CN105925381A - High value utilization method of gutter oil - Google Patents

High value utilization method of gutter oil Download PDF

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Publication number
CN105925381A
CN105925381A CN201610230559.2A CN201610230559A CN105925381A CN 105925381 A CN105925381 A CN 105925381A CN 201610230559 A CN201610230559 A CN 201610230559A CN 105925381 A CN105925381 A CN 105925381A
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China
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oil
raw
waste
waste oil
catalyst
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吴飞跃
刘炳华
周守勇
徐继明
褚效中
陈莉莉
穆飞虎
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Huaiyin Normal University
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Huaiyin Normal University
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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G3/00Production of liquid hydrocarbon mixtures from oxygen-containing or organic materials, e.g. fatty oils, fatty acids
    • C10G3/42Catalytic treatment
    • C10G3/44Catalytic treatment characterised by the catalyst used
    • C10G3/48Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
    • C10G3/49Catalytic treatment characterised by the catalyst used further characterised by the catalyst support containing crystalline aluminosilicates, e.g. molecular sieves
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00Catalysts comprising molecular sieves
    • CCHEMISTRY; METALLURGY
    • C11ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11BPRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00Refining fats or fatty oils
    • C11B3/001Refining fats or fatty oils by a combination of two or more of the means hereafter
    • CCHEMISTRY; METALLURGY
    • C11ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11BPRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00Refining fats or fatty oils
    • C11B3/008Refining fats or fatty oils by filtration, e.g. including ultra filtration, dialysis
    • CCHEMISTRY; METALLURGY
    • C11ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11BPRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00Refining fats or fatty oils
    • C11B3/10Refining fats or fatty oils by adsorption
    • CCHEMISTRY; METALLURGY
    • C11ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11CFATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10After treatment, characterised by the effect to be obtained
    • B01J2229/18After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1003Waste materials
    • C10G2300/1007Used oils
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20Characteristics of the feedstock or the products
    • C10G2300/30Physical properties of feedstocks or products
    • C10G2300/307Cetane number, cetane index
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2400/00Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02Gasoline
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2400/00Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04Diesel oil
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/10Biofuels, e.g. bio-diesel
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00Technologies relating to oil refining and petrochemical industry
    • Y02P30/20Technologies relating to oil refining and petrochemical industry using bio-feedstock

Abstract

The invention discloses a high value utilization method of gutter oil. The method comprises the following steps: purifying and preprocessing gutter oil, subjecting gutter oil to catalytic cracking, and separating and refining the products. The gutter oil is preprocessed in a clarifying tank, then filtered by a filter, washed by hot water, demulsified, desalted, dehydrated, and purified. Then, gutter oil exchanges heat with reaction products, and is delivered to a reactor to carry out catalytic cracking. The reaction products are separated by a separator, the waste heat is recycled, and fuel diesel oil, gasoline, and light hydrocarbon gas are obtained. The method has the following advantages: (1) the gutter oil is effectively converted into valuable resources such as diesel oil, gasoline, and the like, and the products have the advantages of high thermal efficiency, and low pollution environment; (2) the produced diesel oil has the advantages of good color value, high calorific value, low condensation point, and high flash point and meets related national and industrial standards; (3) the yield of liquid oil is high, the coking degree is low during the cracking process, the whole technology is compact, the efficiency is high, and the method can be applied to industry easily.

Description

Waste oil higher value application method
Technical field
The present invention relates to the discarded high-valued comprehensive utilization of waste oil, fuel oil processing and environmental technology field, particularly relate to a kind of abandoned oil lipid new technology through catalystic pyrolysis processing fuel oil.
Background technology
Waste oil is waste animal and vegetable oil, swill oil, the most repeatedly heating use and the general name of food and drink sewer waste oil.Wherein, discarded plant oils and fats is the main source of waste oil and composition.Adding up according to middle business's information network, the annual catering trade in domestic city produces waste oil and is up to 4,500,000 tons.Owing to waste oil is the edible oil and fat of heavy contamination, the materials such as a series of atmosphere pollution, the aldehyde of adverse condition, acid can be discharged through complicated biochemical reaction in water body;If waste oil flows back to dining table society and food safety will be caused the biggest harm through simple processing.
Along with fossil fuel reserves minimizing day by day withNationalThe economic development quick increase to energy resources demand, the making full use of of resource of the exploitation sum of emerging resource is more paid attention to by people.Therefore, it is necessary to realize the waste oil recycling huge to yield, realize reducing environmental pollution, it is to avoid infringement health simultaneously, and bring considerable economic benefit and good social benefit.
The main chemical compositions of waste oil is higher fatty acid fat, the ultimate principle of its comprehensive utilization is to be broken down into higher fatty acids and glycerol at present, then becomes biodiesel, glycerol, industrial oleic acid, stearic acid and commercial grease, non-phosphide detergent and coal slime collecting agent etc. through deep processing.Wherein, waste oil preparing biological diesel oil carry out is a main path of its recycling, and research is the most, most widely used.But, to many based on ester-interchange method during the waste oil recycling including discarded plant oils and fats, the glycerol in " waste oil " sweet three esters is replaced by low-carbon alcohols (such as methanol), one sweet three ester molecule becomes three long-chain fatty acid methyl ester, reduce molecular weight, improve mobility, make biodiesel.Comparatively speaking, remove impurity, purification and ester-exchange reaction are complex, and cost is the highest, the biodiesel obtained compared with petrifaction diesel, equal some gap in calorific value, viscosity, corrosivity.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, the invention provides oneWaste oil higher value application method, the process fuel oil yield of the method is high, and product property is good, technical process is compact, efficient, environmental protection, low energy consumption and can be continuously produced.
The adopted technical solution is that: the method includes purification pretreatment, the catalytic pyrolysis of waste oil and the separation and purification of product of raw material waste oil;Raw material waste oil is stood by depositing reservoir and filter removes suspended solid impurities, and soluble inorganic salt and organic salt, breakdown of emulsion desalting and dewatering are dissolved in hot wash;It is mixed into catalytic cracking reaction device with circulation heavy oil again after heat exchange;Pyrolysis product enters profit decant separator to carry out separating and Waste Heat Recovery, obtains light hydrocarbon gas, gasoline and diesel product.
Wherein, the specifically comprising the following steps that of said method
[1] waste oil of collection is placed in settling tank V-1 standing, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 80-90 DEG C of hot water and carry out mixing, washing, dissolves solubility salt, alcohols and acid in oil product;
[4] after mixing with hot water, oil product enters progressive intensification 85-95 DEG C of raw material/diesel oil heat exchanger E-1, improves washing solute effect;
[5] raw oil/demulsifier blender M-2 is entered from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject demulsifier, mixing oil product enters oil water separator V-2, container bottom discharges brine waste, and oil product reacted feed pump P-2 is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after extracting out;
[6] raw oil enters catalytic cracking reaction device R-1, controls reaction condition and catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas is discharged at top;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1.
Wherein, raw material waste oil derives from the waste grease of food and drink, and Main Ingredients and Appearance is higher fatty acid ester, including saturated and undersaturated higher fatty acid ester, the most saturated and undersaturated higher fatty acids, lower fatty acid, aldehyde, alcohol and ketone.
Wherein, raw material waste oil carries out clarifying, filtering and removing suspended solid impurities, hot wash is heated to 85 ~ 95 DEG C and overwhelming majority salt and solubility alcohol, acid, aldehyde is dissolved and form water in oil type emulsion, add AE type or AR type demulsifier, enter oil water separator removing salinity and moisture, this oil water separator also include using liquid-liquid decant, adsorb, the centrifugal or equipment of additional high-pressure electric field.
Wherein, desalination, the adsorbent of dehydration are a kind of in large pore molecular sieve, activated carbon, active hargil, the high temperature modified attapulgite of acid activation or their mixture;Wherein, during absorption, the liquid volume air speed of waste oil is 2 ~ 5 h- 1
Wherein, catalytic cracking reaction device is made up of preheating section and conversion zone;Preheating section is preheated to 300 ~ 400 DEG C, then introduces cracking reaction bed, at 450 ~ 600 DEG C, 0 ~ 0.3MPa, weight space velocity 10 ~ 50h- 1Generation catalytic cracking reaction is contacted with catalyst;Reaction bed is the tube furnace reactor of prepackage catalyst, or gasoline stock, or fluidized-bed reactor or moving-burden bed reactor.
Wherein, in terms of the gross weight of catalyst, described catalyst contains 20 ~ 60% molecular sieves, 20 ~ 40% aluminium oxidies, 20 ~ 40% attapulgites;Wherein, described molecular sieve is that molecular sieve commonly used by A type, X-type, Y type and modenite;Described attapulgite is light rare earth, Re=La, Ce, Pr, Nd, Sm, Eu, Gd, and it is 2 ~ 6% that rare-earth usage accounts for molecular sieve total amount ratio.
Wherein, the concrete preparation process of described catalyst is as follows:
(1) rare earth material of 50 g is weighed, the oxalates of Re=La, Ce, Pr, Nd, Sm, Eu, Gd rare earth metal or nitrate, pasty state is become after adding 100 g water stirring and dissolving, it is added dropwise over the concentrated nitric acid of mass fraction 65% until dissolving completely in stirring simultaneously, add 5 g citric acid solid powder to dissolve, become colloidal sol at 70 ~ 90 DEG C of slow evaporations;
(2) accounting for molecular sieve gross weight ratio by rare-earth usage is 2 ~ 6% to weigh molecular sieve and add in colloidal sol, stirs, becomes gel after drying, is warming up to 550-650 DEG C of roastings, obtains rare-earth modified molecular-sieve;
(3) sodium hexameta phosphate aqueous dispersant 100 ml of 1.0%~1.2% mass concentration, solid-to-liquid ratio 1:(15-30 are prepared) add commercially available attapulgite, high-speed stirred 0.5 h, then stand 1-2 h, solid-liquid suspension is separated to obtain attapulgite after aquation;
(4) preparation mass concentration is sulphuric acid, nitric acid, hydrochloric acid, phosphoric acid or oxalic acid solution 50 ml of 4% ~ 10%, add attapulgite 20 ml after step (3) gained aquation, stand 4 h after being sufficiently stirred for 20-60 min, be washed with deionized to neutrality, obtain attapulgite modified;
(5) add in the sodium hexameta phosphate aqueous dispersant that 200 ml weight/mass percentage composition are 1.0%~1.2% concentration by 20 ~ 60% modified molecular screens, 20 ~ 40% aluminium oxidies, 20 ~ 40% attapulgite modified totally 50 g, it is sufficiently stirred for, slow evaporation, makes diameter 2 ~ 4 mm length 3 ~ 5 mm cylindrical pellet catalyst precarsor with extrinsion pressing;Catalyst precarsor is warming up to 550 ~ 650 DEG C of roasting 1 ~ 2 h the most again, obtains catalyst for cracking.
Wherein, high-temperature split product gas phase enters from separator bottom, declines liquid phase counter current contacting at top, and top gas phase steams, and lateral line withdrawal function fuel diesel fraction, at the bottom of tower, heavy pyrolysis product is through being recycled back into reactor;Wherein, tower top steams line injection weak ammonia.
Wherein, the fuel diesel of separator after lateral line withdrawal function with raw material secondary heat exchange.
The invention have the advantages that
1, the tower top of cracking reactor steams thing and enters oil water separator after circulating water, separator top is discharged and is not coagulated tail gas, it mainly comprises containing substantial amounts of low-carbon alkene, can therefrom extract ethylene, propylene, remaining can be as fuel gas or hydrogen feedstock gas, sour water is discharged in bottom, and fuel gasoline is extracted on liquid phase upper strata out.
2, separator bottom extraction heavy end is oil circulation rear and raw material waste oil is mixed into cracking reactor, improves the conversion ratio of raw material.
3, separator fuel diesel after lateral line withdrawal function with cracking stock secondary heat exchange, send outside after cooling, reduce catalytic cracking reaction device heat demand quantity delivered.
4, the present invention is compared with waste oil traditional esterifications method, and fuel oil liquid phase productivity is high, and character is good, and concise in technology is compact, it is achieved serialization, maximizes and automatically controls, it is easy to carry out industrializing implementation production.
5, catalyst Middle molecule sifter device has good catalytic pyrolysis selectivity, and it significantly improves the yield of light ends oil after rare earth modified, reduces the olefin(e) centent in fuel gasoline, and can improve the ratio of low-carbon alkene in lighter hydrocarbons tail gas;Introduce acid activation in the catalyst attapulgite modified, improve specific activity surface and the acid site density of catalyst, be conducive to improving the conversion per pass of course of reaction;The most also introduce high-temperature inorganic oxide raising and prepare the intensity of catalyst, reduce the disrepair phenomenon during it uses.
6, the catalytic pyrolysis conversion ratio of waste oil is high, and product liquid phase oil product yield is high, and cracking process coking degree is low, and catalyst is long for service life, and discarded plant oils and fats conversion ratio reaches 94%, and liquid phase fuel oil quality yield reaches more than 85%.
7, liquid phase is separated must crack fuel diesel, colour yellowish transparent, calorific value is high, condensation point is low, flash-point is high, meetCountryWith industry relevant criterion, can dissolve each other with arbitrary proportion with No. 0 diesel oil, drippolene octane number is high, and olefin(e) centent is low;Rich in low-carbon alkene in lighter hydrocarbons tail gas, may be recovered utilization.
8, by catalytic pyrolysis mode waste oil converted and be prepared as fuel oil and the lighter hydrocarbons tail gas rich in low-carbon alkene, it is to avoid a large amount of acid-base waste fluids produced because of the use of liquid soda acid in the utilization approaches of waste oil traditional esterifications process problem, beneficially environmental protection.
9, present invention process process has fully reclaimed the used heat of pyrolysis product, by the secondary heat exchange process of fuel diesel Yu waste oil raw material, it is provided that the required heat of waste oil raw material different processing stages, reduces energy consumption, improves total thermal efficiency of technical process.
10, after being processed by the correlation step of this trench oil purification part, in waste oil to catalytic pyrolysis process is easily generated catalyst poisoning, the material composition overwhelming majority of coking is eliminated.
Accompanying drawing explanation
Figure 1Flowage structure for the present invention is illustratedFigure
Figure 2And differential thermal weightless for catalyst sample characterizesFigureSpectrum.
Figure 3It is 510 DEG C of liquid-phase pyrolysis product mass spectraFigure
Detailed description of the invention
Technical scheme is further illustrated below in conjunction with embodiment, but and unrestricted scope involved in the present invention.
Practice ground ditch oil raw material sources are respectively as follows: school lunch service's gutter kitchen waste oil, and food and drink a street frying waste oil, oils and fats factory discards animal oil.
Embodiment 1: prepare catalyst and attapulgite modified
(1) rare earth material of 50 g is weighed, the oxalates of Re=La, Ce, Pr, Nd, Sm, Eu, Gd rare earth metal or nitrate, pasty state is become after 100 g water dissolutioies, it is added dropwise over the concentrated nitric acid of mass fraction 65% until dissolving completely in stirring simultaneously, add 5 g citric acid solid powder to dissolve, become colloidal sol at 70 DEG C of slow evaporations;
(2) accounting for molecular sieve gross weight ratio by rare-earth usage is 2% to weigh molecular sieve and add in colloidal sol, stirs, becomes gel after drying, is warming up to 550 DEG C of roasting 2h, obtains rare-earth modified molecular-sieve;
(3) preparing sodium hexameta phosphate aqueous dispersant 100 ml of 1.0% mass concentration, solid-to-liquid ratio 1:15 adds commercially available attapulgite, high-speed stirred 0.5 h, then stands 1h, is separated by solid-liquid suspension, obtains attapulgite after aquation;
(4) preparation mass concentration is sulfuric acid solution 50 ml of 4%, adds attapulgite 20 ml after step (3) gained aquation, stands 4 h, be washed with deionized to neutrality, obtain attapulgite modified after being sufficiently stirred for 20-min;
(5) add in the sodium hexameta phosphate aqueous dispersant that 200 ml weight/mass percentage composition are 1.0% by 20% modified molecular screen, 40% aluminium oxide, 40% attapulgite modified totally 50 g, it is sufficiently stirred for, slow evaporation, makes diameter 2-4 mm length 3-5 mm cylindrical pellet catalyst precarsor with extrinsion pressing;Catalyst precarsor is warming up to 550 DEG C of roasting 2 h the most again, obtains catalyst for cracking.
Embodiment 2: prepare catalyst and attapulgite modified
(1) rare earth material of 50 g is weighed, the oxalates of Re=La, Ce, Pr, Nd, Sm, Eu, Gd rare earth metal or nitrate, pasty state is become after 100 g water dissolutioies, it is added dropwise over the concentrated nitric acid of mass fraction 65% until dissolving completely in stirring simultaneously, add 5 g citric acid solid powder to dissolve, become colloidal sol at 80 DEG C of slow evaporations;
(2) accounting for molecular sieve gross weight ratio by rare-earth usage is 4% to weigh molecular sieve and add in colloidal sol, stirs, becomes gel after drying, is warming up to 600 DEG C of roasting 2h, obtains rare-earth modified molecular-sieve;
(3) preparing sodium hexameta phosphate aqueous dispersant 100 ml of 1.1% mass concentration, solid-to-liquid ratio 1:22.5 adds commercially available attapulgite, high-speed stirred 0.5 h, then stands 1.5h, is separated by solid-liquid suspension, obtains attapulgite after aquation;
(4) preparation mass concentration is sulphuric acid, nitric acid, hydrochloric acid, phosphoric acid or oxalic acid solution 50 ml of 7%, adds attapulgite 20 ml after step (3) gained aquation, stands 4 h, be washed with deionized to neutrality, obtain attapulgite modified after being sufficiently stirred for 40min;
(5) add in the sodium hexameta phosphate aqueous dispersant that 200 ml weight/mass percentage composition are 1.1% by 40% modified molecular screen, 30% aluminium oxide, 30% attapulgite modified totally 50 g, it is sufficiently stirred for, slow evaporation, makes diameter 2-4 mm length 3-5 mm cylindrical pellet catalyst precarsor with extrinsion pressing;Catalyst precarsor is warming up to 600 DEG C of roasting 1.5h the most again, obtains catalyst for cracking.
Embodiment 3: prepare catalyst and attapulgite modified
(1) rare earth material of 50 g is weighed, the oxalates of Re=La, Ce, Pr, Nd, Sm, Eu, Gd rare earth metal or nitrate, pasty state is become after 100 g water dissolutioies, it is added dropwise over the concentrated nitric acid of mass fraction 65% until dissolving completely in stirring simultaneously, add 5 g citric acid solid powder to dissolve, become colloidal sol at 90 DEG C of slow evaporations;
(2) accounting for molecular sieve gross weight ratio by rare-earth usage is 6% to weigh molecular sieve and add in colloidal sol, stirs, becomes gel after drying, is warming up to 650 DEG C of roasting 2h, obtains rare-earth modified molecular-sieve;
(3) preparing sodium hexameta phosphate aqueous dispersant 100 ml of 1.2% mass concentration, solid-to-liquid ratio 1:30 adds commercially available attapulgite, high-speed stirred 0.5 h, then stands 2 h, is separated by solid-liquid suspension, obtains attapulgite after aquation;
(4) preparation mass concentration is sulphuric acid, nitric acid, hydrochloric acid, phosphoric acid or oxalic acid solution 50 ml of 10%, adds attapulgite 20 ml after step (3) gained aquation, stands 4 h, be washed with deionized to neutrality, obtain attapulgite modified after being sufficiently stirred for 60 min;
(5) add in the sodium hexameta phosphate aqueous dispersant that 200 ml weight/mass percentage composition are 1.2% by 60% modified molecular screen, 20% aluminium oxide, 20% attapulgite modified totally 50 g, it is sufficiently stirred for, slow evaporation, makes diameter 2-4 mm length 3-5 mm cylindrical pellet catalyst precarsor with extrinsion pressing;Catalyst precarsor is warming up to 650 DEG C of roasting 1h the most again, obtains catalyst for cracking.
Embodiment 4: waste oil is processed according to following steps
[1] the kitchen waste oil of collection is placed in settling tank V-1 standing 2 days, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 80 DEG C of hot water and carry out mixing, washing, dissolves solubility salt, alcohols and acid in oil product;
[4] after mixing with hot water, oil product enters raw material/diesel oil heat exchanger E-1 progress and is warming up to 85 DEG C, improves washing solute effect;
[5] raw oil/demulsifier blender M-2 is entered from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject AE type demulsifier, mixing oil product enters oil water separator V-2, container bottom discharges brine waste, and oil product reacted feed pump P-2 is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after extracting out;
[6] raw oil enters catalytic cracking reaction device R-1, uses the catalyst of embodiment 1, and preheating section temperature controls 300 DEG C, reaction bed temperature 450 DEG C, pressure 0.1MPa, weight space velocity 10h- 1, with catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas, propylene 26.7%, positive isobutene. 7.6% in tail gas are discharged in top;Separator extraction fuel gasoline productivity 29%, alkene mass content 28.1%;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1, productivity 59%, product is clear light yellow, its olefin(e) centent 25.7%, proportion 0.882, and cetane index 42(analytical data of mass spectrum calculates), 90% distillation 224 DEG C, condensation point-2 DEG C.
Embodiment 5: waste oil is processed according to following steps
[1] the frying waste oil of collection is placed in settling tank V-1 standing 1 day, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 85 DEG C of hot water and carry out mixing, washing and dissolve solubility salt in oil product, alcohols and acid;
[4] after mixing with hot water, oil product enters the progressive intensification of raw material/diesel oil heat exchanger E-1 90 DEG C, improves washing solute effect;
[5] raw oil/demulsifier blender M-2 is entered from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject AR type demulsifier, mixing oil product enters oily-water seperating equipment V-2, container bottom discharges brine waste, and oil product reacted feed pump P-2 is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after extracting out;
[6] raw oil enters catalytic cracking reaction device R-1, uses the catalyst of embodiment 2, and preheating section temperature controls 350 DEG C, reaction bed temperature 550 DEG C, pressure 0.2MPa, weight space velocity 30 h- 1, with catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas, propylene 29.8%, positive isobutene. 8.6% in tail gas are discharged in top;Knockout tower extraction fuel gasoline productivity 29.5%, alkene mass content 30.5%;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1, productivity 57.3%, product is clear light yellow, its olefin(e) centent 27.4%, proportion 0.897, and cetane index 39(analytical data of mass spectrum calculates), 90% distillation 215 DEG C, condensation point-1 DEG C.
Embodiment 6: waste oil is processed according to following steps
[1] the discarded animal oil collected is placed in settling tank V-1 standing 1 day, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil P-1 pressurizes by waste oil raw material, and injects 90 DEG C of hot water and carry out mixing, washing and dissolve solubility salt in oil product, alcohols and acid;
[4] after mixing with hot water, oil product enters the progressive intensification of raw material/diesel oil heat exchanger E-1, improves washing solute effect;
[5] raw oil/demulsifier blender M-2 is entered from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject AE type demulsifier, mixing oil product enters oily-water seperating equipment V-2, container bottom discharges brine waste, and oil product reacted feed pump P-2 is sent to raw oil/circulation heavy oil M-3 and mixes with circulation heavy oil after extracting out;
[6] raw oil enters catalytic cracking reaction device R-1, uses the catalyst of embodiment 3, and preheating section temperature controls 400 DEG C, reaction bed temperature 600 DEG C, pressure 0.3MPa, weight space velocity 50h- 1, with self-control catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas, propylene 13.1%, positive isobutene. 5.4% in tail gas are discharged in top;Knockout tower extraction fuel gasoline productivity 26%, alkene mass content 25.3%;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1, productivity 56%, product is clear light yellow, its olefin(e) centent 25.3%, proportion 0.901, and cetane index 41(analytical data of mass spectrum calculates), 90% distillation 208 DEG C, condensation point-2 DEG C.
Embodiment 7: waste oil is processed according to following steps
[1] the kitchen waste oil of collection is placed in settling tank V-1 standing 1 week, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 90 DEG C of hot water and carry out mixing, washing, dissolves solubility salt, alcohols and acid in oil product;
[4] after mixing with hot water, oil product enters raw material/diesel oil heat exchanger E-1 progress and is warming up to 95 DEG C, improves washing solute effect;
[5] entering raw oil/demulsifier blender M-2 from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject AE type demulsifier, mixing oil product enters oil water separator V-2 adsorbent equipment, and it is 2 h that charging oil product liquid amasss air speed- 1, container bottom is discharged brine waste, is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after oil product reacted feed pump P-2 extraction;
[6] raw oil enters catalytic cracking reaction device R-1, uses the catalyst of embodiment 1, and preheating section temperature controls 300 DEG C, reaction bed temperature 510 DEG C, pressure 0.1MPa, weight space velocity 10 h- 1, with catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas, propylene 29.1%, positive isobutene. 8.7% in tail gas are discharged in top;Separator extraction fuel gasoline productivity 31%, alkene mass content 27.8%;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1, productivity 56%, product is clear light yellow, its olefin(e) centent 25.7%, proportion 0.895, and cetane index 38(analytical data of mass spectrum calculates), 90% distillation 226 DEG C, condensation point 0 DEG C.
Embodiment 8: waste oil is processed according to following steps
[1] the kitchen waste oil of collection is placed in settling tank V-1 standing 2 days, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 85 DEG C of hot water and carry out mixing, washing, dissolves solubility salt, alcohols and acid in oil product;
[4] after mixing with hot water, oil product enters raw material/diesel oil heat exchanger E-1 progress and is warming up to 90 DEG C, improves washing solute effect;
[5] entering raw oil/demulsifier blender M-2 from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject AR type demulsifier, mixing oil product enters oil water separator V-2 adsorbent equipment, and it is 5 h that charging oil product liquid amasss air speed- 1, container bottom is discharged brine waste, is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after oil product reacted feed pump P-2 extraction;
[6] raw oil enters catalytic cracking reaction device R-1, uses the catalyst of embodiment 3, and preheating section temperature controls 300 DEG C, reaction bed temperature 510 DEG C, pressure 0.2MPa, weight space velocity 10 h- 1, with catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas, propylene 27.2%, positive isobutene. 5.9% in tail gas are discharged in top;Separator extraction fuel gasoline productivity 29%, alkene mass content 26.9%;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1, productivity 59%, product is clear light yellow, its olefin(e) centent 28.4%, proportion 0.875, and cetane index 40(analytical data of mass spectrum calculates), 90% distillation 219 DEG C, condensation point-1 DEG C.
Embodiment 9: waste oil is processed according to following steps
[1] the kitchen waste oil of collection is placed in settling tank V-1 standing 1 day, removes top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 85 DEG C of hot water and carry out mixing, washing, dissolves solubility salt, alcohols and acid in oil product;
[4] after mixing with hot water, oil product enters raw material/diesel oil heat exchanger E-1 progress and is warming up to 90 DEG C, improves washing solute effect;
[5] entering raw oil/demulsifier blender M-2 from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject AE type demulsifier, mixing oil product enters adsorbent equipment in oil water separator V-2, and it is 3.5 h that charging oil product liquid amasss air speed- 1, container bottom is discharged brine waste, is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after oil product reacted feed pump P-2 extraction;
[6] raw oil enters catalytic cracking reaction device R-1, uses the catalyst of embodiment 2, and preheating section temperature controls 300 DEG C, reaction bed temperature 450 DEG C, pressure 0.3MPa, weight space velocity 10 h- 1, with catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas, propylene 23.5%, positive isobutene. 6.2% in tail gas are discharged in top;Separator extraction fuel gasoline productivity 27%, alkene mass content 29.3%;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1, productivity 57%, product is clear light yellow, its olefin(e) centent 27.6%, proportion 0.883, and cetane index 37(analytical data of mass spectrum calculates), 90% distillation 219 DEG C, condensation point-2 DEG C.

Claims (10)

1.Waste oil higher value application method, it is characterised in that: the method includes purification pretreatment, the catalytic pyrolysis of waste oil and the separation and purification of product of raw material waste oil;Raw material waste oil is stood by depositing reservoir and filter removes suspended solid impurities, and soluble inorganic salt and organic salt, breakdown of emulsion desalting and dewatering are dissolved in hot wash;It is mixed into catalytic cracking reaction device with circulation heavy oil again after heat exchange;Pyrolysis product enters profit decant separator to carry out separating and Waste Heat Recovery, obtains light hydrocarbon gas, gasoline and diesel product.
2.According to claim 1 Described waste oil higher value application method, it is characterised in that specifically comprising the following steps that of the method
[1] waste oil of collection is placed in settling tank V-1 stands 24 more than h, remove top layer float, and discharge pot bottom connate water;
[2] extract oil phase out remove solid impurity in oil product further through filter F-1 and be easily generated the material such as colloid of deposition;
[3] raw oil/hot water mixer M-1 sent into again after raw oil pump P-1 pressurizes by waste oil raw material, and injects 80 ~ 90 DEG C of hot water and carry out mixing, washing, dissolves solubility salt, alcohols and acid in oil product;
[4] after mixing with hot water, oil product enters raw material/diesel oil heat exchanger E-1 and further heats up 85 ~ 95 DEG C, improves washing solute effect;
[5] raw oil/demulsifier blender M-2 is entered from raw material/diesel oil heat exchanger E-1 out raw material oil product, and inject demulsifier, mixing oil product enters oil water separator V-2, container bottom discharges brine waste, and oil product reacted feed pump P-2 is sent to raw oil/circulation heavy oil blender M-3 and mixes with circulation heavy oil after extracting out;
[6] raw oil enters catalytic cracking reaction device R-1, controls reaction condition and catalyst haptoreaction;
[7] pyrolysis product entrance knockout tower T-1 carries out product separation, and top gaseous phase steams line and injects weak ammonia, then enters profit decant separator V-3, separator bottom effluent sewerage after water recirculator E-2 cools down;Cracking tail gas is discharged at top;Lateral line withdrawal function fuel diesel in the middle part of knockout tower T-1.
3.According to claim 2 Described waste oil higher value application method, it is characterised in that: raw material waste oil derives from the waste grease of food and drink, and Main Ingredients and Appearance is higher fatty acid ester, including saturated and undersaturated higher fatty acid ester, the most saturated and undersaturated higher fatty acids, lower fatty acid, aldehyde, alcohol and ketone.
4.According to claim 2 Described waste oil higher value application methodIt is characterized in that: raw material waste oil carries out clarifying, filtering and removing suspended solid impurities, hot wash is heated to 85 ~ 95 DEG C and overwhelming majority salt and solubility alcohol, acid, aldehyde is dissolved and form water in oil type emulsion, add AE type or AR type demulsifier, enter oil water separator removing salinity and moisture, this oil water separator also include using liquid-liquid decant, adsorb, the centrifugal or equipment of additional high-pressure electric field.
5.According to claim 1 With 4 Described waste oil higher value application method, it is characterised in that: the adsorbent that desalination, dehydration use is a kind of in large pore molecular sieve, activated carbon, active hargil, the high temperature modified attapulgite of acid activation or their mixture;Wherein, the feeding liquid volume space velocity during absorption of raw material waste oil is 2 ~ 5 h-1
6.According to claim 2 Described waste oil higher value application method, it is characterised in that: catalytic cracking reaction device is made up of preheating section and conversion zone;Preheating section is preheated to 300 ~ 400 DEG C, then introduces cracking reaction bed, at 450 ~ 600 DEG C, 0.1 ~ 0.3MPa, weight space velocity 10 ~ 50h-1Generation catalytic cracking reaction is contacted with catalyst;Reaction bed is the tube furnace reactor of prepackage catalyst, or gasoline stock, or fluidized-bed reactor or moving-burden bed reactor.
7.According to claim 6 Described waste oil higher value application method, it is characterised in that: in terms of the gross weight of catalyst, described catalyst contains 20 ~ 60% molecular sieves, 20 ~ 40% inorganic oxides, 20 ~ 40% attapulgite modified;Wherein, described molecular sieve is that molecular sieve commonly used by A type, X-type, Y type and modenite;Described attapulgite modified in altered contents be light rare earth, Re=La, Ce, Pr, Nd, Sm, Eu, Gd, it is 2 ~ 6% that modified RE consumption accounts for molecular sieve total amount ratio.
8.According to claim 6 Described waste oil higher value application method, it is characterised in that the concrete preparation process of described catalyst is as follows:
(1) rare earth material of 50 g is weighed, the oxalates of Re=La, Ce, Pr, Nd, Sm, Eu, Gd rare earth metal or nitrate, pasty state is become after 100 g water dissolutioies, it is added dropwise over the concentrated nitric acid of mass fraction 65% until dissolving completely in stirring simultaneously, add 5 g citric acid solid powder to dissolve, become colloidal sol at 70 ~ 90 DEG C of slow evaporations;
(2) accounting for molecular sieve gross weight ratio by rare-earth usage is 2 ~ 6% to weigh molecular sieve and add in colloidal sol, stirs, becomes gel after drying, it is warming up to 550- 650 DEG C of roasting 2h, obtain rare-earth modified molecular-sieve;
(3) sodium hexameta phosphate aqueous dispersant 100 ml of 1.0%~1.2% mass concentration, solid-to-liquid ratio 1:(15-30 are prepared) add commercially available attapulgite, high-speed stirred 0.5 h, then stand 1-2 h, solid-liquid suspension is separated, obtains attapulgite after aquation;
(4) preparation mass concentration is sulphuric acid, nitric acid, hydrochloric acid, phosphoric acid or oxalic acid solution 50 ml of 4% ~ 10%, add attapulgite 20 ml after step (3) gained aquation, stand 4 h after being sufficiently stirred for 20-60 min, be washed with deionized to neutrality, obtain attapulgite modified;
(5) add in the sodium hexameta phosphate aqueous dispersant that 200 ml weight/mass percentage composition are 1.0%~1.2% by 20 ~ 60% modified molecular screens, 20 ~ 40% aluminium oxidies, 20 ~ 40% attapulgite modified totally 50 g, it is sufficiently stirred for, slow evaporation, makes diameter 2-4 mm length 3-5 mm cylindrical pellet catalyst precarsor with extrinsion pressing;Catalyst precarsor is warming up to 550-650 DEG C of roasting 1-2 h the most again, obtains catalyst for cracking.
9.According to claim 2 Described waste oil higher value application method, it is characterised in that: high-temperature split product gas phase enters from separator bottom, declines liquid phase counter current contacting at top, and top gas phase steams, and lateral line withdrawal function fuel diesel fraction, at the bottom of tower, heavy pyrolysis product is through being recycled back into reactor;Wherein, tower top steams line injection weak ammonia.
10.According to claim 2 Described waste oil higher value application method, it is characterised in that: the fuel diesel of separator after lateral line withdrawal function with raw material secondary heat exchange.
CN201610230559.2A 2016-04-14 2016-04-14 High value utilization method of gutter oil Pending CN105925381A (en)

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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107364830A (en) * 2017-07-03 2017-11-21 华中师范大学 A kind of method of life waste oil catalytic pyrolysis and conversion reformation hydrogen production
CN108018063A (en) * 2016-11-04 2018-05-11 湖南省林业科学院 A kind of method that bio-based hydrocarbon-rich fuel is prepared using vegetable fat
CN108927290A (en) * 2017-12-19 2018-12-04 辽宁德巴斯实业有限公司 Coal separation collecting agent and preparation method thereof
CN108970810A (en) * 2018-08-07 2018-12-11 安徽理工大学 The method and device of coal slime flotation collector is produced in a kind of gutter oil pyrolysis
CN109439360A (en) * 2018-09-27 2019-03-08 昆明理工大学 A kind of natural pelelith catalysis gutter oil prepares the device and method of biologically based fuels
CN110314767A (en) * 2019-08-13 2019-10-11 中国矿业大学 A kind of low order/oxidized coal slime floating agent and application method
CN110437872A (en) * 2019-09-03 2019-11-12 四川润和催化新材料股份有限公司 A method of improving oil quality using bio oil catalytic cracking and improves yield of light olefins
CN110479743A (en) * 2019-09-07 2019-11-22 山东农业大学 The energy-saving processing method that a kind of kitchen garbage desalination, de-oiling rouge substep recycle
CN111548860A (en) * 2020-05-14 2020-08-18 广东锦坤实业有限公司 Process method for producing oleic acid by using plant waste oil
WO2020178597A1 (en) * 2019-03-07 2020-09-10 Oxford Sustainable Fuels Limited Process for upgrading a pyrolysis oil

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102504866A (en) * 2011-11-08 2012-06-20 海南临高化工实业有限公司 Method for preparing biodiesel by mixing waste edible oil with mineral diesel oil and hydrogenization
CN102585896A (en) * 2012-03-13 2012-07-18 杭州绿洲能源科技有限公司 Automatic continuous production process for producing diesel oil with waste oil through catalytic cracking method
CN102604663A (en) * 2012-03-23 2012-07-25 海南朗洁新能源科技有限公司 Method for directly producing high-cetane-number diesel oil by using illegal cooking oil
CN202610189U (en) * 2012-03-13 2012-12-19 杭州绿洲能源科技有限公司 Automatic continuous production equipment for regenerated diesel oil from waste oil through catalytic cracking
CN103013554A (en) * 2012-12-18 2013-04-03 青岛福瑞斯生物能源科技开发有限公司 Device and method for producing biodiesel with illegal cooking oil and waste engine oil
CN103756794A (en) * 2014-01-15 2014-04-30 淮北师范大学 Method for producing second-generation biodiesel by hydrogenation production of illegal cooking oil

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102504866A (en) * 2011-11-08 2012-06-20 海南临高化工实业有限公司 Method for preparing biodiesel by mixing waste edible oil with mineral diesel oil and hydrogenization
CN102585896A (en) * 2012-03-13 2012-07-18 杭州绿洲能源科技有限公司 Automatic continuous production process for producing diesel oil with waste oil through catalytic cracking method
CN202610189U (en) * 2012-03-13 2012-12-19 杭州绿洲能源科技有限公司 Automatic continuous production equipment for regenerated diesel oil from waste oil through catalytic cracking
CN102604663A (en) * 2012-03-23 2012-07-25 海南朗洁新能源科技有限公司 Method for directly producing high-cetane-number diesel oil by using illegal cooking oil
CN103013554A (en) * 2012-12-18 2013-04-03 青岛福瑞斯生物能源科技开发有限公司 Device and method for producing biodiesel with illegal cooking oil and waste engine oil
CN103756794A (en) * 2014-01-15 2014-04-30 淮北师范大学 Method for producing second-generation biodiesel by hydrogenation production of illegal cooking oil

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
孙云: ""废食用油脂催化裂解制备燃料油的研究"", 《中国优秀硕士学位论文全文数据库 工程科技I辑》 *

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108018063A (en) * 2016-11-04 2018-05-11 湖南省林业科学院 A kind of method that bio-based hydrocarbon-rich fuel is prepared using vegetable fat
CN107364830A (en) * 2017-07-03 2017-11-21 华中师范大学 A kind of method of life waste oil catalytic pyrolysis and conversion reformation hydrogen production
CN108927290A (en) * 2017-12-19 2018-12-04 辽宁德巴斯实业有限公司 Coal separation collecting agent and preparation method thereof
CN108970810A (en) * 2018-08-07 2018-12-11 安徽理工大学 The method and device of coal slime flotation collector is produced in a kind of gutter oil pyrolysis
CN109439360A (en) * 2018-09-27 2019-03-08 昆明理工大学 A kind of natural pelelith catalysis gutter oil prepares the device and method of biologically based fuels
CN109439360B (en) * 2018-09-27 2021-05-14 昆明理工大学 Device and method for preparing bio-based fuel by catalyzing gutter oil with natural volcanic rocks
WO2020178597A1 (en) * 2019-03-07 2020-09-10 Oxford Sustainable Fuels Limited Process for upgrading a pyrolysis oil
CN110314767A (en) * 2019-08-13 2019-10-11 中国矿业大学 A kind of low order/oxidized coal slime floating agent and application method
CN110437872A (en) * 2019-09-03 2019-11-12 四川润和催化新材料股份有限公司 A method of improving oil quality using bio oil catalytic cracking and improves yield of light olefins
CN110479743A (en) * 2019-09-07 2019-11-22 山东农业大学 The energy-saving processing method that a kind of kitchen garbage desalination, de-oiling rouge substep recycle
CN111548860A (en) * 2020-05-14 2020-08-18 广东锦坤实业有限公司 Process method for producing oleic acid by using plant waste oil

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Application publication date: 20160907