydrogen-manufacturing reactor comparative situation of catalytic reaction zone size.
The reforming reactor and conventional hydrogen production reactor of 2 the present embodiment of table compare
| Type of reactor | Pressure drop, MPa | CH4Conversion ratio/(%) | Air speed, h-1 |
| Conventional reactor | 0.33 | 95 | 3400 |
| The reactor of the present embodiment | 0.093 | ≥96.3 | 53501 |
Embodiment 3
As shown in Fig. 1, Fig. 4, Figure 11, the reforming hydrogen-preparation reactor and reburner of the present embodiment and the reactor of embodiment 1
Size, adjacent two micro- catalysis reaction plate spacing, annular space distance, micro- basic material and unit area active component for being catalyzed reaction plate
NiO load capacity parameter is identical.Difference from Example 1 is that micro- catalysis reaction plate is waveform micro-reaction plate in the present embodiment,
Its waveform direction is along reactor axial direction.For corrugated sheet, peaks and troughs distance is 4mm, and same micro- catalysis is anti-
Answering the distance between two adjacent peaks of plate or adjacent trough is 6.5mm.
The reforming hydrogen-preparation reactor of the present embodiment and reburner are reacted applied to natural gas steam reformation hydrogen production.Hydrogen manufacturing work
Skill condition is same as Example 1, is detected, and outlet methane content (not moisture vapor) is 0.85%.
Provided in table 3 be the reforming hydrogen-preparation reactor and same reactor size in the prior art of the present embodiment and it is identical
The hydrogen-manufacturing reactor comparative situation of catalytic reaction zone size.
The reforming reactor and conventional hydrogen production reactor of 3 the present embodiment of table compare
| Type of reactor | Pressure drop, MPa | CH4Conversion ratio/(%) | Air speed, h-1 |
| Conventional reactor | 0.33 | 95 | 3400 |
| The reactor of the present embodiment | 0.09 | ≥96.5 | 53501 |
Embodiment 4
As shown in Figure 1, shown in Figure 5, the present embodiment reactor, process for making hydrogen condition etc. are identical as 1 number of embodiment.With embodiment 1
The difference is that adjacent micro- catalysis reaction plate 10 of central tube 13 is provided with supplement close to 12 side of shell and micro- urges in the present embodiment
Change reaction plate 17, supplements micro- catalysis reaction plate 17 and be arranged with micro- 10 alternate intervals of catalysis reaction plate, supplement micro- catalysis reaction plate 17
Dependency structure parameter it is identical as micro- catalysis reaction plate 10 of central tube 13, radial width be micro- catalysis reaction plate 10 it is radially-wide
The one third of degree.The reforming hydrogen-preparation reactor of the present embodiment and reburner are reacted applied to natural gas steam reformation hydrogen production.
Process for making hydrogen condition is same as Example 1, is detected, and outlet methane content (not moisture vapor) is 0.3%.
Provided in table 4 be the reforming hydrogen-preparation reactor and same reactor size in the prior art of the present embodiment and it is identical
The hydrogen-manufacturing reactor comparative situation of catalytic reaction zone size.
The reforming reactor and conventional hydrogen production reactor of 4 the present embodiment of table compare
| Type of reactor | Pressure drop, MPa | CH4Conversion ratio/(%) | Air speed, h-1 |
| Conventional reactor | 0.33 | 95 | 3400 |
| The reactor of the present embodiment | 0.12 | ≥97.5 | 53501 |
Embodiment 5
If Fig. 1, Fig. 6 show, the reforming hydrogen-preparation reactor and reburner of the present embodiment, process for making hydrogen condition etc. and embodiment 1
Number is identical.Difference from Example 1 is, the adjacent micro- catalysis reaction plate 10 of central tube 13 is close to shell 12 in the present embodiment
Side is provided with the micro- catalysis reaction plate 17 of supplement, adjacent micro- catalysis reaction plate 10 of sleeve 15 be provided with close to 12 side of shell supplement it is micro-
It is catalyzed reaction plate 17, micro- catalysis reaction plate 17 is supplemented and is arranged with micro- 10 alternate intervals of catalysis reaction plate, supplement micro- catalysis reaction plate
17 dependency structure parameter is identical as central tube 13, micro- catalysis reaction plate 10 of sleeve, cylinder 13, sleeve centered on radial width
The one third of catalysis 10 radial width of reaction plate in 15.The reforming hydrogen-preparation reactor of the present embodiment and reburner are applied to day
Right gas steam reformation hydrogen production reaction.Process for making hydrogen condition is same as Example 1, is detected, and methane content (not aqueous steaming is exported
Vapour) it is 0.21%.
Provided in table 5 be the reforming hydrogen-preparation reactor and same reactor size in the prior art of the present embodiment and it is identical
The hydrogen-manufacturing reactor comparative situation of catalytic reaction zone size.
The reforming reactor and conventional hydrogen production reactor of 5 the present embodiment of table compare
| Type of reactor | Pressure drop, MPa | CH4Conversion ratio/(%) | Air speed, h-1 |
| Conventional reactor | 0.33 | 95 | 3400 |
| The reactor of the present embodiment | 0.14 | ≥98 | 53501 |
Embodiment 6
As shown in Figure 7, Figure 8, the reforming hydrogen-preparation reactor of the present embodiment and reburner are identical as 1 parameter of embodiment.With reality
Apply example 1 the difference is that, the present embodiment middle sleeve number be 6 (being not entirely shown in figure).The present embodiment is using reformation hydrogen
Concentrate PSA resolution gas is shown in Table 6 as reaction raw materials, resolution gas group.Take reformation hydrogen production tipburn furnace shown in Figure 13 as conversion
Furnace, reactor connection relationship are same as Example 1.Fuel burn in the combustion chamber of reburner provide hydrogen production reaction needed for heat
Amount, temperature of reactor are 935 DEG C.Water vapour and CH4The mixed gas (500 DEG C of temperature, pressure 3MPaG) that molar ratio is 2.8, stream
Amount is 43kmol/h, air speed 60540h-1, reburner air inlet pipe is entered after being sufficiently mixed, passes through the first Helicopter-11 of reactor, central tube
6, which enter catalytic reaction zone (central tube 13, sleeve 15), carries out reformation hydrogen production reactions, conversion gas after reacting by annular space 7,
Air collecting chamber 9, the second straight tube 14 leave reactor, and into conversion furnace outlet duct, the conversion gas that will be enriched in hydrogen is expelled to reburner
It is external.It is detected, outlet methane content (not moisture vapor) is 0.35%.
Using the reactor provided in embodiment 1, reaction raw materials, process conditions are different from embodiment 1, obtained reaction knot
Fruit and conventional reactor are shown in Table 7 in the reaction result comparative situation that same reaction raw material and process conditions obtain.
Table 6 reforms hydrogen concentrate PSA resolution gas composition
The reforming reactor and conventional hydrogen production reactor of 7 the present embodiment of table compare
| Type of reactor | Pressure drop, MPa | CH4Conversion ratio/(%) | Air speed, h-1 |
| Conventional reactor | 0.38 | 97 | 4400 |
| The reactor of the present embodiment | 0.16 | ≥98 | 60540 |
The reforming hydrogen-preparation reactor that the disclosure provides is compact-sized, active metal dosage is few；The reactor is reformed
When hydrogen production reaction, bed pressure drop is small, per volume of catalyst production intensity is big, reactant diffusion path is shorter, feed stock conversion
Height, no gas bias current and short circuit phenomenon, can satisfy the production process of existing steam reforming hydrogen manufacturing.
It can be seen that from the data of embodiment 1-6 from reactor bed pressure drop, CH4Three conversion ratio, air speed indexs can be with
To find out, the reforming hydrogen-preparation reactor and reburner of the disclosure show excellent performance, reactor pressure decrease especially is being reduced,
Advantage in terms of raising reactor air speed is especially prominent.
The preferred embodiment of the disclosure is described in detail in conjunction with attached drawing above, still, the disclosure is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the disclosure, a variety of letters can be carried out to the technical solution of the disclosure
Monotropic type, these simple variants belong to the protection scope of the disclosure.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, it can be combined in any appropriate way.In order to avoid unnecessary repetition, the disclosure to it is various can
No further explanation will be given for the combination of energy.
In addition, any combination can also be carried out between a variety of different embodiments of the disclosure, as long as it is without prejudice to originally
Disclosed thought equally should be considered as disclosure disclosure of that.
Claims (10)
1. a kind of reforming hydrogen-preparation reactor, which is characterized in that the reactor includes cylinder-shaped seal and pressure bearing shell (12), air inlet
(1), gas outlet (2), enclosure interior is extend at the top of the shell (12) the first straight tube (11), from the shell (12) bottom
Portion extend into the second straight tube (14) of enclosure interior and is arranged in the shell (12) described in the first straight tube (11) lower section
Radial catalytic reaction zone above second straight tube (14)；The air inlet is connected to first straight tube (11), the gas outlet
(2) it is connected to second straight tube (14)；
The radial direction catalytic reaction zone is sealed by top sealing plate (5) and sealed bottom plate (8) respectively up and down, and the top is close
The edge of sealing plate (5) and the shell (12) inner wall are tightly connected, the radial direction catalytic reaction zone include central tube (13) and
It is set at least one sleeve (15) of central tube (13) outside；Central tube (13) has central tube (6), and central tube (6) passes through top
Portion's sealing plate (5) and the first straight tube (11) are in fluid communication；Between central tube lateral wall and the inner sidewall of innermost layer sleeve and phase
Cushion chamber (16) are respectively formed between the barrel of adjacent sleeve (15)；The lateral wall of outermost sleeve (15) and shell (12)
Annular space (7) are formed between inner wall；
The side wall of the central tube (6), central tube (13) and sleeve (15) is respectively formed with aperture, so that the central tube (6)
It is in fluid communication by the aperture and the annular space (7)；The sealed bottom plate (8) and the shell of the radial direction catalytic reaction zone
(12) it is formed between the inner wall of lower part air collecting chamber (9), the air collecting chamber (9) and the annular space (7) are in fluid communication；
Micro- catalysis reaction plate (10) is respectively equipped in the central tube (13) and the sleeve (15), in the central tube (13)
It is micro- catalysis reaction plate (10) edge respectively with the top sealing plate (5), sealed bottom plate (8), central tube (6) tube wall and in
Heart cylinder (13) inner sidewall is tightly connected, and the edge of micro- catalysis reaction plate (10) in the sleeve (15) is close with the top respectively
It is tightly connected between sealing plate (5), sealed bottom plate (8) and the inner sidewall and lateral wall of the sleeve (15), micro- catalysis is anti-
Answering the plate face of plate to load has reforming hydrogen-production catalyst.
2. reforming hydrogen-preparation reactor according to claim 1, which is characterized in that micro- catalysis in the central tube (13) is anti-
Plate (10) are answered to radially distribute around the central tube (6)；Micro- catalysis reaction plate (10) in the sleeve (15) surrounds institute
Central tube (13) is stated to radially distribute.
3. reforming hydrogen-preparation reactor according to claim 1, which is characterized in that micro- catalysis reaction plate (10) be selected from
At least one of surface plate, castellated plates, corrugated plating and corrugated sheet.
4. reforming hydrogen-preparation reactor according to claim 1, which is characterized in that in the central tube (13) and/or described
The micro- catalysis reaction plate (17) of supplement is additionally provided in sleeve (15), the micro- catalysis reaction plate (17) of supplement is reacted with micro- catalysis
The plate face load of the setting of plate (10) alternate intervals, micro- catalysis reaction plate (17) of supplement has reforming hydrogen-production catalyst；It is described micro-
The ratio between the radial width for being catalyzed reaction plate (10) and micro- catalysis reaction plate (17) of the supplement is greater than 1.5；
It is described supplement it is micro- catalysis reaction plate (10) edge respectively with the top sealing plate (5), sealed bottom plate (8), center
The inner seal connection of cylinder (13) barrel；Alternatively, the edge of micro- catalysis reaction plate (17) of supplement is close with the top respectively
The inner seal connection of sealing plate (5), sealed bottom plate (8), sleeve (15) outer wall.
5. reforming hydrogen-preparation reactor according to claim 1, which is characterized in that the number of the sleeve (15) is 1~500
A, the sleeve (15), central tube (13), central tube (6) and shell (12) are arranged in coaxial manner.
6. a kind of reformation hydrogen production reburner, including air inlet pipe (24), escape pipe (25), burner (23) and combustion chamber (22), it is special
Sign is that the reburner further includes reforming hydrogen-preparation reactor described in any one of Claims 1 to 5 (21), the reformation
Hydrogen-manufacturing reactor (21) is located in the combustion chamber (22), the air inlet (1) of the reforming hydrogen-preparation reactor (21) and it is described into
Tracheae (24) connection, the gas outlet (2) of the reforming hydrogen-preparation reactor is connected to the escape pipe (25).
7. the method for carrying out reformation hydrogen production reaction using reformation hydrogen production reburner as claimed in claim 6, which is characterized in that the party
Method the following steps are included:
(1) make fuel gas and air spray into the combustion chamber (22) by the burner (23) to burn；
(2) air inlet pipe (24) of unstripped gas and vapor through the reburner is made to enter the reforming hydrogen-preparation reactor (21),
Reformation hydrogen production reaction is carried out in the radial direction catalytic reaction zone, obtains the conversion gas rich in hydrogen.
8. the method according to the description of claim 7 is characterized in that the condition of reformation hydrogen production reaction includes: reaction temperature
It is 700~1100 DEG C, reaction pressure is 1.8~5.5MPaG, the H in vapor2The molar ratio of O and the carbon atom in unstripped gas
For (2.5~5): 1, air speed is 1000~100000h-1。
9. the method according to the description of claim 7 is characterized in that the unstripped gas passes through the central tube (13) and the set
Mean flow rate at cylinder (15) radial width half is 0.3~90m/s.
10. the method according to the description of claim 7 is characterized in that the unstripped gas is natural gas, liquefied petroleum gas, refinery
At least one of gas, the resolution gas for reforming hydrogen concentrate PSA and naphtha；The reformation hydrogen production catalysts include the system of reforming
Hydrogen activity component, the reformation hydrogen production active component include at least one of nickel, ruthenium, platinum, palladium, iridium and rhodium.
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| CN109694037B (en) | 2021-03-05 |
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