CN113604247A - A kind of preparation method of bio-based n-alkane phase change material - Google Patents
A kind of preparation method of bio-based n-alkane phase change material Download PDFInfo
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- CN113604247A CN113604247A CN202110961795.2A CN202110961795A CN113604247A CN 113604247 A CN113604247 A CN 113604247A CN 202110961795 A CN202110961795 A CN 202110961795A CN 113604247 A CN113604247 A CN 113604247A
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- Prior art keywords
- oil
- vegetable oil
- phase change
- fat
- preparation
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- 239000012782 phase change material Substances 0.000 title claims abstract description 32
- 238000002360 preparation method Methods 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 29
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- 235000019198 oils Nutrition 0.000 claims abstract description 26
- 239000002994 raw material Substances 0.000 claims abstract description 20
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
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- 238000004519 manufacturing process Methods 0.000 claims abstract description 12
- 239000002699 waste material Substances 0.000 claims abstract description 12
- 230000002378 acidificating effect Effects 0.000 claims abstract description 11
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- YCOZIPAWZNQLMR-UHFFFAOYSA-N pentadecane Chemical compound CCCCCCCCCCCCCCC YCOZIPAWZNQLMR-UHFFFAOYSA-N 0.000 claims description 26
- NDJKXXJCMXVBJW-UHFFFAOYSA-N heptadecane Chemical compound CCCCCCCCCCCCCCCCC NDJKXXJCMXVBJW-UHFFFAOYSA-N 0.000 claims description 24
- RZJRJXONCZWCBN-UHFFFAOYSA-N octadecane Chemical compound CCCCCCCCCCCCCCCCCC RZJRJXONCZWCBN-UHFFFAOYSA-N 0.000 claims description 22
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 229910017604 nitric acid Inorganic materials 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- SECPZKHBENQXJG-FPLPWBNLSA-N palmitoleic acid Chemical compound CCCCCC\C=C/CCCCCCCC(O)=O SECPZKHBENQXJG-FPLPWBNLSA-N 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000005303 weighing Methods 0.000 description 2
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- 229940043268 2,2,4,4,6,8,8-heptamethylnonane Drugs 0.000 description 1
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 1
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- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 1
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- 239000003463 adsorbent Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- DTOSIQBPPRVQHS-PDBXOOCHSA-N alpha-linolenic acid Chemical compound CC\C=C/C\C=C/C\C=C/CCCCCCCC(O)=O DTOSIQBPPRVQHS-PDBXOOCHSA-N 0.000 description 1
- 235000020661 alpha-linolenic acid Nutrition 0.000 description 1
- AMVQGJHFDJVOOB-UHFFFAOYSA-H aluminium sulfate octadecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.[Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O AMVQGJHFDJVOOB-UHFFFAOYSA-H 0.000 description 1
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- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 1
- KUVMKLCGXIYSNH-UHFFFAOYSA-N isopentadecane Natural products CCCCCCCCCCCCC(C)C KUVMKLCGXIYSNH-UHFFFAOYSA-N 0.000 description 1
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- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 1
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- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
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- 239000002383 tung oil Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
-
- 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
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K5/00—Heat-transfer, heat-exchange or heat-storage materials, e.g. refrigerants; Materials for the production of heat or cold by chemical reactions other than by combustion
- C09K5/02—Materials undergoing a change of physical state when used
- C09K5/06—Materials undergoing a change of physical state when used the change of state being from liquid to solid or vice versa
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
- C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
-
- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Physics & Mathematics (AREA)
- Combustion & Propulsion (AREA)
- Thermal Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本发明公开了一种生物基正构烷烃相变材料的制备方法，将脂肪酸甘油酯在酸性固体催化剂作用下反应，即得正构烷烃。本发明以非食用植物油脂、废弃动植物油脂为原料，其主要成分是C16和C18的长链脂肪酸甘油酯，通过精制过程除杂、加氢脱氧/饱和、精馏等步骤即可生成C15、C16、C17、C18等正构烷烃。与石油蜡和费托合成油蜡为原料的生产方法相比所生产的正构烷烃相变材料几乎不含异构烷烃、环烷烃和芳烃，无需对其再进行深度加氢精制和二次提纯；与其他以生物基原料制备正构烷烃的方法相比，本发明对废弃动植物油脂的预处理无需甲酯化反应过程。本发明采用的原料可再生，生产工艺简单，反应条件温和，产品纯度高且绿色环保。
The invention discloses a preparation method of a bio-based n-paraffin phase change material. The fatty acid glyceride is reacted under the action of an acidic solid catalyst to obtain n-paraffin. The present invention uses non-edible vegetable oil and waste animal and vegetable oil as raw materials, and its main components are C16 and C18 long-chain fatty acid glycerides, which can be generated through the steps of refining process of removing impurities, hydrodeoxygenation/saturation, and rectification. n-alkanes such as C 15 , C 16 , C 17 , and C 18 . Compared with the production method using petroleum wax and Fischer-Tropsch synthetic oil wax as raw materials, the produced n-paraffin phase change material contains almost no isoparaffins, naphthenes and aromatic hydrocarbons, and no further deep hydrorefining and secondary purification are required. Compared with other methods for preparing n-alkanes with bio-based raw materials, the present invention does not need a methyl esterification reaction process for the pretreatment of waste animal and vegetable oils. The raw materials used in the invention are renewable, the production process is simple, the reaction conditions are mild, and the product has high purity and is environmentally friendly.
Description
Technical Field
The invention relates to the technical field of environmental protection and energy conservation, in particular to a preparation method of a bio-based n-alkane phase change material.
Background
The phase-change material has little temperature change in the melting or solidification process, but has great latent heat absorbed or released in a small temperature interval, and the characteristic ensures that the energy-saving effect of the phase-change material in the aspects of constant temperature, energy storage and the like is very obvious. Through development for many years, phase change materials have been widely applied to the fields of solar energy storage, low-price electric energy, aerospace, construction, clothing, refrigeration, military, communication, electric power and the like.
The phase change material mainly comprises a plurality of types such as inorganic hydrated salts, polyesters, hydrocarbons, n-alkyl alcohols, fatty acids/esters and the like. The normal alkane is an ideal phase change material recognized in the industry, has the advantages of high enthalpy value, high purity, high chemical stability and the like, and is non-corrosive and non-environment-polluting. The latent heat of phase change of normal paraffins is greater compared to isoparaffins and cycloparaffins, and the temperature and latent heat of phase change of normal paraffins is related to the length of the carbon chain, for example, the liquid-solid phase transition temperature of n-pentadecane is 10 ℃, the latent heat of phase change is 185KJ/kg, and the liquid-solid phase transition temperature of n-octadecane is 28.2 ℃, and the latent heat value is 240 KJ/kg. Through the blending of the composition of normal alkane molecules, the liquid-solid phase transition temperature of the normal alkane phase transition material can be adjusted, and the temperature belongs to the most common range in daily life of people. In summary, n-alkanes have great advantages for use as phase change materials.
At present, petroleum wax and Fischer-Tropsch synthetic oil wax are important sources of normal paraffin, and raw materials of the normal paraffin are from non-renewable petroleum, natural gas and coal. When the petroleum wax and the Fischer-Tropsch synthetic oil wax are used for producing the normal paraffin phase change material, because the normal paraffin phase change material contains olefin, isoparaffin, cycloparaffin, aromatic hydrocarbon, oxygen-containing, sulfur-containing, nitrogen-containing compounds and other complex components, in order to ensure the ideal phase change interval and latent heat enthalpy value of the normal paraffin phase change material, the impurity removal and purification are required to be carried out through the processing processes of deep hydrofining, rectification, normal-isoparaffin separation and the like, such as the methods described in patents of CN103980940A, CN107523274A, CN108102694A, CN111471487A, CN111471486A and the like, but the production processes of the methods are complex and the process conditions are harsh. A new method for preparing bio-based n-alkane phase change materials is needed to solve these problems.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to solve the technical problems of the prior art, provides a preparation method of a bio-based n-alkane phase change material, and solves the problems of complex production process, harsh process conditions and the like of fossil-based raw materials.
In order to solve the technical problems, the invention discloses a preparation method of a bio-based n-alkane phase change material, which comprises the steps of carrying out hydrodeoxygenation/saturation reaction on fatty glyceride under the action of an acidic solid catalyst, and converting the fatty glyceride into n-alkane.
The fatty glyceride can be obtained by direct purchase, can also be prepared according to other existing technical schemes, and can also be obtained by refining grease serving as a raw material.
Wherein the oil is inedible vegetable oil and/or waste animal and vegetable oil.
Wherein the non-edible vegetable oil is vegetable oil containing harmful substances to human body, such as expired edible vegetable oil, jatropha oil, tung oil, castor oil, catalpa oil, wood oil, etc.
Wherein the waste animal and vegetable oil and fat is any one or mixture of waste animal and vegetable oil and fat generated after frying oil and waste animal and vegetable oil and fat obtained in the meat production process.
Wherein the refining comprises any one or more of degumming, water washing, adsorption and distillation.
Wherein the degumming is degumming by using phosphoric acid and/or clay.
Wherein the amount of the phosphoric acid and/or the carclazyte is 0.1-7 wt% of the grease; preferably, the amount of the phosphoric acid and/or the argil is 0.1-5 wt% of the grease; more preferably, the amount of the phosphoric acid and/or the clay is 0.3-4 wt% of the grease.
Wherein the degumming temperature is 40-90 ℃; preferably, the degumming temperature is 60-70 ℃.
Wherein the degumming time is more than 5 min; preferably, the degumming time is 10-120 min; further preferably, the degumming time is 20-60 min.
Wherein the adsorption is performed by adopting alkaline clay.
Wherein the dosage of the alkaline clay is 0.5-4.5 wt% of the grease; preferably, the dosage of the alkaline clay is 2-3 wt% of the grease.
Wherein the adsorption temperature is 30-70 ℃.
Wherein the adsorption time is 1-3 h.
The acidic solid catalyst is a catalyst which is acidic, porous, high in active metal content and large in specific surface area, has good tolerance to impurities in raw oil, and adopts alumina or amorphous silicon-aluminum as a carrier; preferably, the carrier of the acidic solid catalyst is amorphous silica-alumina.
Wherein the specific surface area of the carrier is 150-250 m2(ii)/g; preferably, the specific surface area of the carrier is 180-220 m2(ii)/g; further preferably, the specific surface area of the carrier is 200-210 m2/g。
Wherein the pore volume of the carrier is 0.1-0.7 cm3(ii)/g; preferably, the pore volume of the carrier is 0.2-0.6 cm3(ii)/g; further preferably, the pore volume of the supportIs 0.4-0.5 cm3/g。
Wherein, the acidic solid catalyst adopts at least two of sulfuration state Ni, sulfuration state Co, sulfuration state Mo and sulfuration state W as hydrogenation active components.
Wherein, the mass content of the active metal is 15-25% in terms of oxidation state, and the balance is the carrier.
Wherein, the reactor of the hydrodeoxygenation/saturation reaction is a fixed bed reactor; the loading of catalyst was 200 mL.
Wherein the conditions of the hydrodeoxygenation/saturation reaction are as follows: the reaction temperature is 300-400 ℃, the hydrogen partial pressure is 3-18 MPa, and the liquid hourly space velocity is 0.5-3.0 h-1The volume ratio of hydrogen to oil is 500-1500 Nm3/m3。
Wherein the normal alkanes include n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane.
Preferably, the fatty glyceride is subjected to hydrodeoxygenation/saturation reaction under the action of an acidic solid catalyst to obtain a mixture of n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane, the mixture is rectified, and the n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane are separated to obtain single-carbon-number monomer n-alkane, wherein the monomer n-alkane belongs to the bio-based n-alkane phase change material.
Wherein the purity of the monomer n-alkane is more than 98 percent, and the iodine value is less than 0.3g/100 g.
Has the advantages that: compared with the prior art, the invention has the following advantages:
(1) the invention provides a preparation method of a bio-based n-alkane phase change material, which takes inedible vegetable oil and waste animal and vegetable oil as raw materials, and the main component of the material is C16And C18The long-chain fatty glyceride is subjected to impurity removal, hydrodeoxygenation/saturation, rectification and other steps in a refining process to generate C15、C16、C17、C18And the like. Compared with the production method using petroleum wax and Fischer-Tropsch synthetic oil wax as raw materials, the produced normal paraffin phase change material almost contains no isoparaffin, cycloparaffin and areneDeep hydrofining and secondary purification are required to be carried out on the crude product; compared with other methods for preparing the n-alkane by using the bio-based raw materials, the method disclosed by the invention does not need a methyl esterification reaction process for the pretreatment of the waste animal and vegetable oil. The raw materials adopted by the invention are renewable, the production process is simple, the reaction conditions are mild, the product purity is high, and the method is green and environment-friendly.
(2) The hydrogenation process adopts a fixed bed reactor, the technology is simple and mature, a one-time process flow is adopted, and raw oil does not need to be diluted.
(3) The hydrogenation reaction in the invention adopts Ni-Mo/amorphous silicon-aluminum type catalyst, which not only realizes hydrodeoxygenation and hydrogenation saturation reaction, but also can control the reaction process to generate a small amount of cracking so as to obtain more C15And C17N-alkane phase change materials.
Drawings
The foregoing and/or other advantages of the invention will become further apparent from the following detailed description of the invention when taken in conjunction with the accompanying drawings.
FIG. 1 is a method for preparing a bio-based n-alkane phase change material according to example 2.
FIG. 2 is a method for preparing a bio-based n-alkane phase change material according to example 3.
Detailed Description
The experimental methods described in the following examples are all conventional methods unless otherwise specified; the reagents and materials are commercially available, unless otherwise specified.
Example 1: preparation of the catalyst
Mixing an aluminum sulfate octadecahydrate aqueous solution with the mass concentration of 50% and a water glass solution with the mass concentration of 50% according to a certain proportion, stirring to prepare a mixed solution, then adding ammonia water to adjust the pH value to be alkaline, aging for 120 minutes, washing and filtering by using deionized water until a washing liquid is neutral, drying an obtained filter cake at 120 ℃, roasting at 550 ℃, crushing and sieving to obtain powder with the granularity of 200 meshes, and detecting that the silicon-aluminum ratio of the prepared amorphous silicon-aluminum is 2.2 and the specific surface area is 201m2Per g, pore volume 0.42cm3/g。
Quantitatively weighing the prepared amorphous silicon-aluminum powder, SB powder, a nitric acid solution with the mass concentration of 10% and sesbania powder according to the mass ratio of 10: 1.3: 0.9: 0.5, extruding and molding, drying at 120 ℃ and roasting at 550 ℃ to obtain the strip-shaped carrier. The prepared carrier was examined to have a lateral pressure strength of 122N/cm.
Taking quantitative ammonium molybdate and nickel nitrate, dissolving with deionized water to prepare Ni-Mo co-immersion liquid, loading Ni and Mo on the amorphous silicon-aluminum strip-shaped carrier by adopting a vacuum immersion method, drying at 120 ℃ and roasting at 550 ℃, and finally obtaining the biodiesel hydrodeoxygenation/saturation catalyst. Through detection, the mass content of NiO in the prepared catalyst is 4.0 percent, and the MoO content is3The mass content of (A) is 18.0%.
Example 2
In the preparation method of the bio-based n-alkane phase change material provided by the embodiment, jatropha curcas oil is used as a raw material, as shown in fig. 1, the preparation method comprises the following steps:
step 201, taking jatropha curcas oil as a raw material, firstly adding argil accounting for 4% of the mass fraction of the jatropha curcas oil into the raw material, and reacting at 70 ℃ for 20 minutes to carry out degumming;
step 202, adding alkaline clay which accounts for 3 percent of the mass of the jatropha curcas oil into the material obtained in step 201, and reacting at 50 ℃ for 120 minutes to obtain refined fatty glyceride with the phospholipid content of 0.18mg/g and the acid value of 0.21mgKOH/g, wherein the composition is shown in Table 1;
step 203, adopting a fixed bed reactor, adopting the Ni-Mo/amorphous silicon-aluminum type hydrogenation catalyst of example 1, wherein the loading amount is 200ml, and under the action of the catalyst, the reaction temperature is 360 ℃, the hydrogen partial pressure is 8MPa, and the liquid hourly volume space velocity is 1.0h-1Hydrogen-oil volume ratio 1000Nm3/m3Under the process conditions of (1), carrying out hydrodeoxygenation/saturation reaction on the refined fatty glyceride to obtain normal alkane;
the yield and properties of the product obtained by the hydrogenation of fatty acid glycerides are shown in table 2;
step 204, distilling the normal alkane by adopting a real boiling point distiller to separate C14And C14The following light component, C15And C15The components are separated into n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane one by adopting a reduced pressure rectification device;
wherein the theoretical plate number of each rectifying tower is 40, each rectifying tower is operated under reduced pressure, the operating pressure is 20KPa, the reflux ratio of each rectifying tower is 5, and the tower top temperature is 206.5 ℃, 224.2 ℃, 236.8 ℃ and 249.4 ℃ respectively; the n-pentadecane, the n-hexadecane, the n-heptadecane and the n-octadecane all belong to single-carbon-number monomer n-alkane; the monomer n-alkane belongs to a bio-based n-alkane phase change material; the purity and properties of the resulting single carbon number monomeric n-alkanes are shown in table 3.
TABLE 1 fatty acid composition in refined fatty acid glycerides
| Fatty acid composition | Example 1,% of | Example 2, b |
| Palmitic acid (16:0) | 14.25 | 11.32 |
| Palmitoleic acid (16:1) | 0.13 | 0.13 |
| Stearic acid (18:0) | 6.41 | 3.58 |
| Oleic acid (18:1) | 41.27 | 33.96 |
| Linoleic acid (18:2) | 34.69 | 43.25 |
| Linolenic acid (18:3) | 0.33 | 4.07 |
| Others | 2.92 | 3.69 |
| Total up to | 100.00 | 100.00 |
TABLE 2 hydrodeoxygenation/saturation reaction product yields and compositions
| Analysis item | Example 1 | Example 2 |
| C4+Yield of normal paraffins,% of | 79.41 | 80.50 |
| C4+N-alkanes groupTo% | ||
| C4～C8 | 1.19 | 1.65 |
| C9～C14 | 3.02 | 2.2 |
| N-pentadecane | 7.27 | 6.16 |
| N-hexadecane | 9.08 | 8.19 |
| Isohexadecane | 0.06 | 0.07 |
| N-heptadecane | 28.8 | 32.49 |
| Isoheptadecane | 0.15 | 0.17 |
| N-octadecane | 47.11 | 44.6 |
| Isooctadecane | 0.78 | 1.01 |
| C19 + | 2.54 | 3.46 |
| Total up to | 100 | 100 |
TABLE 3 purity of n-alkanes and related properties of phase change materials
Example 3
In the preparation method of the bio-based n-alkane phase change material provided by the embodiment, the soybean oil frying oil is used as a raw material, as shown in fig. 2, the preparation method includes the following steps:
301, selecting soybean frying oil as a raw material, firstly adding 85% phosphoric acid into the raw material at 60 ℃, wherein the adding amount is 0.3% of the mass of the raw material, and stirring for 60 minutes; then adding deionized water with the same temperature accounting for 10 percent of the mass fraction of the raw materials, and continuing stirring for 60 minutes;
step 302, adding alkaline clay which accounts for 2 percent of the mass of the soybean frying oil into the material obtained in the step 301 at 90 ℃ to adsorb and remove impurities from an oil phase, then distilling the oil from which the adsorbent is separated at normal pressure to remove free fatty acid in the oil, and finally obtaining 240 DEG C+Fraction (b) ofThe refined fatty glyceride had an acid value of 0.6mgKOH/g and a water content of 0.03% by mass, and had a composition as shown in Table 1:
step 303, adopting a fixed bed reactor, adopting the Ni-Mo/amorphous silicon-aluminum type hydrogenation catalyst described in example 1, wherein the loading amount is 200ml, and the reaction temperature is 360 ℃, the hydrogen partial pressure is 8MPa, and the liquid hourly volume space velocity is 1.0h-1Hydrogen-oil volume ratio 1000Nm3/m3Under the process conditions of (1), carrying out hydrodeoxygenation/saturation reaction on the refined fatty glyceride to obtain normal alkane;
the yield and properties of the product obtained by the hydrogenation of fatty acid glycerides are shown in table 2;
304, distilling the normal alkane by adopting a real boiling point distiller to separate C14And C14The following light component, C15And C15The components are separated into n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane one by adopting a reduced pressure rectification device;
wherein the theoretical plate number of each rectifying tower is 40, each rectifying tower is operated under reduced pressure, the operating pressure is 20KPa, the reflux ratio of each rectifying tower is 5, and the tower top temperature is 206.5 ℃, 224.2 ℃, 236.8 ℃ and 249.4 ℃ respectively; the n-pentadecane, the n-hexadecane, the n-heptadecane and the n-octadecane all belong to single-carbon-number monomer n-alkane, and the monomer n-alkane belongs to bio-based n-alkane phase change materials; the purity and properties of the resulting single carbon number monomeric n-alkanes are shown in table 3.
Comparative example 1:
by changing only the hydrodeoxygenation/saturation catalyst as in example 1, C is obtained15-C18The product distribution is shown in table 4;
the comparative catalyst adopts a Ni-Mo/alumina hydrodeoxygenation/saturation catalyst with weak acidity, and the preparation method comprises the following steps:
quantitatively weighing aluminum oxide, SB powder, a nitric acid solution with the mass concentration of 10% and sesbania powder, wherein the mass ratio of the aluminum oxide to the SB powder to the sesbania powder is 10: 1.0: 0.7: 0.3, extruding the mixture into strips, drying the strips at 120 ℃ and roasting the strips at 550 ℃ to obtain the strip-shaped carrier. The side pressure strength of the prepared alumina carrier is detected to be142N/cm and a specific surface area of 230m2Per g, pore volume 0.63cm3(ii) in terms of/g. Taking quantitative ammonium molybdate and nickel nitrate, dissolving with deionized water to prepare Ni-Mo co-immersion liquid, loading Ni and Mo on the strip alumina carrier by adopting a vacuum immersion method, drying at 120 ℃ and roasting at 550 ℃, and finally obtaining the Ni-Mo/alumina type biodiesel hydrodeoxygenation/saturation catalyst. The detection shows that the NiO content of the prepared catalyst is 4.2 percent, and the MoO content is3The content was 17.5%.
TABLE 4 comparison of carbon number distributions of phase change materials obtained with different hydrogenation catalysts
| Catalyst and process for preparing same | Ni-Mo/amorphous silicon-aluminum | Ni-Mo/alumina |
| C15Yield and content of | 5.77 | 1.34 |
| C16Yield and content of | 7.21 | 12.52 |
| C17Yield and content of | 22.87 | 9.91 |
| C18Yield and content of | 37.41 | 49.69 |
Note: the yield of Ni — Mo/amorphous silica-alumina was equal to the content of C15 to C18 in example 1 (table 2) × 79.41%.
It can be seen that the yield of n-pentadecane and n-heptadecane obtained by the method is higher due to the adoption of the Ni-Mo/amorphous silicon-aluminum solid catalyst with stronger acidity compared with the Ni-Mo/alumina catalyst with weaker acidity.
The invention provides a method and a method for preparing a bio-based n-alkane phase change material, and a method and a way for realizing the technical scheme are many, the above description is only a preferred embodiment of the invention, and it should be noted that, for a person skilled in the art, a plurality of improvements and modifications can be made without departing from the principle of the invention, and the improvements and modifications should also be regarded as the protection scope of the invention. All the components not specified in the present embodiment can be realized by the prior art.
Claims (10)
1. A preparation method of a bio-based n-alkane phase change material is characterized in that fatty glyceride reacts under the action of an acidic solid catalyst to obtain n-alkane.
2. The production method according to claim 1, wherein the fatty acid glyceride is obtained by refining a fat or oil as a raw material.
3. The production method according to claim 2, wherein the oil or fat is a non-edible vegetable oil or fat and/or a waste animal or vegetable oil or fat;
wherein the inedible vegetable oil is vegetable oil containing harmful substances to human body;
wherein the waste animal and vegetable oil and fat is any one or mixture of waste animal and vegetable oil and fat generated after frying oil and waste animal and vegetable oil and fat obtained in the meat production process.
4. The method of claim 2, wherein the refining comprises any one or more of degumming, water washing, adsorption and distillation.
5. The preparation method according to claim 1, wherein the acidic solid catalyst uses alumina or amorphous silica-alumina as a carrier, and at least two of sulfided Ni, sulfided Co, sulfided Mo and sulfided W are used as hydrogenation active components.
6. The preparation method according to claim 5, wherein the acidic solid catalyst comprises 15 to 25% by mass of active metal in terms of oxidation state, and the balance of a carrier.
7. The method according to claim 1, wherein the reaction conditions are as follows: the reaction temperature is 300-400 ℃, the hydrogen partial pressure is 3-18 MPa, and the liquid hourly space velocity is 0.5-3.0 h-1The volume ratio of hydrogen to oil is 500-1500 Nm3/m3。
8. The production method according to claim 1, wherein the normal paraffins include n-pentadecane, n-hexadecane, n-heptadecane, and n-octadecane.
9. The preparation method according to claim 1, wherein the fatty acid glyceride is subjected to hydrodeoxygenation/saturation reaction under the action of an acidic solid catalyst to obtain a mixture of n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane, and the mixture is rectified to separate the n-pentadecane, n-hexadecane, n-heptadecane and n-octadecane to obtain single-carbon-number monomer n-alkanes, namely the phase change material.
10. The method according to claim 7, wherein the purity of the monomeric n-alkanes is 98% or more, and the iodine value is 0.3g/100g or less.
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| CN116396136B (en) * | 2023-02-28 | 2025-05-06 | 北京集思拓新材料科技有限公司 | A method for preparing bio-based isoalkanes |
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Effective date of registration: 20241024 Address after: Room 901, Building 2, Tianjin Science and Technology Plaza, Kexue West Road, Nankai District, Tianjin 300300 (Tiankai Park) Patentee after: Tiankai Jisituo (Tianjin) New Materials Technology Co.,Ltd. Country or region after: China Address before: 100000 8-501, Lianhua garden, Beiyuan Jiayuan, Chaoyang District, Beijing Patentee before: Kong Fanhua Country or region before: China Patentee before: Huang Yang Patentee before: Zhou Yuanyuan |
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