CN105293857A - Method for preparing hydrogen through catalytic gasification of residual activated sludge - Google Patents
Method for preparing hydrogen through catalytic gasification of residual activated sludge Download PDFInfo
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- CN105293857A CN105293857A CN201510670083.XA CN201510670083A CN105293857A CN 105293857 A CN105293857 A CN 105293857A CN 201510670083 A CN201510670083 A CN 201510670083A CN 105293857 A CN105293857 A CN 105293857A
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- pyrolyzer
- gasifier
- catalytic gasification
- burner
- active sludge
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Abstract
The invention relates to a method for preparing hydrogen through catalytic gasification of residual activated sludge. The method mainly solves the problems that in the prior art, the gas yield is low and the hydrogen content is low. By means of the method for preparing hydrogen through catalytic gasification of the residual activated sludge, the residual activated sludge with the water content lower than 85% enters a pyrolyzer from the portion above the pyrolyzer, and the sludge is mixed with a carbon deposit catalyst coming from a gasifier to generate a pyrolytic gaseous product and semicoke; the pyrolytic gaseous product and vapour introduced from the bottom of the pyrolyzer move upwards together to enter the gasifier; in the gasifier, the pyrolytic gaseous product and the vapour make contact with a catalyst movable bed in a reflux mode to generate a hydrogen-rich gas product; the carbon deposit catalyst moves downwards to the pyrolyzer, and the solid product semicoke in the pyrolyzer and the carbon deposit catalyst move downwards together and then enter a burner; the regenerated catalyst circulates back to the gasifier, and hot smoke generated due to combustion is discharged from the top of the burner. By means of the technical scheme, the problems are well solved, and the method can be used for preparing hydrogen through catalytic gasification of the residual activated sludge.
Description
Technical field
The present invention relates to the method for a kind of residual active sludge catalytic gasification hydrogen manufacturing.
Background technology
In sewage treatment process, generally adopt activated sludge process, it can purifying domestic sewage and various containing organic trade effluent effectively.This method, while sewage is purified, constantly isolates excess sludge from system.Excess sludge is the concentrated of dirty water pollutant, and in sewage, the COD of 30-50%, the P of 90% proceed to excess sludge.If excess sludge can not be dealt carefully with, the persistent organism contained in excess sludge, heavy metal, viral micro-organisms, will enter into environment, cause secondary pollution, jeopardize the health of the mankind and other biological.On the other hand, excess sludge is primarily of microorganism cells colony and its breakdown products composition, and organic content is high, excess sludge can be used as resource.And developing rapidly along with Chinese Urbanization, the quantity of sewage work increases sharply, and the generation of mud also will significantly increase.Therefore, the research carrying out sludge disposal technology aspect has important economic and social benefit.
The microorganism that excess sludge is is master by bacterium, microfauna and suspended matter, colloidalmaterial formed umbrinaceous flocs unit mixed in together, its water ratio high (general 98%), bulky, complicated component, not easily processes.The excess sludge that different sewage works produces, contained by it, the composition of harmful substances is also not quite similar, such as, except containing except bacterium, microorganism, parasite, suspended matter and colloidalmaterial in the excess sludge of sewage work's generation of process sanitary sewage, also containing some nitrogen, phosphorus etc.
Mud is nutritive substance and energy substance, how to utilize the useful component in mud, realizes turning waste into wealth, and reclaims to have the material of practical value and resource becomes the main development direction solving sludge problem recent years.Recycling sludge, can obtain additional economic benefit by suitable recycling treatment on the one hand, reduce Sewage Plant process and always run spending; Also can avoid the secondary environmental pollution of mud on the other hand.
Hydrogen Energy is one of optimal clear energy sources, and Hydrogen Energy, as a kind of secondary energy, has very high energy density, the advantages such as products of combustion cleanliness without any pollution.Therefore, residual active sludge is converted to Hydrogen Energy and can solve the secondary pollution problem that excess sludge entered environment brings, also there is certain economic benefit simultaneously, farthest can realize low-carbon economy, the recycle of excess sludge.
Summary of the invention
Technical problem to be solved by this invention is the problem that in prior art, gas production rate is low, hydrogen richness is low, provides a kind of method of new residual active sludge catalytic gasification hydrogen manufacturing.The method is used for, in the hydrogen manufacturing of residual active sludge catalytic gasification, having the advantage that gas production rate is high, hydrogen richness is high.
For solving the problem, the technical solution used in the present invention is as follows: the method for a kind of residual active sludge catalytic gasification hydrogen manufacturing, water ratio enters pyrolyzer lower than the residual active sludge of 85% above pyrolyzer, in pyrolyzer, mud mixes with the carbon deposited catalyst coming from gasifier,, there is fast pyrogenation reaction, Heat of Formation solution gaseous product and semicoke in cocurrent flow descending; Pyrolysis gaseous product is advanced into gasifier together with the water vapour passed into bottom pyrolyzer; In gasifier, pyrolysis gaseous product is adverse current and descending catalyst moving bed counter current contact together with water vapour, and tar vapor catalytic conversion reaction occurs, and generate hydrogen-rich gaseous product, hydrogen-rich gaseous product is drawn from gasifier top; In gasification reaction process, catalyzer is inactivation gradually because of surperficial carbon deposit, and the catalyzer of carbon deposit comes downwards to pyrolyzer, and the solid product semicoke in pyrolyzer is descending together with carbon deposited catalyst, then enters burner; In burner, the carbon deposit of semicoke and catalyst surface and from the warm air generation combustion reactions that burner base passes into, makes semicoke and catalyst surface carbon deposit burn, simultaneously releases heat, catalyst recirculation gasifier after regeneration, the heat smoke that burning produces is discharged from burner top.
In technique scheme, preferably, described catalyzer is peridotites.
In technique scheme, preferably, gasifier is that gas-solid is counter-flow moving bed, and burner is fast fluidized bed.
In technique scheme, preferably, independently separately, gas does not leak mutually alters the atmosphere of gasifier, pyrolyzer and burner.
In technique scheme, preferably, the operational condition of pyrolyzer is: 400-600 DEG C.
In technique scheme, preferably, the operational condition of gasifier is: 700-900 DEG C.
In technique scheme, preferably, the operational condition of burner is: 800-900 DEG C.
In technique scheme, preferably, the coke content of semicoke counts 66-78% with massfraction.
In technique scheme, preferably, the coke content of carbon deposited catalyst counts 22-29% with massfraction.
Mud is nutritive substance and energy substance, utilizes the useful component in mud, the method for catalytic gasification hydrogen manufacturing, adopts the counter-flow moving bed catalytic gasification process for making hydrogen of outer circulation, can obtain tar content low, the aerogenesis that hydrogen richness is high.Additional economic benefit can be obtained by suitable recycling treatment on the one hand, reduce Sewage Plant process and always run spending; Also can avoid the secondary environmental pollution of mud on the other hand, achieve good technique effect.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
This patent provides the method for a kind of residual active sludge catalytic gasification hydrogen manufacturing, water ratio enters pyrolyzer lower than the residual active sludge of 60% above pyrolyzer, in pyrolyzer, mud mixes with the carbon deposited catalyst coming from gasifier, cocurrent flow descending, generation fast pyrogenation reacts, Heat of Formation solution gaseous product and semicoke; Pyrolysis gaseous product is advanced into gasifier together with the water vapour passed into bottom pyrolyzer; In gasifier, pyrolysis gaseous product is adverse current and descending catalyst moving bed counter current contact together with water vapour, and tar vapor catalytic conversion reaction occurs, and generate hydrogen-rich gaseous product, hydrogen-rich gaseous product is drawn from gasifier top; In gasification reaction process, catalyzer is inactivation gradually because of surperficial carbon deposit, and the catalyzer of carbon deposit comes downwards to pyrolyzer, and the solid product semicoke in pyrolyzer is descending together with carbon deposited catalyst, then enters burner; In burner, the carbon deposit of semicoke and catalyst surface and from the warm air generation combustion reactions that burner base passes into, makes semicoke and catalyst surface carbon deposit burn, simultaneously releases heat, catalyst recirculation gasifier after regeneration, the heat smoke that burning produces is discharged from burner top.
Residual active sludge quality is 2kg, pyrolytic reaction actuator temperature is 500 DEG C, burner temperature is 800 DEG C, gasification reactor temperature 800 DEG C, Moving Bed layer height 100mm in gasifier, thermal barrier internal circulating load 4.22kg/h, the coke content of semicoke counts 71% with massfraction, and the coke content of carbon deposited catalyst counts 29% with massfraction.Gas yield is 1.56Nm
3the gas production rate of/kg, (H in aerogenesis
2+ CO) content reaches 54%.
[embodiment 2]
According to the condition described in embodiment 1 and step, pyrolytic reaction actuator temperature is 400 DEG C, burner temperature is 800 DEG C, gasification reactor temperature 700 DEG C, Moving Bed layer height 100mm in gasifier, thermal barrier internal circulating load 4.22kg/h, the coke content of semicoke counts 66% with massfraction, and the coke content of carbon deposited catalyst counts 34% with massfraction.Gas yield is 1.42Nm
3the gas production rate of/kg, (H in aerogenesis
2+ CO) content reaches 48%.
[embodiment 3]
According to the condition described in embodiment 1 and step, pyrolytic reaction actuator temperature is 600 DEG C, burner temperature is 900 DEG C, gasification reactor temperature 900 DEG C, Moving Bed layer height 100mm in gasifier, thermal barrier internal circulating load 4.22kg/h, the coke content of semicoke counts 78% with massfraction, and the coke content of carbon deposited catalyst counts 22% with massfraction.Gas yield is 1.71Nm
3the gas production rate of/kg, (H in aerogenesis
2+ CO) content reaches 56%.
Claims (9)
1. the method for residual active sludge catalytic gasification hydrogen manufacturing, water ratio enters pyrolyzer lower than the residual active sludge of 85% above pyrolyzer, in pyrolyzer, mud mixes with the carbon deposited catalyst coming from gasifier, cocurrent flow descending, generation fast pyrogenation reacts, Heat of Formation solution gaseous product and semicoke; Pyrolysis gaseous product is advanced into gasifier together with the water vapour passed into bottom pyrolyzer; In gasifier, pyrolysis gaseous product is adverse current and descending catalyst moving bed counter current contact together with water vapour, and tar vapor catalytic conversion reaction occurs, and generate hydrogen-rich gaseous product, hydrogen-rich gaseous product is drawn from gasifier top; In gasification reaction process, catalyzer is inactivation gradually because of surperficial carbon deposit, and the catalyzer of carbon deposit comes downwards to pyrolyzer, and the solid product semicoke in pyrolyzer is descending together with carbon deposited catalyst, then enters burner; In burner, the carbon deposit of semicoke and catalyst surface and from the warm air generation combustion reactions that burner base passes into, makes semicoke and catalyst surface carbon deposit burn, simultaneously releases heat, catalyst recirculation gasifier after regeneration, the heat smoke that burning produces is discharged from burner top.
2. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, is characterized in that described catalyzer is peridotites.
3. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, it is characterized in that described gasifier is that gas-solid is counter-flow moving bed, burner is fast fluidized bed.
4. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, it is characterized in that the atmosphere of described gasifier, pyrolyzer and burner independently separately, gas does not leak mutually alters.
5. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, is characterized in that the operational condition of described pyrolyzer is: 400-600 DEG C.
6. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, is characterized in that the operational condition of described gasifier is: 700-900 DEG C.
7. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, is characterized in that the operational condition of described burner is: 800-900 DEG C.
8. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, is characterized in that the coke content of described semicoke counts 66-78% with massfraction.
9. the method for residual active sludge catalytic gasification hydrogen manufacturing according to claim 1, is characterized in that the coke content of described carbon deposited catalyst counts 22-29% with massfraction.
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| CN201510670083.XA CN105293857A (en) | 2015-10-13 | 2015-10-13 | Method for preparing hydrogen through catalytic gasification of residual activated sludge |
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| CN201510670083.XA CN105293857A (en) | 2015-10-13 | 2015-10-13 | Method for preparing hydrogen through catalytic gasification of residual activated sludge |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108130346A (en) * | 2017-12-15 | 2018-06-08 | 清华大学 | A kind of method and system using sludge thermal chemical reaction hydrogen manufacturing |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000056671A1 (en) * | 1999-03-22 | 2000-09-28 | Environmental Solutions International Ltd. | Process and apparatus for the conversion of carbonaceous materials |
| CN101045524A (en) * | 2007-05-04 | 2007-10-03 | 大连理工大学 | Method for preparing hydrogen-riched gas by solid fuel catalytic gasification |
| CN201459073U (en) * | 2009-09-04 | 2010-05-12 | 刘黎黎 | Biomass catalytic gasification furnace |
| CN103468322A (en) * | 2013-07-25 | 2013-12-25 | 易高环保能源研究院有限公司 | Preparation method for hydrogen-rich gas through steam gasification of solid organic matter |
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2015
- 2015-10-13 CN CN201510670083.XA patent/CN105293857A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000056671A1 (en) * | 1999-03-22 | 2000-09-28 | Environmental Solutions International Ltd. | Process and apparatus for the conversion of carbonaceous materials |
| CN101045524A (en) * | 2007-05-04 | 2007-10-03 | 大连理工大学 | Method for preparing hydrogen-riched gas by solid fuel catalytic gasification |
| CN201459073U (en) * | 2009-09-04 | 2010-05-12 | 刘黎黎 | Biomass catalytic gasification furnace |
| CN103468322A (en) * | 2013-07-25 | 2013-12-25 | 易高环保能源研究院有限公司 | Preparation method for hydrogen-rich gas through steam gasification of solid organic matter |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108130346A (en) * | 2017-12-15 | 2018-06-08 | 清华大学 | A kind of method and system using sludge thermal chemical reaction hydrogen manufacturing |
| CN108130346B (en) * | 2017-12-15 | 2019-11-22 | 清华大学 | A method of utilizing sludge thermal chemical reaction hydrogen manufacturing |
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Address after: Yanan City, Shandong province Qingdao City three road 266071 No. 218 Applicant after: Sinopec Corp. Applicant after: Qingdao Safety Engineering Research Institute of Sinopec Co., Ltd. Address before: 100728 Chaoyangmen street, Beijing, No. 22, No. Applicant before: Sinopec Corp. Applicant before: Qingdao Safety Engineering Research Institute of Sinopec Co., Ltd. |
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Application publication date: 20160203 |
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