CN105439189B - Method and device for preparing aromatic liquid fuel by adopting successive two-step method - Google Patents
Method and device for preparing aromatic liquid fuel by adopting successive two-step method Download PDFInfo
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Abstract
The invention discloses a method for preparing aromatic liquid fuel by adopting a successive two-step method. The method comprises the following steps: mixing ethyl alcohol with bio oil fraction according to the mass ratio of ethyl alcohol to bio oil fraction being (1:3)-(1:1), so as to obtain a reaction raw material; performing atomization on the reaction raw material, and introducing atomized reaction raw material to two fixed bed reactors successively, wherein the outlet product of the second fixed bed reactor is collected and separated after condensation, so as to obtain an oil-phase product, which is the aromatic liquid fuel; the first fixed bed reactor is filled with a Pd/SiO2 catalyst, and the second fixed bed reactor is filled with an HZSM-5 catalyst; the invention further relates to a reaction device for preparing the aromatic liquid fuel by adopting the successive two-step method. The method and device provided by the invention further solve the problem that the catalyst is prone to coking and deactivation in the conventional cracking process, the reaction activity and stability are improved, and the conversion rate of bio oil fraction into the aromatic liquid fuel is increased.
Description
Technical field
The present invention relates to organic synthesis field, and in particular to a kind of method that continuous two-step method produces fragrant hydrocarbon liquid fuel
And device.
Background technology
As the day by day exhaustion of global fossil energy is increasingly serious with environmental problem, exploitation regenerative resource becomes compels
The heat subject of the eyebrows and eyelashes.Biomass energy receives the extensive concern of people as a kind of regenerative resource of cleaning.Biomass are fast
Speed heat cracking is a kind of important thermochemical study method, biomass material can be converted into into bio oil.However, rough bio oil
The features such as inferior quality, rich oxygen content, high-moisture, corrosivity and low heat value, limits its high-grade and utilizes.
Catalytic cracking is a kind of conventional bio oil modification technology, by the oxygen in bio oil with CO, CO2And H2The form of O takes off
Remove, produce the liquid fuel of aromatic hydrocarbon.However, the component in bio oil is sufficiently complex, by groups such as ketone, acid, aldehyde, phenol and carbohydrates
There is obvious carbon distribution trend into, macromolecular phenol polymer therein and carbohydrate, be very easy to cause catalyst coking and deactivation.
Therefore, bio oil crude oil full constituent is modified produces fragrant hydrocarbon liquid fuel and is difficult to.Molecular clock is a kind of efficient separation
Technology.Different from traditional vacuum distillation, it can overcome the coking of thermal sensitivity bio oil, and cause different same clans compound
Separation and concentration.Therefore, the study on the modification based on bio oil molecular clock cut is more meaningful.Due to biological oil distillate available hydrogen
Carbon ratio ((H/C)eff=(H-2O)/C) it is still relatively low, easy carbon distribution causes catalyst quick in traditional catalytic cracking process
Inactivation.
Researcher is had at present by the typical modelling thing acetic acid using biological oil distillate, hydroxypropanone-, cyclopentanone and second
Alcohol concerted reaction, and using solid acid catalyst HZSM-5, the carbon selectivity that can make aromatic hydrocarbon reaches 48% or so
(Chinese Journal of Catalysis 2014,35,709-722).But, also generate under the catalyst action
More C3, C4 gaseous hydrocarbons, the concentration in tail gas can reach more than 50%, and this have impact on the selectivity of aromatic hydrocarbon, need
Further to strengthen the aromatization in modifying process；Meanwhile, also containing the single phenyl ring phenols in part and aldehyde in biological oil distillate
Class, this kind of material deoxidation aromatisation under conventional H ZSM-5 catalyst is less efficient.Chinese invention patent (CN104152175A,
Publication date is 2014.11.19) a kind of method that aromatic hydrocarbon is prepared by biological oil distillate is disclosed, by biological oil distillate and ethanol
Mixed liquor is mixed to get, fixed bed reactors are entered Jing after atomization, catalytic reaction occurs on a catalyst, product is condensed
And gas-liquid separation, the product liquid of collection is described aromatic hydrocarbon.Catalyst is bifunctional catalyst in the technical scheme
Ga2O3/ HZSM-5, products therefrom includes single phenyl ring hydro carbons, heterocycle and polycyclic hydro carbons.Split altogether by adding alcohols in research
Change, achieve good cracking effect.But altogether ethanol Blend proportion is still higher in cracking process, while containing in biological oil distillate
Phenols, there is relatively low reactivity and stronger carbon distribution trend, very unfavorable to prolonged cracking reaction.Therefore, it is traditional
Bio oil catalytic cracking process is required further improvement.
The content of the invention
Present invention aims to the deficiencies in the prior art, there is provided a kind of continuous two-step method produces fragrant hydrocarbon liquid combustion
The method and device of material, further solve the problems, such as it is conventional cracking during the easy coking and deactivation of catalyst, increased reaction
Activity and stability, improve biological oil distillate to the transformation efficiency of fragrant hydrocarbon liquid fuel.
The invention discloses a kind of method that continuous two-step method produces fragrant hydrocarbon liquid fuel, step is as follows：
By ethanol and biological oil distillate in mass ratio 1:3～1:1 ratio mixing, obtains reaction raw materials；By reaction raw materials
Two fixed bed reactors are continued through after atomization, is collected after second fixed bed reactors outlets products is condensed and is separated
Obtain oil-phase product, as described fragrant hydrocarbon liquid fuel；
First fixed bed reactors loads Pd/SiO2Catalyst, and it is passed through H simultaneously in reaction raw materials2, mass space velocity
For 0.5～5h-1, reaction temperature is 250～350 DEG C, and reaction pressure is 1～6MPa；Second fixed bed reactors loads HZSM-
5 catalyst, reaction temperature is 350～450 DEG C, and reaction pressure is 1～6MPa.
Further preferably, the reaction temperature of first described fixed bed reactors is 280～320 DEG C, and reaction pressure is 3
～4MPa；The reaction temperature of second fixed bed reactors is 370～430 DEG C, and reaction pressure is 3～4MPa.
Biological oil distillate to the conversion of fragrant hydrocarbon liquid fuel is filled in a set of reaction by two fixed bed reactors series connection
Complete in putting, biological oil distillate continues through two fixed bed reactors after atomization, reaction atmosphere is H2.Due to bio oil
Cut has higher oxygen content and degree of unsaturation, and hydrogen content is relatively low, therefore individually cut is easy in course of reaction
The middle coke for forming low hydrogen-carbon ratio.In first fixed bed reactors, biological oil distillate first adsorbs in Pd/SiO2Catalyst table
Face, while Pd can effectively by H2Activation, the subsequently unsaturated double-bond generation addition reaction in active hydrogen atom and cut,
The poor oxygenatedchemicals of cracking activity is converted into the hydrogen-rich compound for being easier to cracking, such as ketone is converted into alcohols, acids
Esters are converted into, furfuran compound is converted into alcohols or gaseous product, and phenols is first converted into ketone and then is converted into alcohols, greatly
Amplitude improves effective hydrogen-carbon ratio and saturation degree of reactant.
In second fixed bed reactors, the reactant of hydrogen-rich is directly entered in reactor in high-temperature gas form,
First there is deoxygenation in the presence of HZSM-5 catalyst and generate light olefin intermediate product, and then aromatisation effect generation occurs
Aromatic hydrocarbon.Because the effective hydrogen-carbon ratio of reactant into cracker is very high, thus the situation of carbon distribution is bright in deoxygenation
It is aobvious to improve, Catalysts Deactivation Problems are preferably solved, so as to ensure being smoothed out for follow-up aromatisation effect.Using two sections
Continous way method for hydrogen cracking produces fragrant hydrocarbon liquid fuel, on the one hand, is conducive to the Efficient Conversion of reaction raw materials, and reduces energy
The loss of amount；On the other hand, continuity and operability are good, reduce loss when reactant is transported in feed and reactor,
Avoid hydrogenation products that condensation reaction occurs during storage to go bad, compared with the reaction of two sections of partition types industry is significantly facilitated
Change.
Described biological oil distillate preparation method is：Biomass obtain bio oil through fast pyrolysis, and bio oil is passed through
Molecular clock obtains biological oil distillate, and vapo(u)rizing temperature is 90～130 DEG C, and distillation pressure is 600～1000Pa.Described molecule steams
Evaporate and prepare the method that the process of biological oil distillate may be referred in the A of Publication No. CN 102206141 and carry out.
The Mass Distribution of the biological oil distillate be carboxylic acid compound 28～40%, ketone compounds 38～54%, aldehyde
Class compound 3～8%, single benzene ring phenolic compound 8～18%, ester type compound 1～3% does not contain macromolecular carbohydrate and phenol
Birds of the same feather flock together compound.
Further preferably, the Mass Distribution of the biological oil distillate be hydroxypropanone- 34～42%, cyclopentanone 4～12%,
Acetic acid 30～40%, phenol 3～6%, guaiacol 5～12% and furfural 4～6%.
Described Pd/SiO2Catalyst, carrier is Nano-meter SiO_22, the load capacity of Pd is 0.5～8wt%, preferably 2～
5wt%, more preferably 3wt%.Described Pd/SiO2The preparation method of catalyst is：Equi-volume impregnating, by nanometer
SiO2Sample impregnated in PdCl2In solution, after standing 12 hours, mixture is dried at 110 DEG C, and in 550 DEG C of roastings 5
Hour, final sizing into 40～60 mesh little particle, described Pd/SiO2The average grain diameter of Pd is 1～15nm in catalyst, excellent
Elect 3～7nm as.
The silica alumina ratio of described HZSM-5 catalyst is 10～200, preferably 15～100, still more preferably for 20～
50, specific surface area is 200～350m2/g。
Described ethanol and the mass ratio of biological oil distillate is preferably 1:3～1:1, more preferably 2:3～1:1.Second
Alcohol can be easier to generate alkene by direct intramolecular dehydration, and alkene (H/C=2) forms aromatic hydrocarbon (1≤H/ in aromatisation
C ＜ 2) during, hydrogen atom more than needed, the H in hydrogen atom and atmosphere more than needed can be produced2Synergy, supply is biological
The deoxidation aromatization process of oil distillate, promotes its conversion to aromatic hydrocarbon.
Present invention also offers a kind of continuous two-step method produces the reaction unit of fragrant hydrocarbon liquid fuel, described reaction dress
Put including：Feed well, feed pump, mass flow controller, bypass, atomising device, first fixed bed reactors, Heat preservation
System, second fixed bed reactors, gas-liquid separator, flowmeter, gas chromatograph and fluid reservoir；
Described feed pump connects feed well and atomising device；Described mass flow controller and bypass is connected in parallel mist
Makeup is put, for controlling H2Flow velocity；Described atomising device connects first fixed bed reactors, and positioned at first fixation
Bed reactor front end；First described fixed bed reactors are connected in series with second fixed bed reactors, at connecting pipeline
Heat preservation system is provided with, second fixed bed reactors is connected in series the gas-liquid separator with cooling water circulation cooling, institute
The gentle chromatography of gas vent difference connection flow gauge of the gas-liquid separator stated, the liquid outlet connection storage of gas-liquid separator
Flow container, the liquid that fluid reservoir is collected is analyzed using the method for off-line analysis.First fixed bed reactors loads Pd/SiO2Catalysis
Agent, second fixed bed reactors load HZSM-5 catalyst.
In described reaction unit, biological oil distillate through feed well, feed pump and atomising device, into first fixation
Bed reactor and second fixed bed reactors, eventually pass gas-liquid separator and collect product.Described produces fragrant hydrocarbon liquid
The method of fuel is specifically applied in described reaction unit, further increases reactant transformation in planta rate；The course of reaction
Can continuously continual reaction, while expanding production can also be industrialized, improve efficiency.
Compared with the existing technology, beneficial effects of the present invention are embodied in：
(1) fragrant hydrocarbon liquid fuel is produced using two sections of continous way method for hydrogen cracking, on the one hand, be conducive to reaction raw materials
Efficient Conversion, and reduce the loss of energy；On the other hand, continuity and operability are good, and reduction reactant is in feed and instead
Answer in device loss during conveying, it is to avoid hydrogenation products occur that condensation reaction is rotten during storage, it is anti-with two sections of partition types
Should compare and significantly facilitate industrialization；
(2) hydrogenation process of first paragraph improves effective hydrogen-carbon ratio of reactant, enhance second segment reaction activity and
Stability, promotes the synergy of deoxidation and aromatisation, not only increases biological oil distillate and changes into fragrant hydrocarbon liquid fuel
Transformation efficiency, but also preferably solve the problems, such as catalyst coking and deactivation.In the present invention, reactant transformation in planta rate can
Up to 99%, arene content reaches 93% in oil phase, predominantly the important industrial chemicals such as benzene,toluene,xylene, catalyst
Life-span up to tens of hours more than.
Description of the drawings
Fig. 1 is the structural representation of reaction unit in embodiment.
In figure：1 feed well；2 feed pumps；3 mass flow controllers；4 bypasses；5 atomising devices；6 first fixed beds are anti-
Answer device；7 Heat preservation systems；8 second fixed bed reactors；9 gas-liquid separators；10 flowmeters；11 gas chromatographs；12 storages
Flow container.
Specific embodiment
Present invention is described further below in conjunction with the accompanying drawings.
A kind of continuous two-step method as shown in Figure 1 produces the reaction unit of fragrant hydrocarbon liquid fuel, and reaction unit includes：
Feed well 1, feed pump 2, mass flow controller 3, bypass 4,5, first fixed bed reactors 6, Heat preservation of atomising device
System 7, second fixed bed reactors 8, gas-liquid separator 9, flowmeter 10, gas chromatograph 11 and fluid reservoir 12；
Feed pump 2 connects feed well 1 and atomising device 5；Mass flow controller 3 and bypass 4 are connected in parallel atomising device
5, for controlling H2Flow velocity；Atomising device 5 connects first fixed bed reactors 6, and positioned at first fixed bed reactors 6
Front end；First fixed bed reactors 6 is connected in series with second fixed bed reactors 8, and Heat preservation is provided with connecting pipeline
System 7, second fixed bed reactors 8 are connected in series the gas-liquid separator 9 with cooling water circulation cooling, gas-liquid separator 9
Respectively connection flow gauge 10 and gas chromatograph 11 carry out on-line analysis, the liquid outlet connection of gas-liquid separator 9 to gas vent
Fluid reservoir 12, the liquid fuel collected is analyzed using off-line analysis method；First fixed bed reactors 6 loads Pd/SiO2
Catalyst, second fixed bed reactors 8 load HZSM-5 catalyst.
Embodiment 1
By quality consist of 40% hydroxypropanone-, 10% cyclopentanone, 30% acetic acid, 5% phenol, 10% guaiacol and
The biological oil distillate of 5% furfural, with ethanol with 1:1 mass ratio homogeneous mixture, and be placed in feed well 1.First
3g Pd/SiO are loaded in individual fixed bed reactors 62Catalyst, second filling 3g of fixed bed reactors 8 commercial HZSM-5,
Its silica alumina ratio is 25, and specific surface area is 340m2/g.For Pd/SiO2Catalyst, is prepared, concrete steps using equi-volume impregnating
It is as follows：By 0.5g PdCl2Powder is dissolved in 16ml deionized waters, and PH is adjusted to into 3 prepared PdCl with hydrochloric acid2Solution, then will
9.7g Nano-meter SiO_22Sample impregnated in the PdCl2In solution, after standing 12 hours, mixture is dried at 110 DEG C, and
550 DEG C of roastings 5 hours, final sizing into 40～60 mesh little particle, gained Pd/SiO2The average grain diameter of Pd is in catalyst
4nm, load capacity is 3wt%.Reduction treatment is carried out to it before reaction, reducing condition is 350 DEG C of normal pressure, recovery time 2h, hydrogen
Flow 30ml/min.Question response device is down to after room temperature and starts boosting, opens hydrogen valve by 4 rapid pressures of bypass to 4MPa,
Bypass 4 is closed, mass flow controller 3 is opened, and is 30ml/min by flow set.Then it is respectively that first fixed bed is anti-
Answer device 6 and second fixed bed reactors 8 to be warming up to 300 DEG C and 400 DEG C, feed pump 2 is opened after gas flow is stable, and will
Feed rate is set to 0.05ml/min, starts charging.High temperature gas-phase product is by the gas-liquid point with cooling water circulation cooling
From oil phase and water-phase product that device 9 obtains being layered, final oil-phase product is obtained by separating.In this embodiment, react
Thing transformation in planta rate be 99%, arene content reaches 93% in oil phase, and remaining is aliphatic hydrocarbon, reaction 22h in catalyst not
There is inactivation.
Embodiment 2
Similar to Example 1, the temperature for differing only in cracking reaction is 370 DEG C.Reactant transformation in planta rate is 81%,
Arene content is 74% in oil phase, and inactivation does not occur in catalyst in reaction 16h.
Embodiment 3
Similar to Example 1, the temperature for differing only in cracking reaction is 430 DEG C.Reactant transformation in planta rate is 99%,
Arene content reaches 90% in oil phase, and inactivation does not occur in catalyst in reaction 22h.
Embodiment 4
Similar to Example 1, the mixing proportion for differing only in ethanol and biological oil distillate is 2:3.Reactant integrally turns
Rate is 96%, and arene content is 87% in oil phase, and inactivation does not occur in catalyst in reaction 16h.
Embodiment 5
Similar to Example 1, it is 2 that difference is the mixing proportion of ethanol and biological oil distillate:3, the temperature of cracking reaction
For 370 DEG C.Reactant transformation in planta rate is 76%, and arene content is 69% in oil phase, and catalyst does not occur in reaction 12h
Inactivation.
Embodiment 6
Similar to Example 1, it is 2 that difference is the mixing proportion of ethanol and biological oil distillate:3, the temperature of cracking reaction
For 430 DEG C.Reactant transformation in planta rate is 96%, and arene content is 86% in oil phase, and catalyst does not occur in reaction 16h
Inactivation.
Embodiment 7
It is similar to Example 1, differ only in biological oil distillate quality consist of 38% hydroxypropanone-, 8% cyclopentanone,
34% acetic acid, 5% phenol, 9% guaiacol and 6% furfural.Reactant transformation in planta rate is 98%, and arene contains in oil phase
Amount reaches 90%, and inactivation does not occur in catalyst in reaction 22h.
Embodiment 8
It is similar to Example 1, differ only in biological oil distillate quality consist of 36% hydroxypropanone-, 6% cyclopentanone,
38% acetic acid, 6% phenol, 10% guaiacol and 4% furfural.Reactant transformation in planta rate is 96%, arene in oil phase
Content is 88%, and inactivation does not occur in catalyst in reaction 16h.
Embodiment 9
It is similar to Example 1, difference be the quality of biological oil distillate consist of 38% hydroxypropanone-, 8% cyclopentanone,
The mixing proportion of 34% acetic acid, 5% phenol, 9% guaiacol and 6% furfural, ethanol and biological oil distillate is 2:3.Reactant
Transformation in planta rate is 95%, and arene content is 85% in oil phase, and inactivation does not occur in catalyst in reaction 16h.
Embodiment 10
It is similar to Example 1, difference be the quality of biological oil distillate consist of 36% hydroxypropanone-, 6% cyclopentanone,
The mixing proportion of 38% acetic acid, 6% phenol, 10% guaiacol and 4% furfural, ethanol and biological oil distillate is 2:3.Reactant
Transformation in planta rate is 93%, and arene content is 81% in oil phase, and inactivation does not occur in catalyst in reaction 12h.
Embodiment 11
It is similar to Example 1, the HZSM-5 for using is differed only in, its silica alumina ratio is 40, and specific surface area is 280m2/g。
Reactant transformation in planta rate is 99%, and arene content is 91% in oil phase, and inactivation does not occur in catalyst in reaction 22h.
Embodiment 12
Similar to Example 1, difference is to prepare Pd/SiO2By 0.3g PdCl during catalyst2Powder be dissolved in 11ml go from
In sub- water, the Pd/SiO of gained2In catalyst, the average grain diameter of Pd is 5nm, and load capacity is 2wt%.Reactant transformation in planta rate
For 98%, arene content is 91% in oil phase, and inactivation does not occur in catalyst in reaction 20h.
Claims (8)
1. a kind of method that continuous two-step method produces fragrant hydrocarbon liquid fuel, it is characterised in that step is as follows：
By ethanol and biological oil distillate in mass ratio 1:3～1:1 ratio mixing, obtains reaction raw materials；Reaction raw materials are passed through
Two fixed bed reactors are continued through after atomization, collects isolated after second fixed bed reactors outlets products is condensed
Oil-phase product, as described fragrant hydrocarbon liquid fuel；
First fixed bed reactors loads Pd/SiO2Catalyst, and it is passed through H simultaneously in reaction raw materials2, mass space velocity is 0.5
～5h-1, reaction temperature is 250～350 DEG C, and reaction pressure is 1～6MPa；Second fixed bed reactors filling HZSM-5 catalysis
Agent, reaction temperature is 350～450 DEG C, and reaction pressure is 1～6MPa；
The Mass Distribution of the biological oil distillate be carboxylic acid compound 28～40%, ketone compounds 38～54%, aldehydes
Compound 3～8%, single benzene ring phenolic compound 8～18%, ester type compound 1～3%, does not contain macromolecular carbohydrate and phenols is poly-
Compound；
Described Pd/SiO2Catalyst, carrier is Nano-meter SiO_22, the load capacity of Pd is 0.5～8wt%.
2. the method that continuous two-step method according to claim 1 produces fragrant hydrocarbon liquid fuel, it is characterised in that described
Biological oil distillate preparation method is：Biomass obtain bio oil through fast pyrolysis, and bio oil is given birth to through molecular clock
Thing oil distillate, vapo(u)rizing temperature is 90～130 DEG C, and distillation pressure is 600～1000Pa.
3. the method that continuous two-step method according to claim 1 produces fragrant hydrocarbon liquid fuel, it is characterised in that the life
The Mass Distribution of thing oil distillate is hydroxypropanone- 34～42%, cyclopentanone 4～12%, acetic acid 30～40%, phenol 3～6%, more
The wooden phenol 5～12% of wound and furfural 4～6%.
4. the method that continuous two-step method according to claim 1 produces fragrant hydrocarbon liquid fuel, it is characterised in that described
Pd/SiO2The preparation method of catalyst is：Equi-volume impregnating, by Nano-meter SiO_22Sample impregnated in PdCl2In solution, standing
After 12 hours, mixture is dried at 110 DEG C, and in 550 DEG C of roastings 5 hours, final sizing into 40～60 mesh little particle,
Described Pd/SiO2The average grain diameter of Pd is 1～15nm in catalyst.
5. the method that continuous two-step method according to claim 1 produces fragrant hydrocarbon liquid fuel, it is characterised in that described
The silica alumina ratio of HZSM-5 catalyst is 10～200, and specific surface area is 200～350m2/g。
6. the method that continuous two-step method according to claim 1 produces fragrant hydrocarbon liquid fuel, it is characterised in that described
The reaction temperature of first fixed bed reactors is 280～320 DEG C, and reaction pressure is 3～4MPa；Second fixed bed reactors
Reaction temperature be 370～430 DEG C, reaction pressure be 3～4MPa.
7. the method that continuous two-step method according to claim 1 produces fragrant hydrocarbon liquid fuel, it is characterised in that described
The mass ratio of ethanol and biological oil distillate is 2:3～1:1.
8. a kind of continuous two-step method produces the reaction unit of fragrant hydrocarbon liquid fuel, it is characterised in that described reaction unit bag
Include：Feed well, feed pump, mass flow controller, bypass, atomising device, first fixed bed reactors, Heat preservation system
System, second fixed bed reactors, gas-liquid separator, flowmeter, gas chromatograph and fluid reservoir；
Described feed pump connects feed well and atomising device；
Described mass flow controller and bypass is connected in parallel atomising device, for controlling H2Flow velocity；
Described atomising device connects first fixed bed reactors, and positioned at the front end of first fixed bed reactors；
First described fixed bed reactors are connected in series with second fixed bed reactors, insulation is provided with connecting pipeline and is added
Hot systems, second fixed bed reactors are connected in series the gas-liquid separator with cooling water circulation cooling, described gas-liquid point
From the gentle chromatography of gas vent difference connection flow gauge of device, the liquid outlet of described gas-liquid separator connects liquid storage
Tank；
Described first fixed bed reactors filling Pd/SiO2Catalyst, second fixed bed reactors filling HZSM-5 catalysis
Agent.
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