CN2725267Y - Serial Fluidized bed biomass gasification hydrogen making device - Google Patents
Serial Fluidized bed biomass gasification hydrogen making device Download PDFInfo
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- CN2725267Y CN2725267Y CNU200420079615XU CN200420079615U CN2725267Y CN 2725267 Y CN2725267 Y CN 2725267Y CN U200420079615X U CNU200420079615X U CN U200420079615XU CN 200420079615 U CN200420079615 U CN 200420079615U CN 2725267 Y CN2725267 Y CN 2725267Y
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/145—Feedstock the feedstock being materials of biological origin
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Abstract
Disclosed is a serial fluidized bed biomass gasification hydrogen making device, which is a hydrogen making device by biomass catalysis, decomposition and gasification. The device is composed of a circulating fluidized bed, a cyclone separator and a bubbling fluidized bed, which are connected in series. The upper part of the circulating fluidized bed (1) is connected with the upper part of the cyclone separator (2), and the side at the lower part of the circulating fluidized bed (1) is connected with the bubbling fluidized bed (3). A biomass granule feed inlet (B) is arranged on the side at the lower part of the circulating fluidized bed (1), and a water vapour inlet (A) is arranged at the bottom of the circulating fluidized bed (1), and the bed fuels in the circulating fluidized bed (1) are calcia/magnesia granules of catalyst (11). A hydrogen-rich gas air outlet (C) is arranged on the top of the cyclone separator (2), and a feed outlet tube (21) at the lower part of the cyclone separator (2) is inserted into the bubbling fluidized bed (3). A smoke gas air outlet (D) is arranged on the top of the bubbling fluidized bed (3), and an air/oxygen inlet (E) is arranged at the bottom of the bubbling fluidized bed (3), and the bed fuels in the bubbling fluidized bed (3) are calcium carbonate/magnesium carbonate granules (31).
Description
Technical field
The utility model is a kind of device for producing hydrogen of biomass catalytic pyrolysis gasification, and especially a kind of employing circulating fluidized bed carries out the biomass-making hydrogen production device.
Background technology
Hydrogen is not only important industrial raw material, and is the optimal following clean energy carrier of generally acknowledging.Production, processing and the transportation of fossil oil (coal, oil, Sweet natural gas) all can cause in various degree pollution to environment, and gases such as carbonic acid gas that its burning generates and sulfurous gas produce Greenhouse effect and acid rain again respectively; Utilize reproducible biomass resource hydrogen manufacturing, ensure power supply safety, satisfy the requirement of industrial and agricultural production Sustainable development.
As a kind of low-carbon (LC) clean fuel, biomass have the volatile content height, the carbon activity height, 0.1～5%) low (sulphur: 0.1～1.5%, nitrogen: 0.5～3%, ash: advantage such as of sulphur, nitrogen and the ash content of coal, and its growth and utilize process just in time can realize carbon dioxide zero discharge, this is that fossil oil is incomparable.
Prior biological matter hydrogen production process mainly can be divided into biochemical process and thermochemistry (pyrolytic gasification) method two big classes, and biochemical reaction speed is slow, and the large-scale production difficulty is bigger; Thermochemical method has more advantage at aspects such as efficient, cost and mass-producings.The biomass pyrogenation gasification method has air gasification, oxygen-rich gasification and water vapor gasification, and when wherein selecting water vapor as vaporized chemical, hydrogen richness is the highest in the gasification product.
The reactor of prior biological matter water vapor catalyse pyrolysis/gasification hydrogen-producing adopts fixed bed and fluidized-bed, in the fixed-bed reactor between biomass and the catalyzer heat and mass speed low, biomass are difficult to fast pyrogenation, and the catalyst deactivation problem is serious; Heat and mass speed is big in the fluidized-bed reactor, but granules of catalyst surface carbon deposit is serious, makes rapid catalyst deactivation.In addition, the biomass water vapor gasification reaction produces the carrying out that a large amount of carbonic acid gas suppresses the biomass-making H-H reaction, is difficult to realize biomass efficient hydrogen manufacturing.
Summary of the invention
Technical problem: the purpose of this utility model provides and a kind ofly biomass pyrogenation gasification hydrogen manufacturing and the separated biomass-gasifying hydrogen generating serial fluid bed apparatus of coke combustion can realize biomass efficient hydrogen manufacturing with this device, and device structure is can simple.
Technical scheme: be specially biomass pyrogenation gasification and adopt circulating fluidized bed, bubbling fluidized bed is adopted in the coke burning, the combustion processes of biomass pyrogenation gasification hydrogen manufacturing and coke is separated, relied on calcium oxide/magnesium oxide and lime carbonate/hydrotalcite particle thereof to carry out the heat transmission between two; The not only catalysis biomass pyrolytic gasification hydrogen manufacturing of calcium oxide in circulating fluidized bed/magnesia catalyst particle, and carbon dioxide in the gasification product is cured reaction, quicken the carrying out of biomass-making H-H reaction, realize the hydrogen manufacturing of catalytic pyrolysis of biomass gasification high efficient.
Biomass-gasifying hydrogen generating serial fluid bed apparatus of the present utility model, be by circulating fluidized bed, cyclonic separator and bubbling fluidized bed are composed in series, it is characterized in that in the circulating fluidized bed, the bed material is calcium oxide/magnesia catalyst particle, adopt the water vapor fluidisation, biological particles adds in the circulating fluidized bed, carry out the pyrolytic gasification hydrogen production reaction, calcium oxide/magnesia catalyst particle is the reforming reaction of catalytic tar and water vapor both, generate and do not contain tar or tar content hydrogen-rich gas seldom, simultaneously again with gas-phase product in carbonic acid gas be cured reaction, generate lime carbonate/hydrotalcite particle; The coke granule that lime carbonate/hydrotalcite particle and biomass pyrolytic produce enters bubbling fluidized bed after cyclonic separator separates; Bubbling fluidized bed adopts the air/oxygen fluidisation, and coke granule and air/oxygen are burnt, and impel lime carbonate/magnesiumcarbonate calcining and decomposing, discharge carbonic acid gas; On the other hand, be adsorbed on lip-deep carbon deposit of lime carbonate/magnesiumcarbonate and air/oxygen and carry out combustion reactions, the catalyzer of inactivation is regenerated; High temperature oxidation calcium/magnesia catalyst particle after the calcination and regeneration turns back in the circulating fluidized bed, and the form biomass pyrolysis gasification hydrogen-producing provides regenerated catalyzer and thermal source.Its concrete structure is: the top of circulating fluidized bed is connected with the top of cyclonic separator, the discharge nozzle of cyclonic separator bottom inserts in the bubbling fluidized bed, the top of cyclonic separator is the hydrogen-rich gas air outlet, the bottom of circulating fluidized bed is connected with bubbling fluidized bed, the top of bubbling fluidized bed is coke incendiary flue gas air outlet, the bottom of circulating fluidized bed is the water vapor inlet mouth, the bubbling fluidized bed bottom is the air/oxygen inlet mouth, and the bottom of circulating fluidized bed is provided with the biological particles charging opening.
Biomass-gasifying hydrogen generating serial fluid bed method of the present utility model is: biological particles is added in the circulating fluidized bed, biological particles and water vapor, calcium oxide/magnesia catalyst particle acutely mixes, intensive heat and mass exchange take place, make the biological particles instantaneously heating that has just entered bed to the interior temperature (650～900 ℃) of bed, Mierocrystalline cellulose mainly produces volatile matter and tar in the biomass, xylogen mainly is decomposed into coke granule in the biomass, coke granule further with water vapor generation water-gas reaction, calcium oxide/magnesia catalyst particle is the reforming reaction of catalytic tar and water vapor both, generate and do not contain tar or tar content hydrogen-rich gas seldom, simultaneously again with gas-phase product in carbonic acid gas be cured reaction, generate lime carbonate/hydrotalcite particle, quicken the carrying out of biomass-making H-H reaction, remaining gas-entrained lime carbonate/hydrotalcite particle, and coke granule enters cyclonic separator together, reject water after the clean gas condensation that cyclonic separator is discharged, obtain hydrogen-rich gas; Lime carbonate/the hydrotalcite particle and the coke granule that separate through cyclonic separator enter bubbling fluidized bed, and coke granule and be adsorbed on the lip-deep carbon deposit of lime carbonate/hydrotalcite particle and air/oxygen is carried out combustion reactions is regenerated to the catalyzer of inactivation; The high temperature that the coke burning produces impels lime carbonate/magnesiumcarbonate calcining and decomposing, discharge carbonic acid gas, high temperature oxidation calcium/magnesia catalyst particle after the calcination and regeneration turns back in the circulating fluidized bed, and both the form biomass pyrolysis gasification hydrogen-producing provided the regenerated catalyzer, and thermal source is provided again; In whole biomass gasifying hydrogen making reaction process, circulating fluidized bed is in 650～900 ℃ middle temperature state, bubbling fluidized bed is in 850～1100 ℃ of conditions of high temperature, relies on calcium oxide/magnesium oxide and lime carbonate/hydrotalcite particle thereof to carry out the heat transmission between circulating fluidized bed and the bubbling fluidized bed.Also can contain Ni-basedly in described calcium oxide/magnesia catalyst, become calcium oxide/magnesium oxide-nickel-base catalyst.
Technique effect: conventional biomass fluid bed gasification hydrogen-producing, with quartz sand is the bed material, the mixed gas of air (oxygen), water vapor or oxygen and water vapor is a fluidizing agent, the tar that biomass pyrolytic produces is gaseous state when high temperature, mix fully with synthetic gas, (be lower than 200 ℃) and be condensed into liquid when low temperature, its separation and processing be difficulty very; In addition, carbonic acid gas suppresses the carrying out of biomass gasifying hydrogen making reaction in the gasification product, makes the biomass hydrogen preparation inefficiency.
The utility model is a kind of device for producing hydrogen of biomass catalytic pyrolysis gasification, be specially biomass pyrogenation gasification and adopt circulating fluidized bed, bubbling fluidized bed is adopted in the coke burning, the combustion processes of biomass pyrogenation gasification hydrogen manufacturing and coke is separated, relied on calcium oxide/magnesium oxide and lime carbonate/hydrotalcite particle thereof to carry out the heat transmission between two; In circulating fluidized bed endogenous substance pyrolytic gasification hydrogen production process, calcium oxide/magnesia catalyst particle is the reforming reaction of catalytic tar and water vapor both, generate and do not contain tar or tar content hydrogen-rich gas seldom, simultaneously again with gas-phase product in carbonic acid gas be cured reaction, generate lime carbonate/hydrotalcite particle, quicken the carrying out of biomass-making H-H reaction, realize the hydrogen manufacturing of catalytic pyrolysis of biomass gasification high efficient; In bubbling fluidized bed, coke granule and carry out combustion reactions at lip-deep carbon deposit of lime carbonate/hydrotalcite particle and air/oxygen at the circulating fluidized bed internal adsorption is regenerated to the catalyzer of inactivation; The high temperature that the coke burning produces impels lime carbonate/magnesiumcarbonate calcining and decomposing, discharge carbonic acid gas, high temperature oxidation calcium/magnesia catalyst particle after the calcination and regeneration turns back in the circulating fluidized bed, both the form biomass pyrolysis gasification hydrogen-producing provided the regenerated catalyzer, thermal source is provided again, and its device and method has social benefit and prospects for commercial application widely.
Description of drawings
Fig. 1 is an apparatus structure synoptic diagram of the present utility model.Circulating fluidized bed 1 is wherein arranged, calcium oxide/magnesia catalyst particle 11, cyclonic separator 2, the discharge nozzle 21 of cyclonic separator, bubbling fluidized bed 3, lime carbonate/hydrotalcite particle 31, water vapor inlet mouth A, biological particles charging opening B, hydrogen-rich gas air outlet C, flue gas air outlet D, air/oxygen inlet mouth E.
Embodiment
Biomass-gasifying hydrogen generating serial fluid bed apparatus of the present utility model is to be composed in series by circulating fluidized bed 1, cyclonic separator 2 and bubbling fluidized bed 3.Circulating fluidized bed 1 top is connected with the top of cyclonic separator 2, the bottom of circulating fluidized bed 1 is connected with bubbling fluidized bed 3, the bottom of circulating fluidized bed 1 also is provided with biological particles charging opening B, the bottom of circulating fluidized bed 1 is provided with water vapor inlet mouth A, and the bed material is calcium oxide/magnesia catalyst particle 11 in the circulating fluidized bed 1; The top of cyclonic separator 2 is hydrogen-rich gas air outlet C, and the discharge nozzle 21 of cyclonic separator 2 bottoms inserts in the bubbling fluidized bed 3; The top of bubbling fluidized bed 3 is flue gas air outlet D, and bubbling fluidized bed 3 bottoms are air/oxygen inlet mouth E, and the bed material is lime carbonate/hydrotalcite particle 31 in the bubbling fluidized bed 3.
In circulating fluidized bed 1, biological particles and water vapor are carried out the pyrolytic gasification reaction, Mierocrystalline cellulose mainly produces volatile matter and tar in the biomass, xylogen mainly is decomposed into coke granule in the biomass, coke further with water vapor generation water-gas reaction, calcium oxide/magnesia catalyst particle 11 is the reforming reaction of catalytic tar and water vapor both, generate and do not contain tar or tar content hydrogen-rich gas seldom, simultaneously again with gas-phase product in carbonic acid gas be cured reaction, generate lime carbonate/hydrotalcite particle, quicken the carrying out of biomass-making H-H reaction, remaining gas-entrained lime carbonate/hydrotalcite particle, and coke granule enters cyclonic separator 2 together.
Lime carbonate/the hydrotalcite particle and the coke granule that separate through cyclonic separator enter bubbling fluidized bed 3, coke granule and be adsorbed on the lip-deep carbon deposit of lime carbonate/magnesiumcarbonate and air/oxygen is carried out combustion reactions, the high temperature that the coke burning produces impels lime carbonate/magnesiumcarbonate 31 calcining and decomposing, discharge carbonic acid gas, high temperature oxidation calcium/magnesia catalyst particle after the calcination and regeneration turns back in the circulating fluidized bed 1, both the form biomass pyrolysis gasification hydrogen-producing provided the regenerated catalyzer, and thermal source is provided again.
In whole biomass hydrogen preparation reaction process, circulating fluidized bed is in 650～900 ℃ middle temperature state, and bubbling fluidized bed is in 850～1100 ℃ of conditions of high temperature; Rely on calcium oxide/magnesium oxide and lime carbonate/hydrotalcite particle thereof to carry out the heat transmission between circulating fluidized bed 1 and the bubbling fluidized bed 3, the combustion processes of biomass pyrogenation gasification hydrogen manufacturing and coke is separated.Also can contain Ni-basedly in described calcium oxide/magnesia catalyst, become calcium oxide/magnesium oxide-nickel-base catalyst.
Claims (2)
1, a kind of biomass-gasifying hydrogen generating serial fluid bed apparatus, be composed in series by circulating fluidized bed, cyclonic separator and bubbling fluidized bed, it is characterized in that circulating fluidized bed (1) top is connected with the top of cyclonic separator (2), the lower side of circulating fluidized bed (1) is connected with bubbling fluidized bed (3), the lower side of circulating fluidized bed (1) also is provided with biological particles charging opening (B), the bottom of circulating fluidized bed (1) is provided with water vapor inlet mouth (A), and the bed material is calcium oxide/magnesia catalyst particle (11) in the circulating fluidized bed (1); The top of cyclonic separator (2) is hydrogen-rich gas air outlet (C), and the discharge nozzle (21) of cyclonic separator (2) bottom inserts in the bubbling fluidized bed (3); The top of bubbling fluidized bed (3) is flue gas air outlet (D), and bubbling fluidized bed (3) bottom is air/oxygen inlet mouth (E), and the bed material is lime carbonate/hydrotalcite particle (31) in the bubbling fluidized bed (3).
2, biomass-gasifying hydrogen generating serial fluid bed apparatus according to claim 1 is characterized in that also containing in described calcium oxide/magnesia catalyst Ni-based, becomes calcium oxide/magnesium oxide-nickel-base catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200420079615XU CN2725267Y (en) | 2004-09-20 | 2004-09-20 | Serial Fluidized bed biomass gasification hydrogen making device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200420079615XU CN2725267Y (en) | 2004-09-20 | 2004-09-20 | Serial Fluidized bed biomass gasification hydrogen making device |
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| CN2725267Y true CN2725267Y (en) | 2005-09-14 |
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| CNU200420079615XU Expired - Fee Related CN2725267Y (en) | 2004-09-20 | 2004-09-20 | Serial Fluidized bed biomass gasification hydrogen making device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ITRM20080632A1 (en) * | 2008-11-27 | 2010-05-27 | Shap Corp S R L | INTEGRATED GASIFICATION / COMBUSTOR PLANT WITH FLUID BED |
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2004
- 2004-09-20 CN CNU200420079615XU patent/CN2725267Y/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ITRM20080632A1 (en) * | 2008-11-27 | 2010-05-27 | Shap Corp S R L | INTEGRATED GASIFICATION / COMBUSTOR PLANT WITH FLUID BED |
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| CF01 | Termination of patent right due to non-payment of annual fee |