CN106987285B - A kind of method that multi phase state prepares high alcohol bio-fuel - Google Patents
A kind of method that multi phase state prepares high alcohol bio-fuel Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L2200/00—Components of fuel compositions
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- C10L2200/0461—Fractions defined by their origin
- C10L2200/0469—Renewables or materials of biological origin
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/12—Regeneration of a solvent, catalyst, adsorbent or any other component used to treat or prepare a fuel
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Abstract
本发明公开了一种多相态制备高级一元醇生物燃料的方法，该方法将浓度为5‑30wt％的糖醇水溶液与氢气并流进入固定床反应器，在温度为140‑300℃、氢气压力为2‑10MPa和液体空速为1.0‑10.0h‑1的条件下，在Ru‑MoOx/AC或Ru‑MoOx/CNT多功能催化剂协同作用下，糖醇在多相态的状态下选择性脱氧制备以戊醇和己醇为主要组分的高级一元醇生物燃料；糖醇转化率达99％，生物燃料中高级一元醇选择性达80％以上，具有过程简单、绿色低碳、转化条件温和、氢气消耗低、能源利用效率高及产物附加值高等优点，易于工业化生产，得到的戊醇和己醇均是重要的化工原料、溶剂及添加剂。The invention discloses a method for preparing high-grade monohydric alcohol biofuel in a heterogeneous state. In the method, an aqueous sugar alcohol solution with a concentration of 5-30 wt% and hydrogen are co-flowed into a fixed-bed reactor, and the temperature is 140-300° C. and hydrogen Under the conditions of pressure of 2-10MPa and liquid space velocity of 1.0-10.0h -1 , under the synergistic effect of Ru-MoOx/AC or Ru-MoOx/CNT multifunctional catalysts, the selectivity of sugar alcohols in the heterogeneous state Deoxygenation prepares higher monohydric alcohol biofuels with amyl alcohol and hexanol as main components; the conversion rate of sugar alcohols reaches 99%, and the selectivity of higher monohydric alcohols in biofuels reaches more than 80%, with simple process, green and low carbon, and mild conversion conditions. , low hydrogen consumption, high energy utilization efficiency and high added value of products, easy industrial production, the obtained amyl alcohol and hexanol are important chemical raw materials, solvents and additives.
Description
Technical field:
The present invention relates to low-carbon bio-fuel technical fields, and in particular to a kind of multi phase state prepares the combustion of high alcohol biology
The method of material.
Background technique:
Biomass is the carbon resource that liquid fuel and chemicals can be uniquely produced in renewable energy.Agriculture and forestry organic waste material etc.
It is a variety of can be translated into alcohol, ether and hydrocarbon etc. by the synthetic technology that gasifies for lignocellulose-like biomass resource very abundant
Product, but the product carbochain distribution that the F- T synthesis technology that gasifies obtains is wide, and the crude oil of production also needs distillation cutting separation difference to evaporate
Point, technology path is longer, and lower difficulty has economy on a small scale.Lignocellulosic can produce alcohol fuel, but ethyl alcohol through hydrolysed ferment
Fermenting microbe has not been achievable the Efficient Conversion of pentose, and the energy consumption of ethanol distillation purification is high, at present cellulose fuel
The cost of ethyl alcohol is also higher, and vehicle-use alcohol gasoline is because it needs the reasons such as waterproof, anticorrosion, in reconciliation, storage and transportation, sale and after sale
Service etc. increases cost.Ethanol petrol is hygroscopic, calorific value is lower, the automobile power deficiency of combusting ethanol gasoline etc. is asked
Topic, hinders the application of ethanol petrol, prospect allows of no optimist.Therefore, it explores the new biomass efficient of one kind and is converted into biological fluids
Fluid fuel approach is one of domestic and international research hotspot.
In recent years, biomass is by hydrolyzing and add hydrogen means to obtain sugar alcohol, then can by catalytic hydrogenation, aqueous phase reforming technology
To synthesize hydrogen, liquid alkane and chemicals.Huber et al. (Angew Chem Int Ed, 2004,43:1549) is prepared for one
Kind Pt/Al2O3-SiO2Catalyst can efficiently control sorbitol aqueous phase reforming selectivity synthesis C1~C6 alkane, 225
DEG C, under 3.96MPa, the overall selectivity of alkane can achieve 58~89%, and wherein the selectivity of pentane and n-hexane is respectively
21% and 40%.Chinese patent CN 101550350A discloses the preparation method and catalyst preparation process of a kind of biogasoline,
It is characterized in that, using carried noble metal Pt/HZSM-5 catalyst, being carried out using miniature slurry bed system high using sorbierite as raw material
Hydrogenation reaction is pressed, liquid alkane product can be obtained more with high selectivity.But biomass water phase be catalytically conveted to alkane need by
Oxygen atom in sugar alcohol molecule is totally removed, and not only hydrogen gas consumption is big for the process, but also sugar alcohol is converted into the quality receipts of alkane
Rate is lower, and the process conversion temperature is higher, energy consumption is larger, and whole efficiency is still to be improved.
Summary of the invention:
The object of the present invention is to provide a kind of methods that multi phase state prepares high alcohol bio-fuel, relatively low
Under conversion temperature, oxygen atom in selectively removing sugar alcohol molecule, orientation is produced using amylalcohol and hexanol as the advanced of main component
Monohydric alcohol bio-fuel, has that conversion condition is mild, hydrogen consumption is low, efficiency of energy utilization is high and product added value height etc. is excellent
Point.
The present invention is achieved by the following technical programs:
A kind of method that multi phase state prepares high alcohol bio-fuel, the sugar alcohol water that concentration is 5-30wt% by this method
Solution and hydrogen cocurrent enter fixed bed reactors, temperature is 140-300 DEG C, Hydrogen Vapor Pressure is 2-10MPa and liquid air speed
For 1.0-10.0h-1Under conditions of, under Ru-MoOx/AC or Ru-MoOx/CNT multifunction catalyst synergistic effect, sugar alcohol is more
Selective deoxidation preparation is using amylalcohol and hexanol as the high alcohol bio-fuel of main component in the state of phase；The sugar alcohol
Aqueous solution is the hydrolysis sugar liquid (main component is glucose and xylose) or hydrolysis sugar of starch and lignocellulose-like biomass
Liquid adds polyalcohol (main component is sorbierite and xylitol) aqueous solution after hydrogen；Method includes the following steps:
1) Ru-MoOx/AC or Ru-MoOx/CNT multifunction catalyst is loaded on to the reaction tube constant temperature of fixed bed reactors
Area, replacing hydrogen is until air is replaced completely by hydrogen in fixed bed reactors at room temperature；
2) it is passed through hydrogen, while fixed bed reactors with the heating rate of 5 DEG C/min rise to 350 DEG C from room temperature and in 350
DEG C constant temperature 3-5 hours until Ru-MoOx/AC or Ru-MoOx/CNT multifunction catalyst sufficiently restores；
3) fixed bed reactors temperature is down to 140-300 DEG C of reaction temperature of setting, is 5-30wt% sugar alcohol by concentration
Aqueous solution and hydrogen enter fixed bed reactors by volume flow ratio 1:50-1:200 cocurrent, and control liquid air speed is 1.0-
10.0h-1With Hydrogen Vapor Pressure 2-10MPa, make sugar alcohol aqueous solution that evaporation-condensation alternately and repeatedly more occur in fixed bed reactors
Amylalcohol and hexanol are converted into Ru-MoOx/AC or Ru-MoOx/CNT catalyst surface selectivity deoxygenation under phase；
4) it is condensed from the gas-liquid mixture of fixed bed reactors outlet discharge through 2-10MPa high pressure, is separated into product liquid
With incoagulable gas product, product liquid is layered as oily phase and water phase, and oil is mutually the mixture of amylalcohol and hexanol；Water phase is used for water
Solve technique preparation hydrolysis sugar alcohol liquid, gas phase is mainly to have neither part nor lot in the excess hydrogen of reaction, after recycle compressor is pressurized again into
Enter fixed bed reactors to recycle.
Step 1) at room temperature replacing hydrogen until air by hydrogen replaces complete specific steps such as in fixed bed reactors
Under: be passed through at room temperature hydrogen enter in fixed bed reactors to total reactor pressure reach 0.3MPa stop be added hydrogen, stand
Fixed bed reactors are vented to normal pressure after 1-10 minutes, repeatedly until air is replaced by hydrogen in fixed bed reactors
Entirely.
The Ru-MoOx/AC catalyst the preparation method is as follows: cocoanut active charcoal use nitric acid dousing 12 hours, then
It is cleaned, impregnated repeatedly and cleaned 3 times using deionized water, sufficiently remove the salinity in cocoanut active charcoal；Then after treatment
30wt%MoO is loaded on cocoanut active charcoal2, secondary load 3wt%Ru after drying prepares Ru-MoOx/AC catalyst.
The Ru-MoOx/CNT catalyst the preparation method is as follows: multi-walled carbon nanotube use nitric acid dousing 12 hours, and
It is cleaned, impregnated repeatedly and cleaned 3 times using deionized water afterwards, sufficiently remove the metal component in multi-walled carbon nanotube；Then exist
30wt%MoO is loaded after processing on multi-walled carbon nanotube2, secondary load 2wt%Ru after drying prepares Ru-MoOx/CNT and urges
Agent.
Beneficial effects of the present invention are as follows: the present invention is under relatively low conversion temperature, selectively removing sugar alcohol molecule
In oxygen atom, orientation produce using amylalcohol and hexanol as the high alcohol bio-fuel of main component, sugar alcohol conversion ratio reaches
99%, bio-fuel middle-and-high-ranking monohydric alcohol selectivity up to 80% or more, have process is simple, green low-carbon, conversion condition are mild,
The advantages that hydrogen consumption is low, efficiency of energy utilization is high and product added value is high, easy to industrialized production, obtained amylalcohol and hexanol
It is important industrial chemicals, solvent and additive, organic synthesis, coating, fine chemistry industry additive etc. is can be widely used for, also may be used
It is added in motor petrol and diesel oil at high proportion, compared with ethanol petrol, in the side such as waterproof, burn into calorific value and engine power
Face all has clear superiority, suitable for the power-equipment on all general commercial petrol and diesel oil vehicles and ship.
Specific embodiment:
It is to further explanation of the invention, rather than limiting the invention below.
Embodiment 1:
Cocoanut active charcoal uses nitric acid dousing 12 hours, is then cleaned using deionized water, impregnates and cleans 3 times repeatedly,
Sufficiently remove the salinity in cocoanut active charcoal.Then 30wt%MoO is loaded on cocoanut active charcoal after treatment2, two after drying
Secondary load 3wt%Ru, prepares Ru-MoOx/AC catalyst.
300g multifunction catalyst Ru-MoOx/AC is loaded on to the reaction tube flat-temperature zone of fixed bed reactors, at room temperature
It is passed through hydrogen to enter in fixed bed reactors, until total reactor pressure reaches 0.3MPa stops that hydrogen is added, after standing 1-10 minutes
Fixed bed reactors are vented to normal pressure, repeatedly inflation exhaust 3-5 times, until air is replaced by hydrogen in fixed bed reactors
Completely；
Be continually fed into hydrogen into fixed bed reactors, at the same fixed bed reactors with the heating rate of 5 DEG C/min from normal
Temperature rise to 350 DEG C and in 350 DEG C constant temperature 5 hours, until catalyst sufficiently restores；
Fixed bed reactors temperature is down to 300 DEG C of reaction temperature, concentration is that 20wt% sugar alcohol aqueous solution and hydrogen press body
Product flow-rate ratio 1:50 cocurrent enters fixed bed reactors, strict control liquid air speed 1.5h-1It is constant in 8.5- with Hydrogen Vapor Pressure
8.7MPa carries out sugar alcohol selective deoxygenation under multi phase state；
The product being discharged from fixed bed reactors outlet is separated into product liquid and incoagulability after the condensation of 8.0MPa high pressure
Gaseous product, product liquid is layered as oil mutually and water phase, oily phase are the mixture of amylalcohol and hexanol, selective up to 82.5%.Water
Mutually for hydrolysis process preparation hydrolysis sugar alcohol liquid, gas phase is mainly to have neither part nor lot in the excess hydrogen of reaction, is pressurized through recycle compressor
After be again introduced into fixed bed reactors and recycle.It is remaining from gas-liquid separator bottom collection high alcohol bio-fuel
Hydrogen is again introduced into fixed bed reactors after recycle compressor is pressurized and recycles through being discharged at the top of gas-liquid separator.
Embodiment 2:
Cocoanut active charcoal uses nitric acid dousing 12 hours, is then cleaned using deionized water, impregnates and cleans 3 times repeatedly,
Sufficiently remove the salinity in cocoanut active charcoal.Then 30wt%MoO is loaded on cocoanut active charcoal after treatment2, two after drying
Secondary load 3wt%Ru, prepares Ru-MoOx/AC catalyst.
300g multifunction catalyst Ru-MoOx/AC is loaded on to the reaction tube flat-temperature zone of fixed bed reactors, at room temperature
It is passed through hydrogen to enter in fixed bed reactors, until total reactor pressure reaches 0.3MPa stops that hydrogen is added, after standing 1-10 minutes
Fixed bed reactors are vented to normal pressure, repeatedly inflation exhaust 3-5 times, until air is replaced by hydrogen in fixed bed reactors
Completely；
Be continually fed into hydrogen into fixed bed reactors, at the same fixed bed reactors with the heating rate of 5 DEG C/min from normal
Temperature rise to 350 DEG C and in 350 DEG C constant temperature 5 hours, until catalyst sufficiently restores；
Fixed bed reactors temperature is down to 240 DEG C of reaction temperature, concentration is that 15wt% sugar alcohol aqueous solution and hydrogen press body
Product flow-rate ratio 1:100 cocurrent enters fixed bed reactors, strict control liquid air speed 1.5h-1It is constant in 3.4- with Hydrogen Vapor Pressure
3.6MPa carries out sugar alcohol selective deoxygenation under multi phase state；
The product being discharged from fixed bed reactors outlet is separated into product liquid and incoagulability after the condensation of 3.0MPa high pressure
Gaseous product, product liquid is layered as oil mutually and water phase, oily phase are the mixture of amylalcohol and hexanol, selective up to 86.8%.Water
Mutually for hydrolysis process preparation hydrolysis sugar alcohol liquid, gas phase is mainly to have neither part nor lot in the excess hydrogen of reaction, is pressurized through recycle compressor
After be again introduced into fixed bed reactors and recycle.It is remaining from gas-liquid separator bottom collection high alcohol bio-fuel
Hydrogen is again introduced into fixed bed reactors after recycle compressor is pressurized and recycles through being discharged at the top of gas-liquid separator.
Embodiment 3:
Multi-walled carbon nanotube uses nitric acid dousing 12 hours, is then cleaned using deionized water, repeatedly immersion and cleaning 3
It is secondary, sufficiently remove the metal component in multi-walled carbon nanotube.Then 30wt%MoO is loaded on multi-walled carbon nanotube after treatment2,
Secondary load 2wt%Ru after drying prepares Ru-MoOx/CNT catalyst.
300g multifunction catalyst Ru-MoOx/CNT is loaded on to the reaction tube flat-temperature zone of fixed bed reactors, in room temperature
Under be passed through hydrogen and enter in fixed bed reactors, until total reactor pressure reaches 0.3MPa stop that hydrogen is added, stand 1-10 minutes
Fixed bed reactors are vented to normal pressure afterwards, repeatedly inflation exhaust 3-5 times, until air is set by hydrogen in fixed bed reactors
It changes completely；
Be continually fed into hydrogen into fixed bed reactors, at the same fixed bed reactors with the heating rate of 5 DEG C/min from normal
Temperature rise to 350 DEG C and in 350 DEG C constant temperature 5 hours, until catalyst sufficiently restores；
Fixed bed reactors temperature is down to 220 DEG C of reaction temperature, concentration is that 20wt% sugar alcohol aqueous solution and hydrogen press body
Product flow-rate ratio 1:100 cocurrent enters fixed bed reactors, keeps liquid air speed 6.0h-1It is constant in 2.3-2.5MPa progress with pressure
Sugar alcohol selective deoxygenation under multi phase state；
The product being discharged from fixed bed reactors outlet is separated into product liquid and incoagulability after the condensation of 2.0MPa high pressure
Gaseous product, product liquid is layered as oil mutually and water phase, oily phase are the mixture of amylalcohol and hexanol, selective up to 81.7%.Water
Mutually for hydrolysis process preparation hydrolysis sugar alcohol liquid, gas phase is mainly to have neither part nor lot in the excess hydrogen of reaction, is pressurized through recycle compressor
After be again introduced into fixed bed reactors and recycle.It is remaining from gas-liquid separator bottom collection high alcohol bio-fuel
Hydrogen is again introduced into fixed bed reactors after recycle compressor is pressurized and recycles through being discharged at the top of gas-liquid separator.
Claims (1)
1. a kind of method that multi phase state prepares high alcohol bio-fuel, which is characterized in that concentration is 5- by this method
The sugar alcohol aqueous solution of 30wt% and hydrogen cocurrent enter fixed bed reactors, temperature be 140-300 DEG C, Hydrogen Vapor Pressure 2-
10MPa and liquid air speed are 1.0-10.0h-1Under conditions of, it is cooperateed in Ru-MoOx/AC or Ru-MoOx/CNT multifunction catalyst
Under effect, sugar alcohol selective deoxidation preparation in the state of multi phase state is raw as the high alcohol of main component using amylalcohol and hexanol
Object fuel；After the sugar alcohol aqueous solution adds hydrogen for the hydrolysis sugar liquid or hydrolysis sugar liquid of starch and lignocellulose-like biomass
Polyatomic alcohol water solution；The Ru-MoOx/AC catalyst the preparation method is as follows: cocos active carbon use nitric acid dousing 12 hours,
It is then cleaned, impregnated repeatedly and cleaned 3 times with deionized water, remove the salinity in cocos active carbon；Then coconut palm after treatment
30wt%MoO is loaded on shell activated carbon2, secondary load 3wt%Ru after drying prepares Ru-MoOx/AC catalyst；The Ru-
MoOx/CNT catalyst the preparation method is as follows: multi-walled carbon nanotube use nitric acid dousing 12 hours, then use deionized water
Cleaning is impregnated repeatedly and is cleaned 3 times, and the metal component in multi-walled carbon nanotube is removed；Then multi-walled carbon nanotube after treatment
Upper load 30wt%MoO2, secondary load 2wt%Ru after drying prepares Ru-MoOx/CNT catalyst；This method includes following
Step:
1) Ru-MoOx/AC or Ru-MoOx/CNT multifunction catalyst is loaded on to the reaction tube flat-temperature zone of fixed bed reactors,
Replacing hydrogen is until air is replaced completely by hydrogen in fixed bed reactors at room temperature；
2) it is passed through hydrogen, while fixed bed reactors with the heating rate of 5 DEG C/min rise to 350 DEG C from room temperature and in 350 DEG C of perseverances
Warm 3-5 hours until Ru-MoOx/AC or Ru-MoOx/CNT multifunction catalyst sufficiently restores；
3) fixed bed reactors temperature is down to 140-300 DEG C of reaction temperature of setting, is that 5-30wt% sugar alcohol is water-soluble by concentration
Liquid and hydrogen enter fixed bed reactors by volume flow ratio 1:50-1:200 cocurrent, and control liquid air speed is 1.0-10.0h-1With
Hydrogen Vapor Pressure 2-10MPa, make sugar alcohol aqueous solution occur in fixed bed reactors under the multi phase state of evaporation-condensation alternately and repeatedly
Ru-MoOx/AC or Ru-MoOx/CNT catalyst surface selectivity deoxygenation is converted into amylalcohol and hexanol；
4) it is condensed from the gas-liquid mixture of fixed bed reactors outlet discharge through 2-10MPa high pressure, is separated into product liquid and not
Solidifying property gaseous product, product liquid are layered as oily phase and water phase, and oil is mutually the mixture of amylalcohol and hexanol；Water phase is for hydrolyzing work
Skill preparation hydrolysis sugar alcohol liquid, gas phase is mainly to have neither part nor lot in the excess hydrogen of reaction, is again introduced into after recycle compressor is pressurized solid
Fixed bed reactor cycles utilize.
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| US6291725B1 (en) * | 2000-03-03 | 2001-09-18 | Board Of Trustees Operating Michigan State University | Catalysts and process for hydrogenolysis of sugar alcohols to polyols |
| CN101613253A (en) * | 2008-06-25 | 2009-12-30 | 中国科学院大连化学物理研究所 | A kind of catalytic cracking method of sugar and sugar alcohol |
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| US6291725B1 (en) * | 2000-03-03 | 2001-09-18 | Board Of Trustees Operating Michigan State University | Catalysts and process for hydrogenolysis of sugar alcohols to polyols |
| CN101613253A (en) * | 2008-06-25 | 2009-12-30 | 中国科学院大连化学物理研究所 | A kind of catalytic cracking method of sugar and sugar alcohol |
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