CN100417588C - Process of preparing high purity hydrogen with liquid hydrocarbon in a palladium film reactor - Google Patents
Process of preparing high purity hydrogen with liquid hydrocarbon in a palladium film reactor Download PDFInfo
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- CN100417588C CN100417588C CNB200510086418XA CN200510086418A CN100417588C CN 100417588 C CN100417588 C CN 100417588C CN B200510086418X A CNB200510086418X A CN B200510086418XA CN 200510086418 A CN200510086418 A CN 200510086418A CN 100417588 C CN100417588 C CN 100417588C
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Abstract
The process of preparing high purity hydrogen with liquid hydrocarbon in a palladium film reactor adopts Ni base catalyst with high activity at low temperature to obtain liquid hydrocarbon converting rate near 100 % at the conditions of 450-550 deg.c temperature and carbon space velocity as high as 30,000/hr, and uses high performance composite metal palladium film simultaneously at the conditions of 500-600 deg.c temperature and carbon space velocity as high as 2000/hr for timely separating hydrogen generated through water vapor reformation of liquid hydrocarbon to avoid methanation reaction, so as to obtain methane selectivity lower than 3 % and hydrogen selectivity higher than 97 % and obtain high pure hydrogen in the permeation side of the palladium film. The present invention has low hydrogen producing cost and may be used widely in hydrogen refilling station and small dispersed power station.
Description
Technical field
The present invention relates to a kind of liquefied hydrocarbon and produce the method for high-purity hydrogen in palladium film reactor, specifically, employing has highly active Ni base hydrocarbon steam reforming catalyst at low temperatures and produce high-purity hydrogen in high-performance composition metal palladium film reactor.Originally produce the method for high-purity hydrogen, will and disperse the power station to obtain widespread use aspect the hydrogen manufacturing on a small scale at the hydrogenation station, and for the hydrogenation station with disperse the power station that cheap hydrogen producing technology is provided.
Background technology
Energy shortage, efficiency of energy utilization is low and environmental pollution that caused thus, is just becoming the important restraining factors of human social.Active development new forms of energy and renewable energy source are the basic outlets that solves energy problem.Hydrogen is as a kind of secondary energy carrier, has cleaning, pollution-free, plurality of advantages such as efficient is high, application form is many, thereby it is received much attention.Simultaneously, at the Hydrogen Energy conversion aspect, proton membrane fuel battery is also because of advantage is subjected to day by day people's such as its energy conversion efficiency height, environmental friendliness, assembling be flexible very big concern.In addition, Hydrogen Technology can realize CO
2Focus on and seal up for safekeeping, can realize the CO of fossil energy trans-utilization
2Near zero release, enter the nineties in 20th century after, especially in recent years, some countries obviously accelerated the research and development paces of Hydrogen Energy.The development of clean Hydrogen Technology and proton membrane fuel battery power truck is particularly noticeable.At present, fuel cell electric vehicle has been taken leave of concept car.Therefore, provide hydrogen fuel extremely urgent for fuel cell electric vehicle.In recent years, abroad begun to pay attention to carry out the corresponding techniques research and development for setting up the hydrogenation station.
As everyone knows, for extensive hydrogen manufacturing, gas water steam reformation (SMR) is successfully realized suitability for industrialized production already, and the cost of its extensive hydrogen manufacturing is US$1/kg.Yet when the scale of the steam reformation of multistep process was reduced to the hydrogenation station or disperses the needed small-scale in power station, it is about 90% that fixed cost will reach the hydrogen total production cost, and the hydrogen manufacturing cost will reach about US$11/kg.
Therefore, existing gas water steam reformation hydrogen production and conventional low temperature separation process or transformation fractionation by adsorption purified hydrogen technology, although technology maturation and playing a significant role in the scale hydrogen production process of chemical plant can't satisfy fuel-cell vehicle or disperse the demand of power station to small-scale hydrogen manufacturing.
The gas water steam reformation is the reaction that is subjected to thermodynamics equilibrium limit, and in order to obtain higher conversion of natural gas rate, temperature of reaction is more than 850 ℃ usually, and this has proposed very high requirement to reactor apparatus.People have carried out big quantity research to gas water steam reforming reaction in the palladium film reactor, wish by the palladium film hydrogen of producing in time to be separated, thereby make chemical equilibrium move right, and are implemented in the higher hydrogen production efficiency of acquisition under the relatively low temperature.As people (SteamReforming of Methane in a Hydrogen-Permeable Membrane Reactor such as Shigeyuki Uemiya, Appl.Catal.67,223,1991), under the 623-773K lesser temps, adopt the catalyst based realization methane steam reformation reaction in palladium film reactor of Ni.U.S Pat.No.5 for another example, 525,322 have proposed to reclaim hydrogen and isotopic method thereof from water and hydro carbons, adopt palladium film and nickel-base catalyst, by the hydrogen that generates is in time separated, make the CO water gas shift reation:
Perhaps methane steam reformation reaction
Perhaps methane cracking reaction:
Almost realized transforming fully under less raw gas flow condition, still, under higher raw gas flow condition, the rate of recovery of hydrogen obviously reduces, and has seriously limited the hydrogen capacity of device.
Liquefied hydrocarbon has high energy density, is easy to transport and store, and is one of important source material of hydrogen manufacturing on a small scale.Usually, liquefied hydrocarbon steam reformation or catalyzing part oxidation need can obtain high hydrocarbon conversion rate and hydrogen production efficiency under the temperature more than 800 ℃.
The inventor discovers, if when temperature of reaction is reduced to 500 ℃ of left and right sides, methane will be its primary product, and its reaction mechanism is as follows:
C
mH
n+H
2O→H
2+CO+CO
2 (1)
H
2+CO+CO
2→CH
4+H
2O (2)
Because the hydrogen that the liquefied hydrocarbon steam reformation produces under the low temperature about 500 ℃, will with the CO and the CO that generate simultaneously
2Carry out methanation reaction, thereby generate a large amount of CH
4, make hydrogen production efficiency lower.Therefore, if the H that the liquefied hydrocarbon steam reformation can be generated about 500 ℃
2In time separate, just can avoid the generation of methanation reaction, improve hydrogen production efficiency.The key that realizes this reaction-isolation integral mainly contains two aspects: (1) has highly active steam reformation catalyzer under about 500 ℃ of low temperature; (2) has the high-performance composition metal palladium film of high saturating hydrogen amount and high hydrogen permeation selectivity.
The advantage of utilizing the palladium metal film to reclaim the hydrogen of hydrogen production process generation is generally accepted by people.United States Patent (USP) U.S.Pat.No.5,741,474 have proposed a kind of method and apparatus of producing high-purity hydrogen.In the reformation chamber of a heating, carry out hydro carbons or oxidation of alcohols steam reforming reaction, hydro carbons or alcohols, water, oxygen or air join in the reactor, and steam reformation and partial oxidation reaction take place, and the gas of generation passes through hydrogen separation membrane, obtain highly purified hydrogen, and the heat that impermeable gas contained is used for heating and the reformation hydro carbons, water, and air or oxygen.Do not mention membrane permeability in this patent and can and install hydrogen capacity.United States Patent (USP) U.S.Pat.No.5,861,137 have proposed the membrane reactor of steam reforming reaction, and raw material is alcohols or hydro carbons and water, by the hydrogen separation membrane recover hydrogen of tubular type.Because the permselective property of the film that uses is poor, in the per-meate side of film, need to load methanation catalyst, or even the steam reforming catalyzer is eliminated the raw material leakage of membrane permeation side or the CO that sees through
xIn the outside of reforming reaction, utilize catalyst combustion reaction tail gas to come to provide heat for reaction.This patent is not mentioned the throughput that membrane permeability can and install.
In a word, it is more to carry out the report of gas water steam reforming reaction in palladium film reactor.To have highly active Ni at low temperatures catalyst based and utilize, make under low temperature and high-speed and to obtain liquefied hydrocarbon transformation efficiency near 100%, and utilize high-performance composition metal palladium film simultaneously, the hydrogen that makes the liquefied hydrocarbon steam reformation generate is in time separated and is avoided the generation of methanation reaction, thereby obtains lower methane selectively and higher hydrogen selective does not still have report.
Summary of the invention
The object of the present invention is to provide a kind of liquefied hydrocarbon in palladium film reactor, to produce the method for high-purity hydrogen.
The present invention adopts that to have highly active high Ni content Ni at low temperatures catalyst based, makes at 450 ℃～550 ℃ low temperature and carbon space velocity up to 30 000h
-1Condition under can obtain liquefied hydrocarbon near 100% transformation efficiency.Use the saturating hydrogen amount for preparing by own patented technology greater than 50m simultaneously
3/ m
2Hbar and H
2/ N
2Separation factor is greater than 10000 high-performance composition metal palladium film, at 500 ℃～600 ℃ of temperature and carbon space velocity up to 2000h
-1Under the condition, the hydrogen that makes the liquefied hydrocarbon steam reformation generate is in time separated and is avoided the generation of methanation reaction, thereby obtains to be lower than 3% methane selectively and be higher than 97% hydrogen selective, sees through side at the palladium film and obtains high-purity hydrogen.
For realizing purpose of the present invention, liquefied hydrocarbon provided by the invention is produced the method for high-purity hydrogen in palladium film reactor, and step is as follows:
A), pack in the composition metal palladium film reactor according to the synoptic diagram shown in the accompanying drawing 1 with Ni base hydrocarbon steam reforming catalyst;
B) under the hydrogen condition, the system that heats up makes the catalyst based reduction of Ni for 550 ℃;
C) be not less than under the 0.5MPa condition, in 500 ℃-600 ℃ of temperature and pressure H
2O/C is than being that 1.8～4 liquefied hydrocarbon and water vapor feed in the composition metal palladium film reactor and react;
D) the hydrogen selective ground of reaction generation sees through composition metal palladium film, is seeing through side acquisition high-purity hydrogen.
It is catalyst based to have highly active Ni under the low temperature that the present invention adopts, and is to adopt the coprecipitation method preparation, has high Ni content, and NiO content is between 25wt%-70wt%, and is relatively good between 30wt%-50wt%.Adopt this Ni catalyst based, at the liquefied hydrocarbon carbon space velocity up to 30,000h
-1The time, under 450～550 ℃ cold condition, liquefied hydrocarbon almost can transform fully, and product is formed and is formed near thermodynamic(al)equilibrium.Ni is catalyst based to be added with one or both oxide compounds among metal La and the Mg as auxiliary agent.
Employing liquefied hydrocarbon efficient cryogenic provided by the invention is produced the method for high-purity hydrogen, will and disperse the power station to obtain widespread use aspect the hydrogen manufacturing on a small scale at the hydrogenation station, and for the hydrogenation station with disperse the power station that cheap hydrogen producing technology is provided.The carbon atom number N of component is in the hydro carbons: 4＜N＜16.Liquefied hydrocarbon is single hydrocarbon compound or hydro carbons miscellany.
Description of drawings
Liquefied hydrocarbon steam reforming hydrogen manufacturing synoptic diagram in Fig. 1 composition metal palladium film reactor.
Embodiment
The invention will be further described below in conjunction with embodiment and Comparative Examples.Need to prove for embodiment, its effect just further specifies technical characterictic of the present invention, rather than limits the present invention.
For sake of convenience, the spy is defined as follows product methane selectively and hydrogen selective:
Methane selectively=100 * [product methane flow * 2/ (product methane flow * 2+ product hydrogen flowing quantity)]
Hydrogen selective=100 * [product hydrogen flowing quantity/(product methane flow * 2+ product hydrogen flowing quantity)]
Embodiment 1:
With Ni (NO
3)
26H
2O and Al (NO
3)
39H
2O is a raw material, adopts (NH
4)
2CO
3Be precipitation agent, control the temperature of two kinds of solution and carry out co-precipitation about room temperature, keep pH in the precipitation process 8.0～8.5, precipitation finishes the aging 2h in back, and washes clean is dry under 120 ℃ then, 600 ℃ of following roasting 4h.NiO content is at 40wt% in the control catalyst, Al
2O
3Be 60wt%.Get above-mentioned catalyzer 5.5g, with the quartz sand dilution, in the palladium film reactor of packing into, the high 100mm of bed.The hydrogen infiltration rate of the composite metal membrane of selecting for use is 52m
3m
-2Bar
-1h
-1, H
2/ N
2Separation factor is more than 10,000.The 6# solvent oil of producing with grand celebration is a raw material, the speed 0.34ml/min of fuel sample introduction, water sample rate 0.80ml/min.Be reflected at 550 ℃, 1.1MPa introduces sweep gas Ar in the side that sees through of film, and the speed of sweep gas is 1.8 with the C feeding rate than (being scaled under the standard state gas).The result shows that the product methane selectively is 2.8%, and hydrogen selective is 97.2%.See through the purity of side hydrogen behind deduction sweep gas Ar greater than 99.9%.
Embodiment 2:
With Ni (NO
3)
26H
2O, Al (NO
3)
39H
2O and La (NO
3)
36H
2O is a raw material, adopts coprecipitation method to prepare Ni/La-Al
2O
3Catalyzer is with NH
3H
2O is a precipitation agent, and about the pH=8.0 of control precipitation process, precipitation process finished the back aging 1 hour, centrifuge washing, and then 120 ℃ of dryings, 600 ℃ of roastings 4 hours prepare and consist of 50wt%NiO, 42wt%Al
2O
3, and 8wt%La
2O
3Catalyzer.In conventional fixed-bed reactor, be raw material with the octane-iso, at 450 ℃, 500 ℃, the 550 ℃ performances of measuring catalyzer respectively, the S/C=2.73 in the reaction process, pressure P=0.8MPa.Table 1 presentation of results, prepared catalyzer have good water at low temperature steam reformation activity, though carbon space velocity up to 30,000h
-1, under 450 ℃, 500 ℃ and 550 ℃ of temperature, liquefied hydrocarbon all can be realized the transformation efficiency near 100%, the product butt is formed near thermodynamic equilibrium value.Simultaneously as seen, when lesser temps, the content that generates methane is higher.
Table 1:
Further in membrane reactor, load the above-mentioned catalyzer of 5.5g, particle diameter 420-630 μ m, with the quartz sand dilution, the high 100mm of filling bed.The hydrogen infiltration rate 58m of the composition metal palladium film of selecting for use
3m
-2Bar
-1h
-1, H
2/ N
2Separation factor is more than 10,000.With the octane-iso is raw material.Octane-iso sample rate 0.34ml/min, water sample rate 0.80ml/min.Be reflected at 550 ℃, 1.3MPa carries out, and the speed of sweep gas is 1.8 with the C feeding rate than (being scaled under the standard state gas).The result shows that the product methane selectively is 2.3%, and hydrogen selective is 97.7%.See through the purity of side hydrogen behind deduction sweep gas Ar greater than 99.9%.
Embodiment 3:
With Ni (NO
3)
26H
2O, Al (NO
3)
39H
2O and Mg (NO
3)
26H
2O is a raw material, adopts (NH
4)
2CO
3Be precipitation agent, control the temperature of two kinds of solution and carry out co-precipitation about room temperature, keep pH in the precipitation process 8.0～8.5, precipitation finishes the aging 2h in back, and washes clean is dry under 120 ℃ then, 700 ℃ of following roasting 4h.Catalyzer consist of 36wt%NiO, 12wt%MgO and 52wt%Al
2O
3, the catalyzer of preparation is got the Ni/MgO-Al that particle diameter is 420-630 μ m through crushing and screening again behind the compression molding
2O
3Catalyzer 5.5g is with the palladium film reactor of packing into after the quartz sand dilution, the high 100mm of filling bed.The hydrogen infiltration rate of the composite metal membrane of selecting for use is 65m
3m
-2Bar
-1h
-1, H
2/ N
2Separation factor is more than 10,000.As raw material, be reflected at the liquefied hydrocarbon carbon space velocity with octane-iso up to 2000h
-1, 550 ℃ of temperature, H
2The O/C ratio is 2.73, carries out under the pressure 1.7MPa condition.The speed of sweep gas is 1.8 with the C feeding rate than (being scaled under the standard state gas).The result shows that the product methane selectively is 1.8%, and hydrogen selective is 98.2%.See through the purity of side hydrogen behind deduction sweep gas Ar greater than 99.9%.
Embodiment and comparative example 4:
Get the Ni/MgO-Al of embodiment 3
2O
3Catalyzer 5.5g, in conventional stainless steel reactor, be that raw material carries out steam reforming reaction with the octane-iso, the sample rate of liquid fuel is 0.17ml/min, the feeding rate of water is 0.40ml/min, be reflected at 550 ℃, carry out under the 0.9MPa, the butt of the product of generation is formed as shown in table 2, as seen, although liquefied hydrocarbon almost 100% transforms, the methane selectively that generates is up to 62%, and the selectivity of hydrogen has only 38%.
Table 2:
| Component | H 2 | CO | CH 4 | CO 2 |
| Content | 42％ | 2.3％ | 34.2％ | 21.5％ |
And adopt the technology of the present invention route, under same reaction conditions, the hydrogen infiltration rate of the composite metal membrane of selecting for use is 68m
3m
-2Bar
-1h
-1, H
2/ N
2Separation factor is more than 10,000, adopts sweep gas Ar in the side that sees through of film, and the speed of sweep gas is 1.8 with the C feeding rate than (being scaled under the standard state gas), and at this moment the gas composition of Sheng Chenging is as shown in table 3.As seen, compare, adopt palladium film reactor can reduce methane selectively (2.6%) significantly, improve the selectivity (97.4%) of hydrogen with the popular response device.
Table 3:
| Component | H 2 | CO | CH 4 | CO 2 |
| Content | 75.3％ | 1.34％ | 1.00％ | 22.4％ |
Claims (5)
1. a liquefied hydrocarbon is produced the method for high-purity hydrogen in palladium film reactor, it is characterized in that, adopts the Ni that to have highly active NiO content at low temperatures be 25-70wt% catalyst based, makes at 450 ℃～550 ℃ low temperature and carbon space velocity up to 30 000h
-1Condition under can obtain liquefied hydrocarbon near 100% transformation efficiency; Use the hydrogen amount greater than 50m
3/ m
2Hbar and H
2/ N
2Separation factor is greater than 10000 high-performance composition metal palladium film, at 500 ℃～600 ℃ of temperature and carbon space velocity up to 2000h
-1Under the condition, the hydrogen that makes the liquefied hydrocarbon steam reformation generate is in time separated and is avoided the generation of methanation reaction, thereby obtains to be lower than 3% methane selectively and be higher than 97% hydrogen selective, sees through side at the palladium film to obtain high-purity hydrogen; Described method comprises the following steps:
A) Ni is catalyst based, in the composition metal palladium film reactor of packing into;
B) under the hydrogen condition, be warming up to 550 ℃ and make the catalyst based reduction of Ni;
C) be not less than under the 0.5MPa condition, in 500 ℃-600 ℃ of temperature and pressure H
2O/C is than being that 1.8～4 liquefied hydrocarbon and water vapor feed in the composition metal palladium film reactor and react;
D) the hydrogen selective ground of reaction generation sees through composition metal palladium film, is seeing through side acquisition high-purity hydrogen.
2. in accordance with the method for claim 1, it is characterized in that NiO content was 30-50wt% during described Ni was catalyst based.
3. in accordance with the method for claim 1, it is characterized in that one or both oxide compounds among described Ni catalyst based interpolation metal La and the Mg are as auxiliary agent.
4. in accordance with the method for claim 1, it is characterized in that the carbon atom number N of component is in the hydro carbons: 4＜N＜16.
5. in accordance with the method for claim 1, it is characterized in that described liquefied hydrocarbon is single hydrocarbon compound or hydro carbons miscellany.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510086418XA CN100417588C (en) | 2005-09-14 | 2005-09-14 | Process of preparing high purity hydrogen with liquid hydrocarbon in a palladium film reactor |
| PCT/GB2006/003305 WO2007031713A1 (en) | 2005-09-14 | 2006-09-07 | Process for hydrogen production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510086418XA CN100417588C (en) | 2005-09-14 | 2005-09-14 | Process of preparing high purity hydrogen with liquid hydrocarbon in a palladium film reactor |
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| CN1931708A CN1931708A (en) | 2007-03-21 |
| CN100417588C true CN100417588C (en) | 2008-09-10 |
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| CN101836318B (en) * | 2007-10-25 | 2013-02-27 | Utc电力公司 | Reduced generation of ammonia in nickel catalyst of reformer |
| US8961627B2 (en) * | 2011-07-07 | 2015-02-24 | David J Edlund | Hydrogen generation assemblies and hydrogen purification devices |
| CN102431970A (en) * | 2011-09-13 | 2012-05-02 | 昆明理工大学 | Method for preparing hydrogen gas through transferring water vapor through oxygen carrying catalysis membranes |
| CN102674247B (en) * | 2012-04-28 | 2016-06-01 | 浙江大学 | A kind of method of decarburization and the dual forced methane steam reforming hydrogen manufacturing of dehydrogenation and device |
| US10717040B2 (en) | 2012-08-30 | 2020-07-21 | Element 1 Corp. | Hydrogen purification devices |
| US9187324B2 (en) | 2012-08-30 | 2015-11-17 | Element 1 Corp. | Hydrogen generation assemblies and hydrogen purification devices |
| US20140065020A1 (en) | 2012-08-30 | 2014-03-06 | David J. Edlund | Hydrogen generation assemblies |
| US11738305B2 (en) | 2012-08-30 | 2023-08-29 | Element 1 Corp | Hydrogen purification devices |
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| CN110817794B (en) * | 2019-10-28 | 2023-08-01 | 中科液态阳光(苏州)氢能科技发展有限公司 | Hydrogen separation and water gas reforming integrated ultrahigh pressure hydrogen production system and method thereof |
| CN110817795B (en) * | 2019-10-28 | 2023-08-01 | 中科液态阳光(苏州)氢能科技发展有限公司 | Hydrogen separation and water gas reforming integrated medium pressure hydrogen production system and method thereof |
| CN110817796B (en) * | 2019-10-28 | 2023-08-01 | 中科液态阳光(苏州)氢能科技发展有限公司 | Methanol steam reforming and hydrogen separation integrated low-pressure hydrogen preparation system and method thereof |
| CN110835095B (en) * | 2019-10-28 | 2023-08-18 | 中科院大连化学物理研究所张家港产业技术研究院有限公司 | Methanol steam reforming and hydrogen separation integrated high-pressure hydrogen preparation system and method thereof |
| CN110902652A (en) * | 2019-11-20 | 2020-03-24 | 中国科学院广州能源研究所 | On-line separation reforming hydrogen production method capable of enhancing reaction efficiency and device for implementing method |
| CN111632616A (en) * | 2020-07-06 | 2020-09-08 | 中国石油化工股份有限公司 | Liquid catalyst and application thereof |
| CN113214872B (en) * | 2021-03-21 | 2023-05-05 | 苏州铧泷磬能新能源科技有限公司 | Heat accumulating type coal gasification hydrogen production hydrogen permeation membrane reactor |
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| US5525322A (en) * | 1994-10-12 | 1996-06-11 | The Regents Of The University Of California | Method for simultaneous recovery of hydrogen from water and from hydrocarbons |
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-
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- 2005-09-14 CN CNB200510086418XA patent/CN100417588C/en not_active Expired - Fee Related
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5741474A (en) * | 1994-05-23 | 1998-04-21 | Ngk Insulators, Ltd. | Process for production of high-purity hydrogen |
| US5525322A (en) * | 1994-10-12 | 1996-06-11 | The Regents Of The University Of California | Method for simultaneous recovery of hydrogen from water and from hydrocarbons |
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