CN103130599A - Method for producing low-carbon olefin from animal and plant oil and waste animal and plant oil - Google Patents
Method for producing low-carbon olefin from animal and plant oil and waste animal and plant oil Download PDFInfo
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- CN103130599A CN103130599A CN2011103774975A CN201110377497A CN103130599A CN 103130599 A CN103130599 A CN 103130599A CN 2011103774975 A CN2011103774975 A CN 2011103774975A CN 201110377497 A CN201110377497 A CN 201110377497A CN 103130599 A CN103130599 A CN 103130599A
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Abstract
The invention discloses a method for producing a low-carbon olefin from animal and plant oil and waste animal and plant oil. The method comprises that animal and plant oil and waste animal and plant oil are subjected to hydrolysis, hydrodeoxygenation and separation and then the products are used as cracking raw materials for production of low-carbon olefins. In the hydrodeoxygenation, a hydrogen-oil ratio is in a range of 50 to 5000; reaction pressure is in a range of 1 to 15MPa; a reaction temperature is in a range of 200 to 500 DEG C; and reaction time is in a range of 0.5 to 8h. The method can remove oxygen and unsaturated bonds in the animal and plant oil and waste animal and plant oil, and realizes preparation of oil products having high n-alkane content. The oil products having high n-alkane content can be used as cracking raw materials so that ethylene and propylene yields at least reach 53% and ethylene, propylene and butadiene yields at least reach above 60%.
Description
Technical field
The present invention relates to chemical field, say further, relate to a kind of method of utilizing animal-plant oil and abendoned oil thereof to produce low-carbon alkene.
Background technology
The low-carbon alkenes such as ethene, propylene, divinyl are the basic materials of Chemical Manufacture, and industrial pyrolysis furnace is the leading production equipment of petrochemical complex, and the economic benefit of olefin production enterprise is had major effect.Because domestic hydrocarbon resources is less, lack the lighter hydrocarbons high-quality cracking stocks such as ethane, propane, the steam crack material of domestic industry pyrolyzer is take refinery's oil product as main at present, mainly comprise petroleum naphtha, hydrogenation tail oil, lighter hydrocarbons and diesel oil etc., its ethene and propene yield are being 37-50% usually, ethene and propylene and divinyl yield scope 41-55%.In recent years along with the ethene production capacity constantly increases, the crude resources of China is in short supply in addition, dependence on foreign countries for oil had reached 54.81% in 2010, made the imbalance between supply and demand of ethylene raw outstanding, thereby how to enlarge the ethylene raw source, improves low-carbon alkene and become particularly important.Cracking stock is all from fossil feedstock, fossil feedstock belongs to Nonrenewable energy resources, how utilizing renewable resources to produce the low-carbon alkenes such as ethene, propylene, divinyl, break away from ethylene unit to the serious dependence of petroleum resources, is also the problem that domestic ethylene industry faces.
Bio-oil, main component are fatty acid triglycercides.Lipid acid wherein mostly is saturated long linear structure, and carbon number and diesel oil distillate approach, and can be used as the substitute of fossil feedstock, is potential ethylene raw.
The raw material that can be used for bio-oil production is extremely abundant, comprises vegetables oil, animal oil and industry and waste cooking oil etc.In China, the woody oleiferous plants aboundresources, in more than 2,140 ten thousand hectares of economic forests, the woody oleiferous plants class is 4,335 ten thousand mu.Can utilize the suitable land afforestations such as deserted mountain, sand ground to set up the oilseed plant of breeding support base more than 30 kinds.In addition, China's rape ultimate production ranks first in the world." middle oil-0361 " rape line that the academy of agricultural sciences cultivates, the seed oleaginousness is up to 54.72%, and per mu yield reaches 180kg, and oil offtake can reach every mu of 98kg.Simultaneously, the crop stalk of 700,000,000 tons also can be converted into 1.17 hundred million tons of oil fuel or 1.67 hundred million tons of oil, considerable number through processing.But the cost of vegetable and animals oils is relatively high, and sewer oil is as waste oil, and the predecessor is the natural animal-plant grease, is mainly derived from the edible oil of frying in shallow oil after stir-fry, through simply heat, dewater, remove slag, the extraction such as precipitation.It is 2,100 ten thousand tons that China consumes edible oil every year, produce waste oil and be about 400～8,000,000 tons, and be the most cheap bio-oil.It through biochemical reaction, produces the repugnant substances such as aldehyde, acid, atmosphere pollution in water body.Consume simultaneously water body oxygen, cause the anoxia asphyxias such as fishes and shrimps, grow insect.The index national regulation head and shoulders above that becomes sour of sewer oil, as enter food chain and taken in for a long time, the health symptom with occurring in various degree even can threaten life security.Thereby for finding the outlet of reasonable utilization, the sewer oil resource has significance on economy, environmental protection, health and food safety.
At present the utilization of bio-oil there are 3 kinds of major ways.The one, the preparation non-phosphide detergent.Use hydrogen peroxide oxidation, be aided with atlapulgite refining with adsorbents and remove coloring matter in sewer oil, then can generate the tensio-active agent alkali soap of glycerine and washing use through saponification.The 2nd, the simple processing such as be hydrolyzed is purified, and isolates various lipid acid, directly as low-grade industrial oleic acid, stearic acid and commercial grease etc.The mode of fat hydrolysis roughly is divided under normal pressure the saponification separation, and acidifying separates these two types with high pressure.The separate mode of mixed fatty acid roughly comprises: freezing milling process, surfactant method, rectification method etc.The 3rd, transesterify preparing biological diesel oil (fatty acid methyl ester).Most techniques are take sewer oil and methyl alcohol as substrate, and they are different is that the catalyzer and the reaction conditions that adopt are different.As sulfuric acid catalysis method, phosphoric acid catalyzed method, dressing enzyme catalysis method, immobilized-lipase, 1-methyl-3-butyl imidazole hydroxide-catalyzed method, solid acid, solid caustic soda two step heterogeneous catalysis methods etc.
But present bio-oil utilizes the industrial chain of technology short, can bring the derived product development wretched insufficiency of abundant profit.Also do not possess the condition that extensive reprocessing utilizes, be mostly fatty acid methyl ester is sold with the increase profit as solvent etc., do not carry out deep processing.Also need to strengthen the research and development to the high downstream Chemicals of added value, improve product competition.Long linear saturated hydrocarbon component in bio-oil is the ethylene raw of high-quality, as is used and will greatly alleviates cracking stock pressure, and can realize producing reusable edible and the CO of the low-carbon alkene resources such as ethene
2Reduction of discharging.But because contain a large amount of oxygen in the bio-oil molecule, as cracking stock, not only olefin yields is low, and can generate a large amount of CO
2, CO, follow-up separation process is caused have a strong impact on.Therefore need exploitation suitable processing route and process matched therewith, to remove oxygen and unsaturated link(age) wherein, obtain high normal paraffin content oil product.
Summary of the invention
For solving problems of the prior art, the invention provides a kind of method of utilizing animal-plant oil and abendoned oil thereof to produce low-carbon alkene, can remove oxygen and unsaturated link(age) in animal-plant oil and abendoned oil thereof, obtain high normal paraffin content oil product.And with the oil product of this high normal paraffin content as cracking stock, can make ethene and propene yield reach at least 53%, ethene, propylene and divinyl yield can reach more than 60% at least.
The purpose of this invention is to provide a kind of method of utilizing animal-plant oil and abendoned oil thereof to produce low-carbon alkene.
Comprise:
To animal-plant oil and abendoned oil thereof be hydrolyzed, hydrogenation deoxidation with separate after produce low-carbon alkene as cracking stock.
Described animal-plant oil and abendoned oil thereof first with after the C6-C16 normal paraffin mixes carry out hydrogenation deoxidation again when hydrolysis obtains lipid acid and carries out hydrogenation deoxidation; Lipid acid is preferably 1 with C6-C16 normal paraffin mixed volume ratio: 1-1: 20;
Described hydrogenation deoxidation catalyst active ingredient comprises cobalt, molybdenum, nickel, palladium, platinum and composition thereof,
Support of the catalyst is selected from oxide compound, mesopore material, carbon-containing carrier and molecular sieve;
The hydrogen-oil ratio of described hydrogenation deoxidation is 50-5000 (vol), and reaction pressure is 1-15Mpa, and temperature of reaction is 200-500 ℃, and the reaction times is 0.5-8h.
Described separation is that liquid phase obtains comprising the hydrocarbon mixture of C5-C28 normal paraffin to the cooling rear gas-liquid separation of hydrogenation deoxidation product; Described cooling temperature is 0-100 ℃.
The hydrocarbon mixture of described C5-C28 normal paraffin is produced low-carbon alkene as cracking stock.
Concrete technical scheme is as follows:
(1) hydrolysis: vegetable and animals oils and abendoned oil are mixed with water carry out hydrolysis reaction, hydrolysate is separated obtaining fatty acid product.
(2) hydrogenation deoxidation: step (1) is obtained fatty acid product first with after the C6-C16 normal paraffin mixes carry out again hydrogenation deoxidation, the product that obtains mainly comprises take the C5-C28 normal paraffin as main hydrocarbon mixture, water, carbon monoxide, carbonic acid gas, wherein mix with the C6-C16 normal paraffin and mainly play dilution, blending ratio can be definite according to practical situation, and in the present invention, preferred blending ratio is 1: 1-1: 20.
(3) separate: step (2) is obtained the hydrogenation deoxidation material process through gas-liquid separation, liquid phase obtains take the C5-C28 normal paraffin as main hydrocarbon mixture;
(4) be that main hydrocarbon mixture is sent into pyrolyzer as cracking stock with the C5-C28 normal paraffin that obtains, produce low-carbon alkene.
Described Vegetable oil lipoprotein comprises vegetable tallow, vegetables oil, vegetable wax etc., and described animal grease comprises Tallow, beef, animal oil, animal wax, fish tallow, fish oil, fish wax etc., and the animals and plants abendoned oil mainly comprises food and drink trench wet goods.
Hydrolysis can be adopted in prior art the common method for hydrolysis of animal-plant oil and abendoned oil thereof, and animal-plant oil and abendoned oil thereof are hydrolyzed to lipid acid, as: subcritical hydrolysis, enzymic hydrolysis, the hydrolysis of saponification acidization.
The lipid acid that obtains generates take the C5-C28 normal paraffin as main hydrocarbon mixture, water, carbon monoxide, carbonic acid gas it by hydrogenation and removing oxygen wherein;
Hydrogenation catalyst can adopt common hydrogenation catalyst in this area, in the present invention, can be preferred, and the activity of hydrocatalyst composition mainly comprises cobalt, molybdenum, nickel, palladium, platinum and composition thereof.Carrier is selected from oxide compound, mesopore material, carbon-containing carrier and structurized support of the catalyst, as Al
2O
3, SiO
2, Cr
2O
3, MgO, TiO
2, gac etc.Catalyzer before use first will be in prevulcanized under hydro condition.
Described hydrogenation catalyst reaction conditions can adopt common hydrogenation conditions in prior art, and in the present invention, preferred hydrogen-oil ratio is 50-5000 (vol), and reaction pressure is 1-15Mpa, and temperature of reaction 200-500 ℃, the reaction times is 0.5-8h.
Described fatty acid ester hydrogenation reaction product obtains take the C5-C28 normal paraffin as main hydrocarbon mixture through separating treatment.Particularly, first to its cooling formation gas-liquid two-phase logistics, liquid phase stream is carried out the standing demix separation obtain take the C5-C28 normal paraffin as main hydrocarbon mixture, cooling temperature is 0-100 ℃.
With passing into respectively in industrial pyrolysis furnace take the C5-C28 normal paraffin as main hydrocarbon mixture that employing treatment process of the present invention obtains, to improve industrial pyrolysis furnace or ethylene unit yield of light olefins.
The present invention obtains take the C5-C28 normal paraffin as main hydrocarbon mixture and lighter hydrocarbons by hydrogenation deoxidation, separating treatment to animal-plant oil and abendoned oil thereof, and normal paraffin is the high quality raw material of producing the low-carbon alkenes such as ethene, propylene, divinyl, above-mentioned raw materials is substituted petroleum naphtha as cracking stock pass into industrial pyrolysis furnace, improve thus the yield of separate unit industrial pyrolysis furnace or ethylene unit low-carbon alkene, can make ethene and propene yield reach at least 53%, ethene, propylene and divinyl yield can reach more than 60% at least.
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
Lard is mixed being hydrolyzed in reactor with water, water oil volume ratio is 5, and temperature of reaction is 270 ℃, and reaction pressure is 10Mpa, and the reaction times is 3h.The transformation efficiency of lard is 91%.
Mixture after hydrolysis passes in standing skimmer, and wherein oil reservoir and water layer carried out standing separation, and the pressure of standing separation is 0.1MPa, room temperature, and the standing separation time is 5 hours, by the separating of oil lipid acid that obtains of water.
To obtain lipid acid mixes according to volume ratio with n-hexadecane at 1: 1, then mixed solution passes into hydrogen and carries out deoxygenation, catalyzer is Pd/C, hydrogen to oil volume ratio is 500, temperature of reaction is 310 ℃, and reaction pressure is 1.9Mpa, reaction times 6h, the transformation efficiency of lipid acid is 62%, and the diesel oil selectivity is 95%.After unreacted fatty acid separation, obtain diesel product (C15-C18 normal paraffin).
The hydrogenation deoxidation product that obtains is down to carries out gas phase and solid-liquid separation under normal temperature and pressure, then solid liquid phase is carried out multi_layer extraction and obtain water, diesel oil, lipid acid, its composition of diesel oil is mainly the normal paraffin of C15-C18, lipid acid reusable edible.
Certain ethylene unit has 6 industrial pyrolysis furnaces, 5 SRT-IV (HS) pyrolyzer wherein, and 1 CBL-III type pyrolyzer is produced 200000 ton/years of ethene per year, and industrial pyrolysis furnace operation particular case sees Table 1, and the petroleum naphtha physical property sees Table 2.
SRT-IV (HS) is the 8-1 configuration boiler tube of U.S. LUMMUS design, adopts 4 large group chargings, has two waste heat boilers.Wherein BA101-BA105 is SRT-IV (HS) pyrolyzer, BA101, BA102 cleavable lighter hydrocarbons or petroleum naphtha, the common cracking light hydrocarbon of BA101, BA102 cracking naphtha, BA103-BA105 cleavable petroleum naphtha.
BA106 is the Cracking furnace made at home (CBL-III) of Sinopec development ﹠ construction, adopts 32 groups of 2-1 configuration boiler tubes, adopts 4 large group chargings, has 4 waste heat boilers.Cracking stock is petroleum naphtha or diesel oil or hydrogenation tail oil.
Table 1 industrial pyrolysis furnace situation
Table 2 petroleum naphtha physical property
The diesel oil that lard processing is obtained passes into the BA106 pyrolyzer to substitute feed naphtha, and the gas oil pyrolysis processing condition are 24.076 tons/hour, and water-oil ratio is that 0.75, COT is 810 ℃, and yield of ethene is 35.72, and propene yield is 18.03, and the divinyl yield is 6.97.
Hence one can see that, after the alternative petroleum naphtha of the diesel oil that BA106 adopts lard to produce, yield of ethene rises to 35.72% by 27.87%, propene yield rises to 18.03 by 17.56, the divinyl yield rises to 6.97% by 5.03, the diene yield rises to 53.75% by 45.43, and the triolefin yield rises to 60.72% by 50.46%, thus yield and the output of the ethene of raising BA106 pyrolyzer, propylene, divinyl, diene, triolefin.
Claims (10)
1. method of utilizing animal-plant oil and abendoned oil thereof to produce low-carbon alkene is characterized in that described method comprises:
To animal-plant oil and abendoned oil thereof be hydrolyzed, hydrogenation deoxidation with separate after produce low-carbon alkene as cracking stock.
2. the method for production low-carbon alkene as claimed in claim 1 is characterized in that:
Described animal-plant oil and abendoned oil thereof first with after the C6-C16 normal paraffin mixes carry out hydrogenation deoxidation again when hydrolysis obtains lipid acid and carries out hydrogenation deoxidation.
3. the method for production low-carbon alkene as claimed in claim 2 is characterized in that:
Described lipid acid is 1 with C6-C16 normal paraffin mixed volume ratio: 1-1: 20.
4. the method for production low-carbon alkene as claimed in claim 2 is characterized in that:
Described hydrogenation deoxidation catalyst active ingredient comprises cobalt, molybdenum, nickel, palladium, platinum and composition thereof,
Support of the catalyst is selected from oxide compound, mesopore material, carbon-containing carrier and molecular sieve.
5. the method for production low-carbon alkene as claimed in claim 4 is characterized in that:
The hydrogen-oil ratio of described hydrogenation deoxidation is 50-5000, and reaction pressure is 1-15Mpa, and temperature of reaction is 200-500 ℃, and the reaction times is 0.5-8h.
6. the method for production low-carbon alkene as claimed in claim 1 is characterized in that:
Described separation is that liquid phase obtains comprising the hydrocarbon mixture of C5-C28 normal paraffin to the cooling rear gas-liquid separation of hydrogenation deoxidation product.
7. the method for production low-carbon alkene as claimed in claim 6 is characterized in that:
Described cooling temperature is 0-100 ℃.
8. the method for production low-carbon alkene as claimed in claim 6 is characterized in that:
The hydrocarbon mixture of described C5-C28 normal paraffin is produced low-carbon alkene as cracking stock.
9. the method for production low-carbon alkene as claimed in claim 5 is characterized in that:
Described separation is that liquid phase obtains comprising the hydrocarbon mixture of C5-C28 normal paraffin to the cooling rear gas-liquid separation of hydrogenation deoxidation product;
Described cooling temperature is 0-100 ℃;
The hydrocarbon mixture of described C5-C28 normal paraffin is produced low-carbon alkene as cracking stock.
10. the method for production low-carbon alkene as described in one of claim 1～9 is characterized in that:
Described Vegetable oil lipoprotein comprises vegetable tallow, vegetables oil, vegetable wax;
Described animal grease comprises Tallow, beef, animal oil, animal wax;
Described abendoned oil comprises the food and drink sewer oil.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104722295A (en) * | 2013-12-20 | 2015-06-24 | 中国科学院大学 | Catalyst for catalysis of biological oil hydrodeoxygenation reaction in water phase or water-oil two phase |
| CN105452431A (en) * | 2013-06-27 | 2016-03-30 | 诺瓦蒙特股份公司 | Process for the selective hydrogenation of vegetable oils |
| CN107163983A (en) * | 2017-06-07 | 2017-09-15 | 常州慧杰电气技术有限公司 | A kind of preparation method of reproducibility diesel fuel |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101342557A (en) * | 2007-07-10 | 2009-01-14 | 上海申驰实业有限公司 | Hydroform mechanism for processing vehicle seat parts |
| CN101778928A (en) * | 2007-06-12 | 2010-07-14 | Ifp公司 | Production of vapour-cracking loads with a high yield of the resulting ethylene, propylene and polymers by hydroprocessing of vegetable oils |
| WO2011012439A1 (en) * | 2009-07-27 | 2011-02-03 | Total Petrochemicals Research Feluy | A process for the production of bio-naphtha from complex mixtures of natural occurring fats & oils |
-
2011
- 2011-11-24 CN CN201110377497.5A patent/CN103130599B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101778928A (en) * | 2007-06-12 | 2010-07-14 | Ifp公司 | Production of vapour-cracking loads with a high yield of the resulting ethylene, propylene and polymers by hydroprocessing of vegetable oils |
| CN101342557A (en) * | 2007-07-10 | 2009-01-14 | 上海申驰实业有限公司 | Hydroform mechanism for processing vehicle seat parts |
| WO2011012439A1 (en) * | 2009-07-27 | 2011-02-03 | Total Petrochemicals Research Feluy | A process for the production of bio-naphtha from complex mixtures of natural occurring fats & oils |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105452431A (en) * | 2013-06-27 | 2016-03-30 | 诺瓦蒙特股份公司 | Process for the selective hydrogenation of vegetable oils |
| CN105452431B (en) * | 2013-06-27 | 2020-04-14 | 诺瓦蒙特股份公司 | Process for the selective hydrogenation of vegetable oils |
| CN104722295A (en) * | 2013-12-20 | 2015-06-24 | 中国科学院大学 | Catalyst for catalysis of biological oil hydrodeoxygenation reaction in water phase or water-oil two phase |
| CN107163983A (en) * | 2017-06-07 | 2017-09-15 | 常州慧杰电气技术有限公司 | A kind of preparation method of reproducibility diesel fuel |
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