CN101045874A - Process of preparing biofuel oil and fuel gas with screw extruder - Google Patents
Process of preparing biofuel oil and fuel gas with screw extruder Download PDFInfo
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- CN101045874A CN101045874A CNA2006100115852A CN200610011585A CN101045874A CN 101045874 A CN101045874 A CN 101045874A CN A2006100115852 A CNA2006100115852 A CN A2006100115852A CN 200610011585 A CN200610011585 A CN 200610011585A CN 101045874 A CN101045874 A CN 101045874A
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Abstract
The present invention belongs to the field of comprehensive biomass utilizing technology, and is especially process of preparing biofuel oil and fuel gas with biomass by using screw extruder. Screw extruder is utilized in compressing water-containing biomass material, and by means of regulating the staying time of the biomass material in the heating area of the screw extruder, biofuel oil and fuel gas with low oxygen content and high heat value may be produced. In the product, fuel gas accounts for 50-70 % and biofuel oil 10-20 %, and the obtained biofuel oil has heat value of 30-46 MJ/kg and oxygen content less than 6 %.
Description
Technical field
The invention belongs to technical field of biomass comprehensive utilization, particularly screw extruder is used for biomass thermal conversion process process of preparing bio-fuel-oil (comprising gasoline, diesel oil, kerosene fraction) and combustible gas, thereby a kind of method of utilizing screw extruder to prepare bio-fuel-oil and combustible gas is provided.
Background technology
Yuan Zhenhong, Wu's wound etc. the people write " biomass utilization philosophy and technique " book (chapter 5 first segment, 149～153 pages) point out, at present, the technology of screw rod extruding biomass is widely used in not seeing the report that is applied to biomass thermal chemical conversion process in the technological process of biomass compressed moulding.And the device of biomass thermal chemical conversion prepare liquid fuel and combustible gas, Yuan Zhenhong, Wu's wound etc. the people write in " biomass utilization philosophy and technique " book (chapter 8 second joint, 296～299 pages) comparatively detailed introduction arranged: mainly contain air flow bed cracker, fast fluidized bed cracker, vacuum cracking device, whirlpool ablation cracker, rotation awl scission reaction device, spouted bed cracker etc.The general structure more complicated of above reactor, operating procedure is loaded down with trivial details, and device volume is bigger; In addition, (" solar energy journal ", the 23rd the 1st phase of volume, in February, 2002, Wang Shurong etc., the biomass flash thermo-cracking is produced the experimental study of bio oil) contain more oxygenatedchemicals (aldehyde by the resulting bio oil of above reaction unit, ketone, acid, ester etc.), therefore oxygen level is higher, and calorific value is lower.As the calorific value of the product liquid oil by air flow bed cracker lysed biomass gained 24.57MJ/h only.
Summary of the invention
The objective of the invention is to overcome in the existing biomass thermal conversion process, the reaction unit volume is bigger, the consumption carrier gas, and the thing fuel oil calorific value that produces low, the deficiency that oxygen level is high, a kind of method of utilizing screw extruder to prepare bio-fuel-oil and combustible gas is provided, thereby advances the low temperature thermal transition technology of (extruding) technology and biomass to combine preparation bio-fuel-oil and combustible gas screw rod.
The method of utilizing screw extruder to prepare bio-fuel-oil and combustible gas of the present invention, be to adopt screw extruder, biomass material is compressed propelling, rotating speed by adjusting screw(rod), control the residence time of biomass material at heating region, avoid the incomplete or overreact of biomass material reaction, and then obtain low oxygen content, the bio-fuel-oil of high heating value and combustible gas.
The present invention realizes by following measure: the biomass material that will contain 8～10% water adds (extrusion machine conversion zone and pre-reaction section are furnished with intensification, attemperator) in the screw extruder continuously from the hopper of screw extruder, temperature of reaction is at 250～680 ℃, 10～30 ℃/min of temperature rise rate, under temperature of reaction the biomass material residence time be about 1 minute～3 hours; Gas (comprising combustible gas and bio-fuel-oil) and the solid collecting under the temperature of reaction simultaneously to be produced, directly with gas and solids constituent from; Gas is isolated bio-fuel-oil and combustible gas by condensing works (being lower than 50 ℃) again.The output of combustible gas accounts for 50～70% of raw material, and the output of bio-fuel-oil accounts for 10～20% of raw material, and the calorific value of bio-fuel-oil is 30～46MJ/kg approximately, oxygen level＜6%.
Described bio-fuel-oil component comprises gasoline, diesel oil, kerosene fraction.
Described combustible gas component comprises H
2, CO, CH
4
Biomass material of the present invention is agricultural crop straw, herbaceous plant, xylophyta etc. or their any mixture.In order to obtain the output of higher bio-fuel-oil and combustible gas, biomass materials such as agricultural crop straw, herbaceous plant or xylophyta can be pulverized length less than 30mm.
Described agricultural crop straw is selected from one or more the mixture in straw, wheat straw, maize straw, soybean stalk, cotton stalk, the sweet potato vine etc.; Described herbaceous plant is selected from one or more the mixture in the grass bits on reed, reed reed, awns bar, bamboo, lawn etc.; Described xylophyta comprises fallen leaves, wood chip of trees etc. or their any mixture.
The present invention is used to prepare bio-fuel-oil and combustible gas with screw extruder, and the oxygen level of the bio-fuel-oil that this preparation method obtains is low, the calorific value height.
The invention will be further described below in conjunction with embodiment and accompanying drawing.
Description of drawings
Fig. 1. the embodiment of the invention 1 resulting bio-fuel-oil sample and marketable gasolines, diesel oil, kerosene mix the stratographic analysis figure of sample.
Embodiment
Embodiment 1.
To pulverize straw raw material (0.5～0.8mm) with suitable quantity of water mix charging (weight ratio 10: 3), add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by single screw extrusion machine, control reaction temperature is at 270 ℃, and the straw residence time is 20min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 65% of raw material.Bio-fuel-oil is about 19%, the about 39.8MJ/kg of calorific value, oxygen level＜6%.
The chromatographic peak of the chromatographic peak of resulting bio-fuel-oil and marketable gasolines, diesel oil, kerosene compound sample is overlapping substantially as can be seen from accompanying drawing.By the result that mass spectra peak is analyzed, the major ingredient of resulting bio-fuel-oil is:
(1) hydrocarbon polymer mainly contains: decane, undecane, dodecane, tridecane, the tetradecane, pentadecane, n-Hexadecane, heptadecane, octadecane, nonadecane, eicosane, heneicosane, docosane, methylcyclohexane, the propyl group pentamethylene, pentamethylene, 1,2,3-trimethylammonium-cyclopentenes, 2-ethyl-3-methyl cyclopentene, toluene, ethylbenzene, 1, the 3-dimethyl benzene, dimethylbenzene, 1-ethyl-4-methylbenzene, 1,2, the 4-Three methyl Benzene, the 2-ethylbenzene, 1-ethyl-2, the 3-dimethyl benzene, crotyl benzene, 3 methyl-2 butylbenzene, 1,4,6-trimethyl-naphthalene etc.
(2) oxygenatedchemicals mainly contains: 2-methylphenol, 4-methylphenol, 2,5-xylenol, 2,4-xylenol, 3-ethylphenol, 4-ethylphenol etc.
Thereby the resulting bio-fuel-oil of proof this method is based on gasoline, diesel oil, kerosene fraction.
Embodiment 2.
With ground corn stalk raw material (1.0～1.5mm) with suitable quantity of water mix charging (weight ratio 10: 5), add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by single screw extrusion machine, controlled temperature is at 320 ℃, and the residence time is 60min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 52% of raw material, and bio-fuel-oil is about 15%, the about 40MJ/kg of calorific value, oxygen level＜6%.
Embodiment 3.
(10～15mm) mix charging (weight ratio 10: 4) with suitable quantity of water with the soybean stalk pulverized, add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by twin screw extruder, controlled temperature is at 350 ℃, and the residence time is 30min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 65% of raw material, and bio-fuel-oil is about 17%, the about 38.5MJ/kg of calorific value, oxygen level＜6%.
Embodiment 4.
(5.5～10mm) mix charging (weight ratio 10: 8) with suitable quantity of water with the straw raw material pulverized, add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by single screw extrusion machine, controlled temperature is at 420 ℃, and the residence time is 90min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 50% of raw material, and bio-fuel-oil is about 16%, the about 42MJ/kg of calorific value, oxygen level＜6%.
Embodiment 5.
To pulverize sweet potato vine (18～25mm) with suitable quantity of water mix charging (weight ratio 10: 15), add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by twin screw extruder, controlled temperature is at 480 ℃, and the residence time is 150min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 40% of raw material, and bio-fuel-oil is about 14%, the about 38MJ/kg of calorific value, oxygen level＜6%.
Embodiment 6.
To pulverize wheat straw raw material (10～20mm) with suitable quantity of water mix charging (weight ratio 10: 6), add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by twin screw extruder, controlled temperature is at 550 ℃, and the residence time is 60min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 50% of raw material, and bio-fuel-oil is about 16.7%, the about 40MJ/kg of calorific value, oxygen level＜6%.
Embodiment 7.
(2.8～10mm) mix charging (weight ratio 10: 10) with suitable quantity of water, add continuously from the hopper of screw extruder, advance by twin screw extruder, and 10～30 ℃/min of temperature rise rate, controlled temperature are at 650 ℃, and the residence time is 150min with wood chip.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 60% of raw material, and bio-fuel-oil is about 17.2%, the about 38MJ/kg of calorific value, oxygen level＜6%.
Embodiment 8.
(8.8～18mm) mix charging (weight ratio 10: 12) with suitable quantity of water with the trees fallen leaves pulverized, add continuously from the hopper of screw extruder, advance 10～30 ℃/min of temperature rise rate by single screw extrusion machine, controlled temperature is at 420 ℃, and the residence time is 30min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 60% of raw material, and bio-fuel-oil is about 17.2%, the about 38MJ/kg of calorific value, oxygen level＜6%.
The 35g reed pulverizes that (1.8～10mm) mix with 40ml water, add continuously from the hopper of screw extruder, advance by single screw extrusion machine, and 10～30 ℃/min of temperature rise rate, controlled temperature are at 420 ℃, and the residence time is 1 hour.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 55% of raw material, and the output of bio-fuel-oil is about 18%.Calorific value is 37.2MJ/kg, oxygen level＜6%.
The grass on 40g lawn bits pulverize that (2.0～10mm) mix with 28ml water, add continuously from the hopper of screw extruder, advance by single screw extrusion machine, and 10～30 ℃/min of temperature rise rate, controlled temperature are at 450 ℃, and the residence time is 30min.With the gas that obtains and solids constituent from; Gas is after condenser condenses, and the output that obtains combustible gas accounts for 62% of raw material, and the output of bio-fuel-oil is about 18%.Calorific value is 39.1MJ/kg, oxygen level＜6%.
Claims (9)
1. method of utilizing screw extruder to prepare bio-fuel-oil and combustible gas, it is characterized in that: the biomass material that will contain 8～10% water adds in the screw extruder from the hopper of screw extruder continuously, temperature of reaction is at 250～680 ℃, 10～30 ℃/min of temperature rise rate, the biomass material residence time is 1 minute～3 hours under temperature of reaction; Gas and the solid collecting under the temperature of reaction simultaneously to be produced, directly with gas and solids constituent from; Gas is isolated bio-fuel-oil and combustible gas by condensing works again.
2. method according to claim 1 is characterized in that: the calorific value of described bio-fuel-oil is 30～46MJ/kg, oxygen level＜6%.
3. method according to claim 1 and 2 is characterized in that: described bio-fuel-oil component comprises gasoline, diesel oil, kerosene fraction.
4. method according to claim 1 is characterized in that: described combustible gas component comprises H
2, CO, CH
4
5. method according to claim 1 is characterized in that: described biomass material is agricultural crop straw, herbaceous plant, xylophyta or their any mixture.
6. method according to claim 5 is characterized in that: the length of described agricultural crop straw, herbaceous plant, xylophyta is less than 30mm.
7. according to claim 5 or 6 described methods, it is characterized in that: described agricultural crop straw is selected from one or more the mixture in straw, wheat straw, maize straw, soybean stalk, cotton stalk, the sweet potato vine.
8. according to claim 5 or 6 described methods, it is characterized in that: described herbaceous plant is selected from one or more the mixture in the grass bits on reed, reed reed, awns bar, bamboo, lawn.
9. according to claim 5 or 6 described methods, it is characterized in that: described xylophyta is selected from fallen leaves, wood chip or their any mixture of trees.
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| CN2006100115852A CN101045874B (en) | 2006-03-29 | 2006-03-29 | Process of preparing biofuel oil and fuel gas with screw extruder |
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| CN101045874B CN101045874B (en) | 2010-07-28 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7955508B2 (en) | 2008-03-11 | 2011-06-07 | Xtrudx Technologies, Inc. | Supercritical fluid biomass conversion systems |
| US8057666B2 (en) | 2008-03-11 | 2011-11-15 | Xtrudx Technologies, Inc. | Biomass and waste plastics to neodiesel and valuable chemicals via supercritical water |
| US8980143B2 (en) | 2008-03-11 | 2015-03-17 | Thomas E. Loop | Biomass and waste plastics depolymerization machine and methods via supercritical water |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI417374B (en) * | 2010-11-25 | 2013-12-01 | Univ Nat Taiwan | Rapid Pyrolysis System of Biogenic Raw Material into Biomass Oil and Its |
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| JPS5036665B2 (en) * | 1971-08-18 | 1975-11-26 | ||
| JPS5036664B2 (en) * | 1971-08-18 | 1975-11-26 | ||
| FR2601380B1 (en) * | 1986-07-08 | 1989-08-18 | Clextral | PROCESS AND DEVICE FOR THE CONTINUOUS MANUFACTURE OF MIXED FUELS BASED ON ORGANIC MATERIALS AND HYDROCARBON MATERIALS |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7955508B2 (en) | 2008-03-11 | 2011-06-07 | Xtrudx Technologies, Inc. | Supercritical fluid biomass conversion systems |
| US8057666B2 (en) | 2008-03-11 | 2011-11-15 | Xtrudx Technologies, Inc. | Biomass and waste plastics to neodiesel and valuable chemicals via supercritical water |
| US8980143B2 (en) | 2008-03-11 | 2015-03-17 | Thomas E. Loop | Biomass and waste plastics depolymerization machine and methods via supercritical water |
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| CN101045874B (en) | 2010-07-28 |
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Owner name: BEIJING RUIZENG LANYU NEW ENERGY CO., LTD. Free format text: FORMER OWNER: PHYSICAL CHEMISTRY TECHNOLOGY INST., CHINESE ACADEMY OF SCIENCES Effective date: 20091225 |
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