CN109126812A - Utilize the method for long-chain natural plants wax in production of biodiesel - Google Patents

Utilize the method for long-chain natural plants wax in production of biodiesel Download PDF

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Publication number
CN109126812A
CN109126812A CN201811081074.7A CN201811081074A CN109126812A CN 109126812 A CN109126812 A CN 109126812A CN 201811081074 A CN201811081074 A CN 201811081074A CN 109126812 A CN109126812 A CN 109126812A
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catalyst
biodiesel
natural plants
hydrogen
auxiliary agent
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CN201811081074.7A
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叶活动
陈丹
林泽虎
谢运羲
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LONGYAN ZHUOYUE NEW ENERGY CO Ltd
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LONGYAN ZHUOYUE NEW ENERGY CO Ltd
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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
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • 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
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/883—Molybdenum and nickel
    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/42—Refining of petroleum waxes
    • 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
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)
  • Fats And Perfumes (AREA)

Abstract

The invention discloses a kind of methods using long-chain natural plants wax in production of biodiesel, it prepares the natural plants wax of C15~C24 using Long carbon chain C16~C24 fatty acid methyl ester as raw material；(1) Ni-Co-Mo/Al is prepared3O2Catalyst: Al will be added after ammonium molybdate and auxiliary agent I citric acid deionized water dissolving3O2Carrier supersaturation absorption, excessive adsorption liquid is concentrated with temperature programming again, and then the catalyst obtained after drying is roasted, catalyst after roasting is impregnated in again in the mixed aqueous solution of nickel nitrate, cobalt nitrate and auxiliary agent II alkali metal soln, above-mentioned drying and calcination steps are repeated after carrying out supersaturated absorption, obtain Ni-Co-Mo/Al3O2Catalyst；(2) catalyst is passed through hydrogen and vulcanizing agent is vulcanized and restored；(3) catalysis reaction: being passed through the reactor equipped with catalyst simultaneously with hydrogen after fatty acid methyl ester is preheated, product obtains C15~C24 natural plants wax through separating rectifying after reaction.Present invention process is simple, low manufacture cost, stable product quality.

Description

Utilize the method for long-chain natural plants wax in production of biodiesel
Technical field
The present invention relates to a kind of methods of biodiesel deep processing, belong to catalysis technique and biodiesel application field, tool Body relates to the use of the method for long-chain natural plants wax in production of biodiesel.
Background technique
It is reacted by propagation waste oil rouge with methanol, the biodiesel (rouge handled by chemical technologies such as esterification alcoholysis Fatty acid methyl esters) it is typical " green energy resource ", there are the advantages such as sulfur content is low, flash-point is high, but exist simultaneously freezing point high and low temperature Poor fluidity is oxidized easily the defects of rotten, therefore to obtain, added value is higher and product matter by carrying out deep processing to it Better product is measured, disadvantages described above can be effectively solved.
104250558 A of Chinese patent CN discloses a kind of method of fatty acid ester through hydrogenation production n-alkane, this method Carrying out pre-add hydrogen to aliphatic ester first reduces iodine number, add product after hydrogen again go into the reactor of hydrogenation deoxidation catalyst into Row hydrogenation deoxidation, decarbonylation, decarboxylic reaction obtain C15~C18 n-alkane.This method, which has a defect that, needs secondary plus hydrogen, adds Hydrogen technique is cumbersome.
106350096 A of Chinese patent CN discloses a kind of biodiesel hydrogenation deoxidation technique, it uses fixed bed reaction Device, there are three types of the compound and catalyst promoter of different mesopore molecular sieves, catalyst life is small up to 500 for filling in reactor When above catalytic activity without being decreased obviously, but catalyst preparation process is complicated, higher cost.
103666519 A of Chinese patent CN discloses the method that non-edible animals and plants oil hydrogenation deoxidation prepares alkane, uses The nickel molybdenum catalyst of cerium oxide and silica containing 3~5wt%, non-edible animals and plants oil are added in the presence of hydrocarbon solvent Hydrogen deoxidation, most preferably 320~380 DEG C of reaction temperature.This method has a defect that reaction temperature is higher, and using a large amount of molten Agent, need to separate solvent again causes process for refining complexity, energy consumption higher.
Summary of the invention
The object of the present invention is to provide a kind of simple process, low manufacture cost, the utilization biodiesel of stable product quality The method of long-chain natural plants wax in production.
In order to achieve the above object, the present invention is using the method for long-chain natural plants wax in production of biodiesel with C16~C24 Fatty acid methyl ester is raw material, and the natural plants wax of C15~C24 is prepared by the method for Industrial Catalysis, specific steps are as follows:
(1)Ni-Co-Mo/Al3O2The preparation of catalyst: ammonium molybdate and auxiliary agent I citric acid are used deionized water by the first step Sufficiently dissolution adds the Al that granularity after drying is 40-60 mesh3O2Carrier carries out supersaturation absorption 12h；Second step uses vacuum Excessive adsorption liquid is concentrated in baking oven temperature programming, and technological parameter is 60 DEG C/4h-, 80 DEG C/2h-, 120 DEG C/8h；Third step is dry The catalyst obtained afterwards is placed in Muffle furnace and carries out temperature-programmed calcination again, technological parameter be room temperature~300 DEG C, 5 DEG C/min, 300 DEG C of holding 2h；300~500 DEG C, 5 DEG C/min, 500 DEG C of holding 4h；Catalyst after 4th one-step baking is impregnated in nitric acid again 12h in the mixed aqueous solution of nickel, cobalt nitrate and auxiliary agent II alkali metal soln repeats above-mentioned drying and roasting step after supersaturation absorption Suddenly, Ni-Co-Mo/Al is obtained3O2Catalyst；Wherein, metal component content be in molar ratio Ni 10~20%, Co 30~ 50%, 40~50% Mo, content of metal are calculated as 16~20% according to oxide weight, auxiliary agent I citric acid solution mass concentration 1~3%, auxiliary agent II alkali metal soln mass concentration 1~5%；
(2) by Catalyst packing into fixed bed reactors, 190 catalyst vulcanization and reduction: are warming up to after nitrogen purging DEG C, while it being passed through hydrogen and vulcanizing agent vulcanization 2h, it is warming up to 230 DEG C and continues to vulcanize 4h, stopping is passed through vulcanizing agent, reactor heating Hydrogen reducing 4h after to 300 DEG C；
(3) it catalysis reaction: by biodiesel after preheater is preheated to 40~50 DEG C, then is passed through to be equipped with simultaneously with hydrogen and urge The fixed bed reactors of agent, 300~330 DEG C of reaction temperature, 3~4MPa of reaction pressure, hydrogen to oil volume ratio be 1000:1~ 1500:1,0.5~2.0h of volume space velocity-1；For product after reaction after gas-liquid separator gas-liquid separation, liquid phase enters grease point Water phase is separated from device, oil-phase product enters rectifying column vacuum distillation, and overhead collection C15~C24 natural plants wax, tower reactor is given birth on a small quantity Object diesel oil is unified to be recycled.
Auxiliary agent II alkali metal soln in described (1) step is one of sodium carbonate liquor or solution of potassium carbonate.
Vulcanizing agent in described (2) step is one of carbon disulfide or dimethyl disulfide.
Using gas-chromatography to product carry out analysis biodiesel conversion rate and C15~C24 natural plants wax Rate.
The present invention is entered biodiesel with hydrogen using the method for long-chain natural plants wax in production of biodiesel simultaneously It is mounted with the fixed bed hydrogenation deoxidation reactor of catalyst, is saturated unsaturated double-bond in biodiesel, removes the oxygen in raw material, it can Colorless and transparent natural liquid vegetable wax is obtained, a kind of main component is the crystallizable white of low temperature of C15~C24 n-alkane Solid state wax.The wax can be used as the raw material of chlorinated paraffin, on the one hand solves chlorinated paraffin from raw material sources and contains short chain chlorination On the other hand the environmental issue that paraffin causes persistent organism to pollute is prepared using the biodiesel that waste animal and plant fat is got Natural plants wax is renewable resource, not only solves oil shortage problem, has even more widened the application range of biodiesel, mentioned The high added value of biodiesel.In addition, the present invention has, reaction process is simple, catalyst life is long, at low cost, target product High income and the pure advantage of quality.
In short, the present invention had both improved the benefit of biodiesel using the method for long-chain natural plants wax in production of biodiesel With value, and solves from raw material the pollution problem that chlorinated paraffin currently on the market contains short carbon chain, technical characterstic and beneficial Effect is summarized as follows:
1, the added value of biodiesel is improved.
2, the natural plants wax prepared is mainly C15~C24 n-alkane, carbon chain length and carbochain narrowly distributing, product are pure.
3, it is prepared for non-noble metal supported catalyst, the catalyst preparation is simple, and at low cost, hydrogenation deoxidation effect is bright Aobvious, stable in catalytic performance, catalyst life is long, and biodiesel conversion rate reaches 99.99%, no isocracking, vegetable wax yield It is high.
4, the hydrogenation deoxidation simple process used, hydrogenation deoxidation are completed at the same time, and low energy consumption.
Detailed description of the invention
Fig. 1 is process flow diagram of the present invention using the method for long-chain natural plants wax in production of biodiesel.For For the sake of concise clear, capital equipment and process flow are only provided in figure, and pump, valve, instrument and automatically controlled etc. is omitted.
Appended drawing reference: biodiesel preheater E1, fluidized bed or fixed bed catalytic reactor R1, gas-liquid separator E2, oil Separator V1, rectifying column T1.
Specific embodiment
Long-chain natural plants wax in production of biodiesel is utilized to the present invention with reference to the accompanying drawings and detailed description Method is described in further detail.
The present invention is original with C16~C24 fatty acid methyl ester using the method for long-chain natural plants wax in production of biodiesel Material, the natural plants wax of C15~C24 is prepared by the method for Industrial Catalysis.
Shown in Fig. 1, biodiesel is preheated to 40~50 DEG C in preheater E1, being passed through to be mounted in simultaneously with hydrogen has catalyst Fluidized bed or fixed bed reactors R1,300~330 DEG C of reaction temperature, 3~4MPa of reaction pressure, hydrogen to oil volume ratio 1000: 1~1500:1,0.5~2.0h of liquid hourly space velocity (LHSV)-1, for the product after reaction by gas-liquid separator E2 gas-liquid separation, liquid phase enters oil Separator V1 separates water phase, and oil-phase product enters rectifying column T1 and is evaporated under reduced pressure, overhead collection C15~C24 vegetable wax, and tower reactor is few Measure the unified recycling of biodiesel.
Analysis biodiesel conversion rate is carried out to product using gas-chromatography, the yield of long-chain vegetable wax in C15~C24.
Three specific embodiments are exemplified below operating procedure of the invention is further elaborated.
Embodiment 1
1, catalyst prepares: first sufficiently dissolving ammonium molybdate and auxiliary agent I citric acid with deionized water, nothing after drying is added 40~60 mesh Al of water3O2Carrier supersaturation absorption 12h, and the excessive adsorption liquid of vacuum drying oven temperature programming concentration (60 DEG C, 4h；80 DEG C, 2h；120 DEG C, 8h), it is dry after catalyst be placed in temperature-programmed calcination in Muffle furnace (room temperature~300 DEG C, 5 DEG C/min, 300 DEG C of holding 2h；300~500 DEG C, 5 DEG C/min, 500 DEG C of holding 4h)；Catalyst after roasting is impregnated in cobalt nitrate, nitric acid 12h in the mixed aqueous solution of nickel and auxiliary agent II potassium carbonate repeats front after supersaturation absorption and dries calcination steps, obtains Ni-Co- Mo/Al3O2Catalyst.Wherein content of metal is about 16% (oxide meter), metal molar ratio Mo:Co:Ni=5:4:1, auxiliary agent I citric acid mass concentration is 2%, auxiliary agent II potassium carbonate mass concentration 4%.
2, catalyst vulcanization and hydrogenation: the catalyst prepared is directly filled in fixed bed reactors, nitrogen purging After so that reactor is warming up to 190 DEG C, be passed through vulcanizing agent CS2Vulcanize 2h with hydrogen, improves temperature of reactor to 230 DEG C, continue sulphur Change 4h, stops CS2Charging temperature of reactor is improved to 300 DEG C, continues to be passed through hydrogen reducing 4h.Hydrogen flowing quantity 50ml/min, CS2Flow 0.2ml/min.
3, catalytic reaction condition: 320 DEG C of reaction temperature, reaction pressure 3.0MPa, hydrogen to oil volume ratio 1000:1, volume space velocity 1.0h-1。
4, the biodiesel fuel component and reaction result that the present embodiment uses see the table below.Biodiesel conversion rate 99.99%, base This conversion completely.C15~C24 n-alkane yield 82.54%.
5, successive reaction 720h, catalytic activity do not decline, and conversion ratio is still 99.99%.
Embodiment 2
1, method for preparing catalyst is substantially with case study on implementation 1, the difference is that: metal molar ratio Mo:Co:Ni=4:5: 1, content of metal is 16% (oxide meter), and auxiliary agent II solution of potassium carbonate concentration is 5%.Vulcanization and the same embodiment of hydro-reduction 1。
2, catalytic reaction condition is the same as embodiment 1.
3, the biodiesel fuel component and reaction result that the present embodiment uses see the table below.Biodiesel conversion rate 99.99%, base This conversion completely.C15~C24 n-alkane yield 80.14%.
4, successive reaction 720h, catalytic activity do not decline, and conversion ratio is still 99.99%.
Embodiment 3
1, method for preparing catalyst is substantially with case study on implementation 1, the difference is that: metal molar ratio Mo:Co:Ni=4:4: 2, content of metal is about 16% (oxide meter), and auxiliary agent II solution of potassium carbonate concentration is 5%.Vulcanization and hydro-reduction are the same as implementation Example 1.
2, catalytic reaction condition: 320 DEG C of reaction temperature, reaction pressure 3.0MPa, hydrogen to oil volume ratio 1200:1, volume space velocity 1.2h-1。
3, the biodiesel fuel component and reaction result that the present embodiment uses see the table below.Biodiesel conversion rate 99.99%, base This conversion completely.C15~C24 n-alkane yield 80.03%.
4, successive reaction 720h, catalytic activity do not decline, and conversion ratio is still 99.99%.
Compare three above embodiment and can be seen that the complex art quality of embodiment 1 and prepare best, is most preferably to implement Example.

Claims (3)

1. a kind of method using long-chain natural plants wax in production of biodiesel, it is characterized in that: it is with C16~C24 fatty acid The biodiesel of methyl esters is raw material, and the natural plants wax of C15~C24, concrete operation step are prepared by the method for Industrial Catalysis It is as follows:
(1)Ni-Co-Mo/Al3O2The preparation of catalyst: the first step is abundant using deionized water by ammonium molybdate and auxiliary agent I citric acid Dissolution adds the Al that granularity after drying is 40-60 mesh3O2Carrier carries out supersaturation absorption 12h；Second step uses vacuum drying oven Excessive adsorption liquid is concentrated in temperature programming, and technological parameter is 60 DEG C/4h-, 80 DEG C/2h-, 120 DEG C/8h；After third step is dry To catalyst be placed in Muffle furnace and carry out temperature-programmed calcination again, technological parameter is room temperature~300 DEG C, 5 DEG C/min, 300 DEG C Keep 2h；300~500 DEG C, 5 DEG C/min, 500 DEG C of holding 4h；Catalyst after 4th one-step baking is impregnated in nickel nitrate, nitre again 12h in the mixed aqueous solution of sour cobalt and auxiliary agent II alkali metal soln repeats above-mentioned drying and calcination steps after supersaturation absorption, obtains To Ni-Co-Mo/Al3O2Catalyst；Wherein, metal component content is Ni 10~20%, Co 30~50%, Mo in molar ratio 40~50%, content of metal is calculated as 16~20% according to oxide weight, auxiliary agent I citric acid solution mass concentration 1~3%, Auxiliary agent II alkali metal soln mass concentration 1~5%；
(2) catalyst vulcanization and reduction: by Catalyst packing into fixed bed reactors, 190 DEG C are warming up to after nitrogen purging, together When be passed through hydrogen and vulcanizing agent vulcanization 2h, be warming up to 230 DEG C continue vulcanize 4h, stopping be passed through vulcanizing agent, reactor is warming up to 300 Hydrogen reducing 4h after DEG C；
(3) it catalysis reaction: by biodiesel after preheater is preheated to 40~50 DEG C, then is passed through simultaneously equipped with catalyst with hydrogen Fixed bed reactors, 300~330 DEG C of reaction temperature, 3~4MPa of reaction pressure, hydrogen to oil volume ratio be 1000:1~1500:1, 0.5~2.0h of volume space velocity-1；For product after reaction after gas-liquid separator gas-liquid separation, liquid phase enters oil water separator point From water phase, oil-phase product enters rectifying column vacuum distillation, overhead collection C15~C24 natural plants wax, a small amount of biodiesel of tower reactor Unified recycling.
2. as described in claim 1 using the method for long-chain natural plants wax in production of biodiesel, it is characterized in that: described the (1) the auxiliary agent II alkali metal soln in step is one of sodium carbonate liquor or solution of potassium carbonate.
3. as described in claim 1 using the method for long-chain natural plants wax in production of biodiesel, it is characterized in that: described the (2) vulcanizing agent in step is one of carbon disulfide or dimethyl disulfide.
CN201811081074.7A 2018-09-17 2018-09-17 Utilize the method for long-chain natural plants wax in production of biodiesel Pending CN109126812A (en)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104327878A (en) * 2014-10-11 2015-02-04 肖连朝 N-alkane and preparation method thereof
CN105268449A (en) * 2014-07-18 2016-01-27 中国石油化工股份有限公司 Hydrogenation catalyst and application thereof in hydrodeoxygenation

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105268449A (en) * 2014-07-18 2016-01-27 中国石油化工股份有限公司 Hydrogenation catalyst and application thereof in hydrodeoxygenation
CN104327878A (en) * 2014-10-11 2015-02-04 肖连朝 N-alkane and preparation method thereof

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Application publication date: 20190104