CN102826507A - Method and device of hydrogen production by natural gas and steam reforming for micro fuel cells - Google Patents
Method and device of hydrogen production by natural gas and steam reforming for micro fuel cells Download PDFInfo
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- CN102826507A CN102826507A CN201210306523XA CN201210306523A CN102826507A CN 102826507 A CN102826507 A CN 102826507A CN 201210306523X A CN201210306523X A CN 201210306523XA CN 201210306523 A CN201210306523 A CN 201210306523A CN 102826507 A CN102826507 A CN 102826507A
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Abstract
The invention discloses a method and a device of hydrogen production by natural gas and steam reforming for micro fuel cells. The device comprises an upper end cover, a reactor body, a reactor upper flange, a reactor outer cylinder, a combustor and a preheating coiled tube, the preheating coiled tube comprises a natural gas preheating tube, a water preheating tube and a gas mixture preheating tube, the upper end cover and the reactor outer cylinder are of hollow cylindrical structures, the preheating coiled tube is arranged in the upper end cover, the reactor body is arranged in the reactor outer cylinder, the combustor is arranged on the lower portion of the reactor body, the reactor body is in flange connection with the reactor outer cylinder and the upper end cover and is of a hollow annular structure with a hollow center, an annular cavity is arranged on the periphery of the hollow center, two baffles are arranged in the annular cavity and divide the annular cavity into a left cavity and a right cavity, gaps are reserved on the lower portions of the baffles, and catalyst particles are distributed in the left cavity and the right cavity. The device is used for preparing synthesis gas by natural gas and steam reforming, and is fast in starting, convenient and feasible to mount and demount and small in size and occupied area.
Description
Technical field
This patent relates to a kind of non-pressurized Sweet natural gas steam reformation hydrogen production, particularly relates to Sweet natural gas steam reformation hydrogen production method and device, and its device is used to multikilowatt Proton Exchange Membrane Fuel Cells co-generation unit hydrogen-rich synthetic gas is provided.
Technical background
Hydrogen Energy is a kind of novel high-efficiency cleaning energy, is regarded as the Greenhouse effect problem that solves, and improves effective substitute energy of capacity usage ratio.But hydrogen is not the first resources of a large amount of existence of occurring in nature, and its density is low, and is inflammable and explosive, and the expense of storage and transportation is high, and is greatly dangerous, and how obtaining hydrogen easily is that Hydrogen Energy is able to one of extensive bottleneck that utilizes.Sweet natural gas steam reformation technology is the production hydrogen that the most generally adopts in the present industry and the technological method of synthetic gas, and the typical reaction temperature is 800-900 ℃, and pressure is 2.5-3.5MPa.Along with the mass development of Sweet natural gas, especially pipe natural gas is popularized in cities and towns, for distributed hydrogen gas production provides competent, cheap gas material.
Fuel cell is the efficient energy conversion device that chemical energy is converted into electric energy of generally acknowledging, is to utilize hydrogen energy source to alleviate the desirable technique of fossil energy crisis.For family and small business users, the electrogenesis power of fuel cell only needs kilowatt, just is enough to satisfy its demand, and we call micro fuel cell to the less fuel cell of this power ratio.Simultaneously from gas production hydrogen and hydrogen through the process of fuel cell power generation, some heat can be collected and utilize, we can produce electric energy and heat energy calls cogeneration for the system that utilizes simultaneously this.For family and small business users, heat energy generally utilizes through the mode that produces hot water again.
Though the gas renormalizing hydrogen producing technology has obtained widespread usage in industry, should technology in the distributed hydrogen manufacturing of miniaturized, also have a lot of problems to need to solve.This reaction is a strong endothermic reaction, conducts heat and the energy utilization is a bottleneck problem of this reaction, and the reactor volume of using always in the industry is huge, is not suitable for the requirement of distributed hydrogen gas production in the multikilowatt fuel cell system of family and small business users.
Summary of the invention
The objective of the invention is to overcome the technical disadvantages of pre-existing reactors, for multikilowatt small fuel cell co-generation unit provides a kind of quick, safety; Device for producing hydrogen efficiently, it is raw material sources that this device adopts urban duct Sweet natural gas, compact construction; Handled easily, volume is little, is easy to install.
Another purpose of the present invention is providing the Sweet natural gas steam reformation hydrogen production method of using said apparatus.
The object of the invention is realized through following technical scheme:
A kind of Sweet natural gas steam reformation hydrogen production device that is used for micro fuel cell comprises upper end cover, reactor body, reactor drum upper flange, reactor drum urceolus, burner and preheat coil; Preheat coil comprises Sweet natural gas preheating tubes, water preheat pipe and charge heating pipe; Upper end cover and reactor drum urceolus are the hollow cylinder structure; Preheat coil is arranged in the upper end cover; Reactor body is arranged in the reactor drum urceolus; Burner places the bottom of reactor body; Reactor body is connected through flange with upper end cover with the reactor drum urceolus;
The a plurality of eyelets of said reactor drum upper flange outer shroud uniform distribution, a plurality of eyelets of interior ring uniform distribution; Distribute equally in the position corresponding with the reactor drum upper flange eyelet of equivalent amount of reactor body is connected the reactor drum upper flange through bolt with reactor body; Mixed gas inlet is positioned at reactor drum upper flange left side, and the synthetic gas air outlet is positioned at reactor drum upper flange right side; Mixed gas inlet and charge heating pipe coupling; The synthetic gas escape pipe is connected with the synthetic gas air outlet, is upwards stretched out by upper end cover top; The stack gas escape pipe stretches out from upper end cover top;
Said reactor body is the hollow ring structure, and the center is hollow, and hollow periphery is an annular cavity, and annular cavity is provided with two baffle plates; Two baffle plates are divided into left chamber and right chamber with annular cavity, and the space is arranged at the baffle plate bottom; Granules of catalyst is distributed in left chamber and the right chamber, and granules of catalyst is a nickel-base catalyst; Be provided with the passage of two arcuations at the reactor body top, the passage of arcuation is between the reactor body upper flange outside and reactor drum urceolus inboard; Reactor body and reactor drum upper flange center are provided with through hole;
Sweet natural gas preheating tubes and water preheat pipe get in the upper end cover cavity from upper end cover top; The Sweet natural gas preheating tubes is provided with water preheat pipe inboard in the upper end cover cavity; The helicoidal structure rotation downwards; Sweet natural gas preheating tubes and water preheat pipe are through threeway and charge heating pipe coupling, and the charge heating pipe adopts spirane structure.
For further realizing the object of the invention, the outer shroud of said annular cavity and the correction for semi-diameter of interior ring are the width L=aW of annular cavity, and wherein: W is the width of granules of catalyst, is 4-6mm; A gets 4-6 for adorning the number of catalyzer side by side; The outer ring diameter R of annular cavity
2With interior ring diameter R
1And the annular cavity height H satisfies simultaneously:
A＝pH(R
1+R
2)＝(1.2～1.5)Q/KDT；
Wherein: Q is a steam reaction institute heat requirement, Q=nDH, and n is the molar weight of the required Sweet natural gas of reaction, DH is that unit mole Sweet natural gas and water vapour react needed heat; K is the coefficient of heat transfer between reaction gas and the stack gas; DT is reaction gas and stack gas logarithm heat transfer temperature difference; A is the heat interchanging area of reactor drum; V is the volume of reactor drum annular section; V
1Admission space for catalyzer.
Said nickel-base catalyst loadings
Wherein: F is the volumetric flow rate of Sweet natural gas in the virgin gas; V is the carbon space velocity of catalyzer, and the carbon space velocity of catalyzer is 500～1500h
-1
Said baffle plate preferably adopts stainless steel to make, and welds together with the reactor body inner and outer ring; The height in said space is preferably 1/10 of reactor body height.
The width of channel of said arcuation is preferably 1.5～3cm.
The diameter of said preheating tubes is preferably 4～8mm, and the material of preheating tubes material is preferably copper product.
The said Sweet natural gas preheating tubes and the water preheat pipe helicoidal structure coiling number of turns are preferably the 5-10 circle; The charge heating pipe helicoidal structure coiling number of turns is preferably the 7-12 circle.
The diameter R of said reactor drum urceolus
3=R
2+ (6～12) cm, length is than the long 20-30% of reactor body; R
2Outer ring diameter for annular cavity.
Said upper end cover and reactor drum urceolus periphery coat lagging material, and lagging material is a ceramic fiber, and the thickness of lagging material is greater than 10 centimetres.
Use the Sweet natural gas steam reformation hydrogen production method of said device, it is characterized in that may further comprise the steps:
The first step, the maintenance reactor pressure is a normal pressure, starts burner, the preheating reactor body, catalyst temperature reaches 150～200 ℃ in reactor body;
Second step fed water through the water preheat pipe, and burner continues heating, catalyst temperature to 500～800 ℃ to the reactor body;
The 3rd step fed Sweet natural gas through the Sweet natural gas preheating tubes, and the ratio of the molar flow of Sweet natural gas is 2～4 in the molar flow of control water and the Sweet natural gas preheating tubes; Water and Sweet natural gas advanced preheating pipe preheating separately respectively after the charge heating pipe is merged into gas mixture; Be preheating to temperature required 500～800 ℃ of reaction; Get in the chamber, a reactor body left side reforming reaction takes place; Get into the then reaction of the right chamber of reactor body through the baffle plate lower space then, the hydrogen-rich gas that final reaction produces is drawn through the synthetic gas escape pipe.
Principle of work of the present invention is Sweet natural gas and water vapour generation steam reforming reaction, and wherein main reaction process comprises:
CH
4+H
2O＝CO+3H
2ΔH＝206.2kJ/mol
CH
4+2H
2O＝CO
2+4H
2ΔH＝164.9kJ/mol
The selection of burner rating of the present invention is by reaction and the needed heat decision of preheating; Burner adopts atmospheric burner, and fuel used is Sweet natural gas, produces stack gas elder generation and reactor body heat exchange; For reaction provides heat; With the preheating tubes heat exchange,, draw through the stack gas escape pipe at last and carry out next step Btu utilization then for raw material preheating provides heat.
The present invention compared with prior art has the following advantages:
1) preheater, reactor drum, burner combines, the direct cascade utilization of stack gas, heating, insulation and good effect of heat exchange have improved capacity usage ratio, and have guaranteed the temperature condition that reacts required;
2) reactor drum has adopted the hollow ring structure, middle and and outer wall between the cavity stack gas that circulates simultaneously guaranteed enough heat interchanging areas;
3) in the reactor drum annular space use of baffle plate originally annular space be divided into two semi-circular, reduced the influence that feed entrance point distributes to reactant gases, thereby reduced the generation of channel and dead band in the ring structure;
4) be reflected at operation under the normal pressure, safe and reliable to operation;
5) reactor drum is simple in structure, and installation and removal are convenient and easy, and device volume is little, and floor space is few, can place balcony, the inferior idle space of eaves.
Description of drawings
Fig. 1 is the structural representation that is used for the Sweet natural gas steam reformation hydrogen production device of micro fuel cell.
Fig. 2 is the vertical view of reactor drum upper flange among Fig. 1.
Fig. 3 is a reactor body superstructure vertical view among Fig. 1.
Fig. 4 is the reactor body horizontal sectional view.
Fig. 5 be among Fig. 4 A-A to vertical section figure.
Fig. 6 be among Fig. 4 B-B to vertical section figure.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is described further; Following embodiment only is schematic rather than determinate; Other staff are under enlightenment of the present invention; Under aim of the present invention and claim, can make multiple similar expression, such conversion all falls within protection scope of the present invention.
As shown in Figure 1, a kind of Sweet natural gas steam reformation hydrogen production device that is used for micro fuel cell comprises upper end cover 4, reactor body 6, reactor drum upper flange 5, reactor drum urceolus 10, burner 9 and preheat coil; Preheat coil comprises Sweet natural gas preheating tubes 1, water preheat pipe 2 and charge heating pipe 12; Upper end cover 4 is the hollow cylinder structure with reactor drum urceolus 10; Preheat coil is arranged in the upper end cover 4; Reactor body 6 is arranged in the reactor drum urceolus 10; Burner 9 places the bottom of reactor body 6; Reactor body 6 and reactor drum urceolus 10 and upper end cover 4 are connected through flange;
Shown in Fig. 3-6, reactor body 6 is the hollow ring structure, and the center is hollow, and hollow periphery is an annular cavity, and annular cavity is provided with two baffle plates 19; Two baffle plates 19 are divided into left chamber 20 and right chamber 21 with annular cavity, and space 22 is arranged at baffle plate 19 bottoms; The baffle plate 19 preferred stainless steels that adopt are made, and weld together with the reactor body inner and outer ring; The height in space 22 is preferably 1/10 of reactor body height.The outer shroud of annular cavity and the correction for semi-diameter of interior ring are the width L=aW of annular cavity, and wherein: W is the width of granules of catalyst, is taken as 4-6mm; A gets 4-6 for adorning the number of catalyzer side by side; The outer ring diameter R of annular cavity
2With interior ring diameter R
1And the annular cavity height H satisfies simultaneously:
A＝pH(R
1+R
2)＝(1.2～1.5)Q/KDT；
Wherein: Q is a steam reaction institute heat requirement, Q=nDH, and n is the molar weight of the required Sweet natural gas of reaction, DH is that unit mole Sweet natural gas and water vapour react needed heat; K is the coefficient of heat transfer between reaction gas and the stack gas, by reactor material, and the flow characteristics of stack gas and reaction gas and the decision of the heat transfer property of catalyzer, in order to simplify calculating, the K value is 50Wm
-2K
-1DT is reaction gas and stack gas logarithm heat transfer temperature difference, and the temperature negate of reaction gas is answered temperature required 500-800 ℃, and stack gas is got 900-1100 ℃ according to the difference of selected burner; A is the heat interchanging area of reactor drum; V is the volume of reactor drum annular section; V
1Admission space for catalyzer.
Granules of catalyst 11 is distributed in left chamber 20 and the right chamber 21, and granules of catalyst 11 is a nickel-base catalyst, the reforming hydrogen-production catalyst of preferably producing by Shandong Qilu Petrochemical section power chemical institute, and this catalyzer is with α-Al
2O
3Be carrier, metallic nickel is an active ingredient.Said nickel-base catalyst loadings
Wherein: F is the volumetric flow rate of Sweet natural gas in the virgin gas; V is the carbon space velocity of catalyzer, and the carbon space velocity of catalyzer is 500～1500h
-1
As shown in Figure 2,8 eyelets of reactor drum upper flange 5 outer shroud uniform distribution, 6 eyelets of interior ring uniform distribution; Reactor body 6 with distribute the equally eyelet (seeing first, second two circles hole that Fig. 3 begins to calculate from the center) of equivalent amount of reactor drum upper flange 5 corresponding positions; Run through inside and outside eyelet through stainless steel bolt reactor drum upper flange 5 is connected with inside and outside two portions of reactor body 6, the sealing of pinner tampon sheet assurance reactor body 6 interior annular space in the middle of both simultaneously.Mixed gas inlet 16 is positioned at reactor drum upper flange 5 left sides, and synthetic gas air outlet 17 is positioned at reactor drum upper flange 5 right sides; Mixed gas inlet 16 is connected with charge heating pipe 12; Synthetic gas escape pipe 14 is connected with synthetic gas air outlet 17, is upwards stretched out by upper end cover 4 tops; Stack gas escape pipe 15 stretches out from upper end cover 4 tops.
As shown in Figure 3, be provided with the passage 18 of two arcuations at reactor body 6 tops, the passage 18 of arcuation is between reactor body 6 upper flanges, 5 outsides and reactor drum urceolus 10 inboards, and the width of the passage 18 of arcuation is preferably 1.5～3cm; The passage 18 of two arcuations is communicated with upper end cover 4 and reactor drum urceolus 10 internal cavities; Reactor body 6 is provided with through hole with reactor drum upper flange 5 centers simultaneously, and this through hole also is communicated with upper end cover 4 and reactor drum urceolus 10 internal cavities; The center cavity of reactor body 6, the passage between annular cavity and the reactor drum urceolus 10 is a first channel 7; The periphery of upper end cover 4 inner preheat coils constitutes second passage 13; The incendiary high-temperature flue gas gives reactor body 6 heating through first channel 7; Flue gas after the heat exchange gets in the upper end cover 4 with the through hole that reactor drum upper flange 5 centers are provided with through the passage 18 and the reactor body 6 of two arcuations; Through second passage 13 preheating materials; Flue gas is discharged through stack gas escape pipe 15, and funnel temperature maintains about 300 ℃.As shown in Figure 3, reactor body 6 outermosts one circle hole is to be used for reactor body 6 and the hole that reactor drum urceolus 10, upper end cover 4 are connected with flange, is provided with identical hole in upper end cover 4, reactor drum urceolus 10 and flange corresponding position; Be preferably 8 holes; 8 stainless steel bolts connect 8 eyelets, and reactor body 6 and reactor drum urceolus 10, upper end cover 4 and flange are linked together.
Sweet natural gas preheating tubes 1 gets in upper end cover 4 cavitys from upper end cover 4 tops with water preheat pipe 2; Sweet natural gas preheating tubes 1 is provided with water preheat pipe 2 inboards in upper end cover 4 cavitys; The helicoidal structure rotation is downward, and Sweet natural gas preheating tubes 1 is preferably the 5-10 circle with the water preheat pipe 2 helicoidal structures coiling number of turns, and Sweet natural gas preheating tubes 1 is connected with charge heating pipe 12 through threeway 3 with water preheat pipe 2; Charge heating pipe 12 also adopts spirane structure, and coil pipe twines the number of turns and is preferably the 7-12 circle.The diameter of preheating tubes is chosen 4～8mm; The material of preheating tubes material is a copper product, and to play good heat exchange effect, the length of preheating tubes depends on the temperature and the required temperature that is preheating to of stack gas; As stated, water preheat guarantees that card water becomes the water vapour coiling number of turns and is preferably the 5-10 circle; The Sweet natural gas preheating tubes coiling number of turns is preferably the 5-10 circle; Charge heating guarantees that card reaches the temperature of reaction coil pipe winding number of turns and is preferably the 7-12 circle.
The diameter R of reactor drum urceolus
3=R
2+ (6～12) cm, length is than the long 20-30% of reactor body, and reactor drum urceolus 10 is than reactor body 6 preferred long 25%.Upper end cover 4, reactor body 6, reactor drum upper flange 5, reactor drum urceolus 10, baffle plate 19 all adopt high temperature resistant stainless steel to make.Upper end cover 4, reactor drum urceolus 10 insulation materials parcel, this lagging material is a ceramic fiber, the thickness of lagging material is greater than 10 centimetres.Make the heat insulation material surface temperature be lower than 50 ℃.Establish support 8 on the reactor drum urceolus 10, be used for supporting whole reactor, support is processed by four stainless steel strips.
The diameter of preferred upper end cover is identical with the diameter of reactor drum urceolus.
Use the Sweet natural gas steam reformation hydrogen production method of said apparatus, it is characterized in that may further comprise the steps:
The first step, the maintenance reactor pressure is a normal pressure, starts burner 9, preheating reactor body 6, catalyst temperature reaches 150～200 ℃ in reactor body 6;
Second step fed water through water preheat pipe 2, and burner continues heating, catalyst temperature to 500～800 ℃ to the reactor body 6;
The 3rd step fed Sweet natural gas through Sweet natural gas preheating tubes 1, and the molar flow of control water is 2～4 with the ratio of the molar flow of Sweet natural gas preheating tubes 1 interior Sweet natural gas; Water and Sweet natural gas advanced preheating pipe preheating separately respectively after charge heating pipe 12 is merged into gas mixture; Be preheating to temperature required 500～800 ℃ of reaction; Get in the chamber, a reactor body left side reforming reaction takes place; Get into the then reaction of the right chamber of reactor body through the baffle plate lower space then, the hydrogen-rich gas that final reaction produces is drawn through synthetic gas escape pipe 14.
The selection of burner rating is by reaction and the needed heat decision of preheating; Burner adopts atmospheric burner, and fuel used is Sweet natural gas, produces stack gas elder generation and reactor body heat exchange; For reaction provides heat; With the preheating tubes heat exchange,, draw through the stack gas escape pipe at last and carry out next step Btu utilization then for raw material preheating provides heat.
Granules of catalyst 11 is chosen the reforming hydrogen-production catalyst that Shandong Qilu Petrochemical section power chemical institute is produced, and this catalyzer is with α-Al
2O
3Be carrier, metallic nickel is an active ingredient, and particle diameter is 5mm, and loadings is 0.9L; The interior ring diameter R of reactor body 6
1=160mm, outer ring diameter R
2=196mm and height H=200mm, the height in space 22 is 20mm on the baffle plate 19; Reactor body 6 tops and reactor drum upper flange 5 junction both sides external arcuation width of channel are 3cm; The diameter R of reactor drum urceolus 10
3=300mm, length is 240mm, and the length of the steel bar support of four stainless steel making is 12cm, and the diameter of upper end cover 4 is 300mm, highly is 200mm; Lagging material is a ceramic fiber, and its thickness is 12cm; The diameter of Sweet natural gas preheating tubes 1, water preheat pipe 2 and charge heating pipe 12 selects 6mm; The coiling diameter of Sweet natural gas preheating tubes 1 is 10cm; The coiling number of turns is 5 circles, and the coiling diameter of water preheat pipe 2 is 20cm, and the coiling number of turns is 5 circles; The coiling diameter of charge heating pipe is 16cm, and the coiling number of turns is 8 circles; Burner 9 is selected the 4KW atmospheric burner of rated output, and fuel is selected Sweet natural gas for use.
After device starts, start burner 9 earlier, the empty reforming reaction device that burns.When catalyst temperature reached 150 ℃ in the reactor body 6, the valve that is provided with on the preheating tubes 2 of fetching boiling water fed water, and the molar flow of water is 35mol/h.Current get into reactor bodies 6 earlier after become overheated steam behind the water preheat pipe 2, threeway 3,12 heating of charge heating pipe through mixed gas inlet 16, are used for purge main body 6, comprise each feed pipe.When the reactor body temperature reaches 500 ℃, open the valve that is provided with on the Sweet natural gas preheating tubes 1, in Sweet natural gas preheating tubes 1, feed Sweet natural gas, its flow is got 14mol/h, through threeway 3 Sweet natural gas and water vapour is mixed; Gas mixture is through charge heating pipe 12, and mixed gas inlet 16 gets into reactor body 6; Catalyst temperature is at 500～800 ℃ in reactor body 6, and water and Sweet natural gas are at the effect generation steam reformation hydrogen production reaction (CH of catalyzer 6
4+ H
2O=CO+3H
2).It is 315L/H that reaction reaches the flow that stable state is meant Sweet natural gas, and steam/hydrocarbons ratio is about 2.5, and temperature of reaction is about 700 ℃.Hydrogen output is about 800L/H with this understanding, has satisfied the requirement of the distributed hydrogen gas production of 1 multikilowatt fuel cell system that is used for family and small business users, has realized the cascade utilization of energy simultaneously, has improved energy utilization efficiency.
Granules of catalyst 11 is chosen the reforming hydrogen-production catalyst that Shandong Qilu Petrochemical section power chemical institute is produced, and this catalyzer is with α-Al
2O
3Be carrier, metallic nickel is an active ingredient, and particle diameter is 5mm, and loadings is 1.8L; The interior ring diameter R of reactor body 6
1=160mm, outer ring diameter R
2=196mm and height H=400mm, the height in baffle plate 19 spaces is 40mm; Reactor body 6 tops and reactor drum upper flange 5 junction both sides external arcuation width of channel are 3cm; The diameter R of reactor drum urceolus 10
3=300mm, length is 480mm, and the length of the steel bar support of four stainless steel making is 20cm, and the diameter of upper end cover 4 is 300mm, highly is 200mm; Lagging material is a ceramic fiber, and its thickness is 12cm; The diameter of Sweet natural gas preheating tubes 1, water preheat pipe 2 and charge heating pipe 12 selects 6mm; The diameter of Sweet natural gas preheating tubes 1 spirrillum coiling is 10cm; The coiling number of turns is 10 circles, and the diameter of the spirrillum coiling of water preheat pipe 2 is 20cm, and the coiling number of turns is 10 circles; The diameter of the spirrillum coiling of charge heating pipe is 17cm, and the coiling number of turns is 11 circles; Burner 9 is selected the 8KW atmospheric burner of rated output, and fuel is selected Sweet natural gas for use.
After device starts, start burner 9 earlier, the empty reforming reaction device that burns.When catalyst temperature reached 150 ℃ in the reactor body 6, the valve that is provided with on the preheating tubes 2 of fetching boiling water fed water, and the molar flow of water is 70mol/h.Current get into reactor bodies 6 earlier after become overheated steam behind the water preheat pipe 2, threeway 3,12 heating of charge heating pipe through mixed gas inlet 17, are used for purge main body 6, comprise each feed pipe.When catalyst temperature in the reactor body reaches 500 ℃, open the valve that is provided with on the Sweet natural gas preheating tubes 1, in Sweet natural gas preheating tubes 1, feed Sweet natural gas, its flow is got 28mol/h, through threeway 3 Sweet natural gas and water vapour is mixed; Gas mixture is through charge heating pipe 12, and mixed gas inlet 16 gets into reactor body 6; Temperature is at 500～800 ℃ in reactor body 6, and water and Sweet natural gas are at the effect generation steam reformation hydrogen production reaction (CH of catalyzer 6
4+ H
2O=CO+3H
2).It is 630L/H that reaction reaches the flow that stable state is meant Sweet natural gas, and steam/hydrocarbons ratio is about 2.5, and temperature of reaction is about 700 ℃.Hydrogen output is about 1600L/H with this understanding, has satisfied the requirement of the distributed hydrogen gas production of 2 multikilowatt fuel cell systems that is used for family and small business users, has realized the cascade utilization of energy simultaneously, has improved energy utilization efficiency.
Claims (10)
1. a Sweet natural gas steam reformation hydrogen production device that is used for micro fuel cell is characterized in that comprising upper end cover, reactor body, reactor drum upper flange, reactor drum urceolus, burner and preheat coil; Preheat coil comprises Sweet natural gas preheating tubes, water preheat pipe and charge heating pipe; Upper end cover and reactor drum urceolus are the hollow cylinder structure; Preheat coil is arranged in the upper end cover; Reactor body is arranged in the reactor drum urceolus; Burner places the bottom of reactor body; Reactor body is connected through flange with upper end cover with the reactor drum urceolus;
The a plurality of eyelets of said reactor drum upper flange outer shroud uniform distribution, a plurality of eyelets of interior ring uniform distribution; Distribute equally in the position corresponding with the reactor drum upper flange eyelet of equivalent amount of reactor body is connected the reactor drum upper flange through bolt with reactor body; Mixed gas inlet is positioned at reactor drum upper flange left side, and the synthetic gas air outlet is positioned at reactor drum upper flange right side; Mixed gas inlet and charge heating pipe coupling; The synthetic gas escape pipe is connected with the synthetic gas air outlet, is upwards stretched out by upper end cover top; The stack gas escape pipe stretches out from upper end cover top;
Said reactor body is the hollow ring structure, and the center is hollow, and hollow periphery is an annular cavity, and annular cavity is provided with two baffle plates; Two baffle plates are divided into left chamber and right chamber with annular cavity, and the space is arranged at the baffle plate bottom; Granules of catalyst is distributed in left chamber and the right chamber, and granules of catalyst is a nickel-base catalyst; Be provided with the passage of two arcuations at the reactor body top, the passage of arcuation is between the reactor body upper flange outside and reactor drum urceolus inboard; Reactor body and reactor drum upper flange center are provided with through hole;
Sweet natural gas preheating tubes and water preheat pipe get in the upper end cover cavity from upper end cover top; The Sweet natural gas preheating tubes is provided with water preheat pipe inboard in the upper end cover cavity; The helicoidal structure rotation downwards; Sweet natural gas preheating tubes and water preheat pipe are through threeway and charge heating pipe coupling, and the charge heating pipe adopts spirane structure.
2. according to the said device of claim 1, it is characterized in that: the outer shroud of said annular cavity and the correction for semi-diameter of interior ring are the width L=aW of annular cavity, and wherein: W is the width of granules of catalyst, is 4-6mm; A gets 4-6 for adorning the number of catalyzer side by side; The outer ring diameter R of annular cavity
2With interior ring diameter R
1And the annular cavity height H satisfies simultaneously:
A＝pH(R
1+R
2)＝(1.2～1.5)Q/KDT；
Wherein: Q is a steam reaction institute heat requirement, Q=nDH, and n is the molar weight of the required Sweet natural gas of reaction, DH is that unit mole Sweet natural gas and water vapour react needed heat; K is the coefficient of heat transfer between reaction gas and the stack gas; DT is reaction gas and stack gas logarithm heat transfer temperature difference; A is the heat interchanging area of reactor drum; V is the volume of reactor drum annular section; V
1Admission space for catalyzer.
3. according to the said device of claim 1, it is characterized in that: said nickel-base catalyst loadings
Wherein: F is the volumetric flow rate of Sweet natural gas in the virgin gas; V is the carbon space velocity of catalyzer, and the carbon space velocity of catalyzer is 500～1500h
-1
4. according to the said device of claim 1, it is characterized in that: said baffle plate adopts stainless steel to make, and welds together with the reactor body inner and outer ring; The height in said space is 1/10 of a reactor body height.
5. according to the said device of claim 1, it is characterized in that: the width of channel of said arcuation is 1.5～3cm.
6. according to the said device of claim 1, it is characterized in that: the diameter of said preheating tubes is 4～8mm, and the material of preheating tubes material is a copper product.
7. according to the said device of claim 1, it is characterized in that: the said Sweet natural gas preheating tubes and the water preheat pipe helicoidal structure coiling number of turns are the 5-10 circle; The charge heating pipe helicoidal structure coiling number of turns is the 7-12 circle.
8. according to the said device of claim 1, it is characterized in that: the diameter R of said reactor drum urceolus
3=R
2+ (6～12) cm, length is than the long 20-30% of reactor body; R
2Outer ring diameter for annular cavity.
9. according to the said device of claim 1, it is characterized in that: said upper end cover and reactor drum urceolus periphery coat lagging material, and lagging material is a ceramic fiber, and the thickness of lagging material is greater than 10 centimetres.
10. application rights requires the Sweet natural gas steam reformation hydrogen production method of 1 said device, it is characterized in that may further comprise the steps:
The first step, the maintenance reactor pressure is a normal pressure, starts burner, the preheating reactor body, catalyst temperature reaches 150～200 ℃ in reactor body;
Second step fed water through the water preheat pipe, and burner continues heating, catalyst temperature to 500～800 ℃ to the reactor body;
The 3rd step fed Sweet natural gas through the Sweet natural gas preheating tubes, and the ratio of the molar flow of Sweet natural gas is 2～4 in the molar flow of control water and the Sweet natural gas preheating tubes; Water and Sweet natural gas advanced preheating pipe preheating separately respectively after the charge heating pipe is merged into gas mixture; Be preheating to temperature required 500～800 ℃ of reaction; Get in the chamber, a reactor body left side reforming reaction takes place; Get into the then reaction of the right chamber of reactor body through the baffle plate lower space then, the hydrogen-rich gas that final reaction produces is drawn through the synthetic gas escape pipe.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104112866A (en) * | 2013-04-19 | 2014-10-22 | 中国科学院宁波材料技术与工程研究所 | Combustion reforming premixing integrated apparatus for fuel cell system |
| CN104229734A (en) * | 2014-09-03 | 2014-12-24 | 深圳北纯能源科技有限公司 | Reforming hydrogen production reactor and hydrogen production method |
| RU2636726C1 (en) * | 2016-11-24 | 2017-11-27 | Олег Петрович Андреев | Device for vapour catalytic conversion of natural gas into synthetic gas |
| CN113813884A (en) * | 2021-09-29 | 2021-12-21 | 榆林顺为榆成氢能科技有限公司 | Safe and efficient reforming hydrogen production reactor |
| CN114597442A (en) * | 2020-12-03 | 2022-06-07 | 中国科学院大连化学物理研究所 | Quick starting device and method for fuel cell |
| CN115414808A (en) * | 2022-09-19 | 2022-12-02 | 浙江大学 | Shell and tube steam humidifier |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1663908A (en) * | 2004-03-03 | 2005-09-07 | 哈尔滨工业大学 | Natural gas pyrolysis reactor for solid oxide fuel battery |
| CN101054160A (en) * | 2006-04-10 | 2007-10-17 | 中国科学院大连化学物理研究所 | Mini reforming hydrogen-preparation reactor |
| CN101973522A (en) * | 2010-09-29 | 2011-02-16 | 华南理工大学 | Autothermal reforming device for producing hydrogen from natural gas |
| CN102452642A (en) * | 2010-10-27 | 2012-05-16 | 中国科学院大连化学物理研究所 | Compact natural gas reforming hydrogen producing reactor |
| CN202737041U (en) * | 2012-08-24 | 2013-02-13 | 华南理工大学 | Natural gas steam reforming hydrogen production device for micro fuel cells |
-
2012
- 2012-08-24 CN CN201210306523.XA patent/CN102826507B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1663908A (en) * | 2004-03-03 | 2005-09-07 | 哈尔滨工业大学 | Natural gas pyrolysis reactor for solid oxide fuel battery |
| CN101054160A (en) * | 2006-04-10 | 2007-10-17 | 中国科学院大连化学物理研究所 | Mini reforming hydrogen-preparation reactor |
| CN101973522A (en) * | 2010-09-29 | 2011-02-16 | 华南理工大学 | Autothermal reforming device for producing hydrogen from natural gas |
| CN102452642A (en) * | 2010-10-27 | 2012-05-16 | 中国科学院大连化学物理研究所 | Compact natural gas reforming hydrogen producing reactor |
| CN202737041U (en) * | 2012-08-24 | 2013-02-13 | 华南理工大学 | Natural gas steam reforming hydrogen production device for micro fuel cells |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104112866A (en) * | 2013-04-19 | 2014-10-22 | 中国科学院宁波材料技术与工程研究所 | Combustion reforming premixing integrated apparatus for fuel cell system |
| CN104112866B (en) * | 2013-04-19 | 2016-12-28 | 中国科学院宁波材料技术与工程研究所 | The burning of a kind of fuel cell system is reformed and is premixed integrated apparatus |
| CN104229734A (en) * | 2014-09-03 | 2014-12-24 | 深圳北纯能源科技有限公司 | Reforming hydrogen production reactor and hydrogen production method |
| RU2636726C1 (en) * | 2016-11-24 | 2017-11-27 | Олег Петрович Андреев | Device for vapour catalytic conversion of natural gas into synthetic gas |
| CN114597442A (en) * | 2020-12-03 | 2022-06-07 | 中国科学院大连化学物理研究所 | Quick starting device and method for fuel cell |
| CN114597442B (en) * | 2020-12-03 | 2023-11-03 | 中国科学院大连化学物理研究所 | Quick starting device and method for fuel cell |
| CN113813884A (en) * | 2021-09-29 | 2021-12-21 | 榆林顺为榆成氢能科技有限公司 | Safe and efficient reforming hydrogen production reactor |
| CN115414808A (en) * | 2022-09-19 | 2022-12-02 | 浙江大学 | Shell and tube steam humidifier |
| CN115414808B (en) * | 2022-09-19 | 2024-05-28 | 浙江大学 | Shell-and-tube type water vapor humidifier |
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| CN102826507B (en) | 2014-12-31 |
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