CN110028984A - Biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst and its preparation method and application - Google Patents
Biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst and its preparation method and application Download PDFInfo
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- CN110028984A CN110028984A CN201910342392.2A CN201910342392A CN110028984A CN 110028984 A CN110028984 A CN 110028984A CN 201910342392 A CN201910342392 A CN 201910342392A CN 110028984 A CN110028984 A CN 110028984A
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- catalyst
- hydrogenation deoxidation
- pyrolysis liquid
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- oil
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/755—Nickel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/14—Phosphorus; Compounds thereof
- B01J27/185—Phosphorus; Compounds thereof with iron group metals or platinum group metals
- B01J27/1853—Phosphorus; Compounds thereof with iron group metals or platinum group metals with iron, cobalt or nickel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a kind of biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalysts and its preparation method and application.The component and content of catalyst are A) 5~25wt% of active metal；B) 0.1~5wt% of auxiliary agent；C) 70~90wt% of carrier；The active metal component includes two kinds or more of 3d and/or 4d metallic element；The auxiliary agent is one or more of IA, IIA and IIIA metallic element；The carrier is ball-aluminium oxide, and single pressure hardness is not less than 10 Ns, and hydro-thermal deactivation rate is not less than 1.5 days at 800 DEG C‑1.The invention also discloses the preparation method and application of catalyst.The present invention solves the problems, such as that biomass hydrogenation deoxidation oil of the existing technology is difficult to further hydrotreating.
Description
Technical field
The invention belongs to field of biological energy source, add hydrogen to split specifically, being related to a kind of biomass pyrolysis liquid hydrogenation deoxidation oil
Change catalyst and its preparation method and application.
Background technique
Biomass broadly includes all plants, microorganism and using plant, microorganism as the animal of food and its life
The waste of production, in the research and industrialization process of early period, people to the Study on Transformation of sugar, fat and cellulose based biomass compared with
It is more, and formed the production of industrialized scale.It is from a wealth of sources however, lignin-base biomass content is bigger, comparison sugar, fat,
The difficult situation of " strive grain with people, strive ground with grain " that cellulose based biomass faces in China, lignin-base biomass is then at me
State more shows as the agriculture and forestry organic waste material for having generated pollution already to environment, such as stalk, sawdust, shell.Blanket above-mentioned factor
It is not difficult to find that the conversion of lignin-base cellulose and resource utilization are the optimal raw materials of China's Biomass Energy Industry development.
However, lignin and sugar, fatty acid, algae oil, cellulose etc. more study mature life for chemically composition is upper
For physical resources there are essential distinction, lignin is aromatic hydrocarbons and side chain alkane oligomerization based on the phenylpropyl alcohol alkyl structure of natural polymerization
Product；And the latter is then based on the cellular constructions such as hexose, aliphatic ester, fatty acid.This two major classes compound is in chemical activity, heat
There are greatest differences in stabilization, other biological matter technology such as ferments, hydrolyzes, alcoholysis, acidolysis are difficult to use in lignin-base biology
Conversion.
Fast pyrolysis is considered as realizing the extensive pretreated optimal path of lignin-base biomass, however its output
Bio-oil still have the disadvantages that peracidity (PH2~3)；High-moisture (15~40%)；Rich oxygen content (35~
55%)；It is unstable；Low heat value 2 times of coal (units of heat price be)；Hardly possible is dissolved each other with petroleum-type product.So bio-oil
It is suffered restraints using market.Since the end of the nineties in last century, countries in the world start the technology of bio-oil extracting fuel oil successively
Research.Hydrogenation deoxidation, be hydrocracked, the paths such as hydroforming are widely studied, such as middle petrochemical industry Beijing Shi Keyuan, middle petrochemical industry Fushun
The mechanisms such as research institute, triumphant this energy science and technology company that crouches in Sichuan, Beijing University of Chemical Technology, Qingdao energy institute, East China University of Science disclose
By the catalyst of fast pyrolysis oil hydrogenation deoxidation；Middle petrochemical industry Fushun research institute, the Lanzhou Chemistry and Physics Institute, the Renmin University of China, China
The mechanisms such as the stone joint energy disclose the catalyst and process route that bio oil is hydrocracked；East China University of Science, U.S.'s prestige this
Kang Xing university etc. discloses the catalyst and process route of bio oil hydroforming.Wherein hydrogenation deoxidation process is more suitable for lignin
The processing of based biomass, the potentiality with large-scale industrial production, European Union Biocoup joint study plan and U.S. Department of Energy
Funded Projects respectively inquire into hydrogenation deoxidation catalyst, technique and long-term operation feasibility, and result of study shows to urge
There are serious mutual restricting relation between agent cost, catalyst life and product DNA vaccine, hydrogenation deoxidation oil must be carried out
Further hydrotreating.Therefore, the industry, which needs exploitation, can be used for the catalyst that hydrogenation deoxidation oil further adds hydrogen.
Summary of the invention
In order to solve the problems, such as that biomass hydrogenation deoxidation oil of the existing technology is difficult to further hydrotreating, the present invention
Provide a kind of biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst and preparation method thereof.
Biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst provided by the invention includes following components and content:
A) 5~25wt% of active metal；
B) 0.1~5wt% of auxiliary agent；
C) 70~90wt% of carrier；
The active metal component includes two kinds or more of 3d and/or 4d metallic element；
The auxiliary agent is one or more of IA, IIA and IIIA metallic element；
The carrier is ball-aluminium oxide, and single pressure hardness is 10~50N/, and hydro-thermal deactivation rate is at 800 DEG C
1.5~10 days-1。
3d metal in the active metal is Ni and/or Co, and 4d metal is W and/or Mo, total metal (in terms of oxide)
Content is preferably 10~20wt%, in terms of catalyst gross mass.
The content of the auxiliary agent is preferably 0.1~5wt%, in terms of catalyst gross mass.
The present invention also provides a kind of preparation methods of biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst, including
Following steps:
It 1) is mixing presoma with aluminum sulfate and aluminum nitrate, using urea as precipitating reagent, Al and urea concentration ratio be 1/20~
2/1, the ratio of aluminum sulfate and aluminum nitrate is 1/2~1/8；At 90~100 DEG C, 30~120min is reacted in oil bath, uses deionization
Water washing, less than 1%, obtains alumina precursor colloidal sol to conductivity and water inlet difference；
2) the alumina precursor colloidal sol that step 1) obtains is spray-dried at 150~240 DEG C, atomizer pressure is
0.2~0.6MPa, atomizer diameter are 10~30 μm；
3) alumina precursor for obtaining step 2) is calcined 0.5~24 hour at 500~900 DEG C, obtains spherical oxidation
Alumina supporter；
4) mixing salt solution of active metal and auxiliary agent distribution circulation is impregnated on spherical alumina support, dipping time
It is 1~4 time, and is dried overnight at 60~150 DEG C, and roasted at 350~600 DEG C, obtains catalyst.
In addition, the present invention provides the application of biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst, feature exists
In the catalyst is used for the hydrocracked, treated process of biomass pyrolysis liquid hydrogenation deoxidation oil, and the hydrogenation deoxidation oil comes from
Product after biomass pyrolysis liquid hydrogenation deoxidation, density are 0.8g/ml~0.95g/ml, and rate of oxygen is 1~18wt%.
After the hydrogenated cracking processing of hydrogenation deoxidation oil, rate of oxygen is reduced to 1~5wt%, and water content is reduced to 0.1~
The amount of the total aromatic hydrocarbons of 3wt%, mononuclear aromatics Zhan is 85~98wt%, and it is 2~40wt% that aromatic hydrocarbons, which accounts for organic matter ratio,.
The conversion temperature that the biomass pyrolysis liquid hydrogenation deoxidation oil is hydrocracked be 150~400 DEG C, hydrogen partial pressure be 3~
20atm, unit hydrogen consumption are 0.1~1.3.
The invention has the following beneficial effects:
It can efficiently complete to realize its commercialization and high added value to the hydro-upgrading of biomass pyrolysis liquid hydrogenation deoxidation oil
Change；
Catalyst strength height, water resistant good in thermal property, operation period is long, synthetic operation is at low cost；
Catalyst hydrogen consumption is lower, operating condition is mild, it can be achieved that extensive industrialization.
Specific embodiment
Below by embodiment, the present invention will be further described.
Embodiment 1
The preparation of 1.1 alumina precursors: the mixed solution of aluminum sulfate and aluminum nitrate that total concentration is 0.01mol/L is prepared
5L, wherein the ratio of aluminum sulfate and aluminum nitrate is 1/5, is denoted as solution A；Urea is added in room temperature, is stirred continuously to urea concentration and is
0.05mol/L is denoted as solution B.Solution B is heated to 90 DEG C with the temperature gradient of 5 DEG C/min, isothermal reaction 1 hour, is slowly dropped
It warms to room temperature, is replaced using 50L deionization moisture 5 times, obtain colloidal sol C, colloidal sol C is spray-dried at 160 DEG C, atomizer
Pressure is 0.2~0.6MPa, and atomizer diameter is 15 ± 0.2 μm.The alumina precursor of acquisition is small in 600 DEG C of calcinings 12
When, obtain spherical alumina support；
The load of 1.2 active metals: the alumina support of the above-mentioned acquisition of 50g is small with the maceration extract dipping 8 containing Ni-Mo
When, 120 DEG C drying 6 hours, three times, the catalyst precursor finally obtained rises to 500 DEG C with the rate of 10 DEG C/min to circulation, and
Constant temperature calcining 4 hours, obtaining catalyst was ECU-1.
The test of 1.3 catalyst strengths: intensity is surveyed to catalyst obtained, test result is as shown in table 1.
The test of 1.4 catalyst hydrothermal deactivations: catalyst hydro-thermal is carried out using self-built fixed fluidized bed device and subtracts fiery test.
Loading catalyst 200g, using 100% vapor, at 800 DEG C respectively to catalyst aging 1 day, 2 days, 5 days and 10 days, during which
The sample of ceramic filter outlet is collected, and collects the catalyst sample under different number of days processing.Using 50mL Parr
In water heating kettle under catalyst ECU-1 and different hydrothermal agings sample carry out active testing, be added 20ml hydrogenation deoxidation oil and
0.5g the catalyst, (10%H under 180 DEG C, 8atm pressure2in N2), use Teflon stir rotor mixing speed for
400rpm reacts 4 hours, measures process distribution curve and the oxygen content variation of raw material and product, by oxygen content decaying (%, nothing
Unit) it maps with the time, the hydrothermal deactivation rate of catalyst is measured, unit is day-1.The hydrothermal deactivation speed of surveyed catalyst sample
Rate is shown in Table 2.
Embodiment 2
The preparation of alumina precursor is as described in 1.1.By leaching of the alumina support containing Ni-Mo-P of the above-mentioned acquisition of 50g
Stain liquid impregnate 8 hours, 120 DEG C drying 6 hours, recycle three times, the catalyst precursor finally obtained is with the rate of 10 DEG C/min
500 DEG C, and constant temperature calcining 4 hours are risen to, obtaining catalyst is ECU-2.It is catalyzed respectively using the method as described in 1.3,1.4
Agent strength test and hydrothermal deactivation rate determination, are as a result listed in Tables 1 and 2 respectively.
Embodiment 3
The preparation of alumina precursor is as described in 1.1.By leaching of the alumina support containing Ni-Mo-Cr of the above-mentioned acquisition of 50g
Stain liquid impregnate 8 hours, 120 DEG C drying 6 hours, recycle three times, the catalyst precursor finally obtained is with the rate of 10 DEG C/min
500 DEG C, and constant temperature calcining 4 hours are risen to, obtaining catalyst is ECU-3.It is catalyzed respectively using the method as described in 1.3,1.4
Agent strength test and hydrothermal deactivation rate determination, are as a result listed in Tables 1 and 2 respectively.
Embodiment 4
The preparation of alumina precursor is as described in 1.1.By the dipping of the alumina support Ni-Mo-Cr of the above-mentioned acquisition of 50g
Liquid impregnates 8 hours, 120 DEG C drying 6 hours, the catalyst precursor finally obtained rises to 500 DEG C with the rate of 10 DEG C/min, and
Constant temperature calcining 4 hours, obtaining catalyst was ECU-4.Carried out respectively using the method as described in 1.3,1.4 catalyst strength test and
Hydrothermal deactivation rate determination, is as a result listed in Tables 1 and 2 respectively.
Embodiment 5
The mixed solution 5L of aluminum sulfate and aluminum nitrate that total concentration is 0.01mol/L is prepared, wherein aluminum sulfate and aluminum nitrate
Ratio be 1/10, room temperature be added urea, be stirred continuously to urea concentration be 0.05mol/L, be denoted as solution B.By solution B with 5
DEG C/temperature gradient of min is heated to 90 DEG C.Isothermal reaction 1 hour, slow cooling to room temperature, using 50L deionization moisture 5 times
Displacement obtains colloidal sol C；Colloidal sol C is spray-dried at 160 DEG C, atomizer pressure is 0.2~0.6MPa, and atomizer is straight
Diameter is 15 ± 0.2 μm.The alumina precursor of acquisition is calcined 12 hours at 600 DEG C, obtains spherical alumina support；Such as 1.2 institutes
State by Metal Supported on alumina support, obtain catalyst be ECU-5.It is urged respectively using the method as described in 1.3,1.4
Agent strength test and hydrothermal deactivation rate determination, are as a result listed in Tables 1 and 2 respectively.
Embodiment 6
The mixed solution 5L of aluminum sulfate and aluminum nitrate that total concentration is 0.01mol/L is prepared, wherein aluminum sulfate and aluminum nitrate
Ratio be 1/3, room temperature be added urea, be stirred continuously to urea concentration be 0.05mol/L, be denoted as solution B.By solution B with 5
DEG C/temperature gradient of min is heated to 98 DEG C.Isothermal reaction 1 hour, slow cooling to room temperature, using 50L deionization moisture 5 times
Displacement obtains colloidal sol C；Colloidal sol C is spray-dried at 160 DEG C, atomizer pressure is 0.2~0.6MPa, and atomizer is straight
Diameter is 15 ± 0.2 μm.The alumina precursor of acquisition is calcined 12 hours at 600 DEG C, obtains spherical alumina support；Such as 1.2 institutes
State by Metal Supported on alumina support, obtain catalyst be ECU-6.It is urged respectively using the method as described in 1.3,1.4
Agent strength test and hydrothermal deactivation rate determination, are as a result listed in Tables 1 and 2 respectively.
1 catalyst strength test result of table
2 catalyst hydrothermal deactivation rate test result of table
Claims (8)
1. a kind of biomass pyrolysis liquid hydrogenation deoxidation oil hydrocracking catalyst, it is characterised in that including following components and content:
A) 5~25wt% of active metal；
B) 0.1~5wt% of auxiliary agent；
C) 70~90wt% of carrier；
The active metal component includes two kinds or more of 3d and/or 4d metallic element；
The auxiliary agent is one or more of IA, IIA and IIIA metallic element；
The carrier be ball-aluminium oxide, single pressure hardness 10~50N/, the hydro-thermal deactivation rate 1.5~10 at 800 DEG C
It-1, the content is in terms of catalyst gross mass.
2. catalyst according to claim 1, it is characterised in that: the 3d metal in the active metal is Ni and/or Co,
4d metal is W and/or Mo, and total metal contents in soil is 10~20wt%.
3. catalyst according to claim 1, it is characterised in that: the content of the auxiliary agent is 0.1~5wt%.
4. a kind of preparation method of catalyst described in claim 1, it is characterised in that include the following steps:
It 1) is mixing presoma with aluminum sulfate and aluminum nitrate, using urea as precipitating reagent, Al and urea concentration ratio are 1/20~2/1,
The ratio of aluminum sulfate and aluminum nitrate is 1/2~1/8；At 90~100 DEG C, 30~120min is reacted in oil bath, is washed with deionized water
It washs to conductivity and water inlet difference less than 1%, obtains alumina precursor colloidal sol；
2) the alumina precursor colloidal sol that step 1) obtains is spray-dried at 150~240 DEG C, atomizer pressure is 0.2
~0.6MPa, atomizer diameter are 10~30 μm；
3) alumina precursor for obtaining step 2) is calcined 0.5~24 hour at 500~900 DEG C, obtains spherical alumina load
Body；
4) mixing salt solution of active metal and auxiliary agent distribution circulation is impregnated on spherical alumina support, dipping time 1
~4 times, and be dried overnight at 60~150 DEG C, and roasted at 350~600 DEG C, obtain catalyst.
5. a kind of application of catalyst described in claim 1, it is characterised in that: the catalyst adds hydrogen for biomass pyrolysis liquid
The hydrocracked, treated process of deoxidation oil.
6. application according to claim 5, it is characterised in that: the hydrogenation deoxidation oil adds hydrogen from biomass pyrolysis liquid
Product after deoxidation, density are 0.8g/ml~0.95g/ml, and rate of oxygen is 1~18wt%.
7. application according to claim 5, it is characterised in that: oxygen-containing after the hydrogenated cracking processing of hydrogenation deoxidation oil
Rate is reduced to 1~5wt%, and water content is reduced to 0.1~3wt%, and the amount of the total aromatic hydrocarbons of mononuclear aromatics Zhan is 85~98wt%, aromatic hydrocarbons
Accounting for organic matter ratio is 2~40wt%.
8. application according to claim 5, it is characterised in that: what the biomass pyrolysis liquid hydrogenation deoxidation oil was hydrocracked
Conversion temperature is 150~400 DEG C, and hydrogen partial pressure is 3~20atm, and unit hydrogen consumption is 0.1~1.3.
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| CN102531015A (en) * | 2011-05-26 | 2012-07-04 | 中国科学院福建物质结构研究所 | Method for preparing porous aluminum oxide superfine powder |
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| CN108686702A (en) * | 2018-06-06 | 2018-10-23 | 重集团大连工程建设有限公司 | Ebullated bed coal tar hydrogenating handles-it is hydrocracked composite catalyst and preparation method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4870044A (en) * | 1987-03-12 | 1989-09-26 | Phillips Petroleum Company | Treated alumina material for fixed hydrofining beds |
| JP2008212798A (en) * | 2007-03-01 | 2008-09-18 | Jgc Catalysts & Chemicals Ltd | Alumina carrier, hydrogenation demetallation catalyst using it, and manufacturing method thereof |
| CN101831328A (en) * | 2010-05-21 | 2010-09-15 | 张小红 | Green fuel oil and preparation method thereof |
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| US20140221712A1 (en) * | 2013-02-01 | 2014-08-07 | Lummus Technology Inc. | Upgrading raw shale-derived crude oils to hydrocarbon distillate fuels |
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Application publication date: 20190719 |