CN117586101A - Method and device for producing long-chain fatty alcohol by continuous low-pressure rectification of biological waste oil hydrogenated alcohol - Google Patents
Method and device for producing long-chain fatty alcohol by continuous low-pressure rectification of biological waste oil hydrogenated alcohol Download PDFInfo
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- CN117586101A CN117586101A CN202311519175.9A CN202311519175A CN117586101A CN 117586101 A CN117586101 A CN 117586101A CN 202311519175 A CN202311519175 A CN 202311519175A CN 117586101 A CN117586101 A CN 117586101A
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- 150000001298 alcohols Chemical class 0.000 title claims abstract description 62
- 239000010796 biological waste Substances 0.000 title claims abstract description 59
- 150000002191 fatty alcohols Chemical class 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 15
- HLZKNKRTKFSKGZ-UHFFFAOYSA-N tetradecan-1-ol Chemical compound CCCCCCCCCCCCCCO HLZKNKRTKFSKGZ-UHFFFAOYSA-N 0.000 claims abstract description 32
- KBPLFHHGFOOTCA-UHFFFAOYSA-N caprylic alcohol Natural products CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 claims abstract description 30
- MWKFXSUHUHTGQN-UHFFFAOYSA-N decan-1-ol Chemical compound CCCCCCCCCCO MWKFXSUHUHTGQN-UHFFFAOYSA-N 0.000 claims abstract description 30
- LQZZUXJYWNFBMV-UHFFFAOYSA-N dodecan-1-ol Chemical compound CCCCCCCCCCCCO LQZZUXJYWNFBMV-UHFFFAOYSA-N 0.000 claims abstract description 30
- GLDOVTGHNKAZLK-UHFFFAOYSA-N octadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCO GLDOVTGHNKAZLK-UHFFFAOYSA-N 0.000 claims abstract description 30
- BXWNKGSJHAJOGX-UHFFFAOYSA-N hexadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCO BXWNKGSJHAJOGX-UHFFFAOYSA-N 0.000 claims abstract description 23
- TVMXDCGIABBOFY-UHFFFAOYSA-N n-Octanol Natural products CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000004821 distillation Methods 0.000 claims abstract description 14
- 238000004519 manufacturing process Methods 0.000 claims abstract description 12
- 238000010992 reflux Methods 0.000 claims description 68
- 239000003921 oil Substances 0.000 claims description 57
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 30
- 239000000203 mixture Substances 0.000 claims description 22
- 239000004519 grease Substances 0.000 claims description 12
- 239000000126 substance Substances 0.000 claims description 8
- 239000006227 byproduct Substances 0.000 claims description 6
- 238000005984 hydrogenation reaction Methods 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims description 5
- 239000012075 bio-oil Substances 0.000 claims description 3
- 230000029226 lipidation Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 abstract description 15
- 235000019198 oils Nutrition 0.000 description 41
- 239000000047 product Substances 0.000 description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 17
- 238000009833 condensation Methods 0.000 description 15
- 230000005494 condensation Effects 0.000 description 15
- NLZUEZXRPGMBCV-UHFFFAOYSA-N Butylhydroxytoluene Chemical compound CC1=CC(C(C)(C)C)=C(O)C(C(C)(C)C)=C1 NLZUEZXRPGMBCV-UHFFFAOYSA-N 0.000 description 6
- 229960000541 cetyl alcohol Drugs 0.000 description 6
- GOQYKNQRPGWPLP-UHFFFAOYSA-N n-heptadecyl alcohol Natural products CCCCCCCCCCCCCCCCCO GOQYKNQRPGWPLP-UHFFFAOYSA-N 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- 235000019387 fatty acid methyl ester Nutrition 0.000 description 4
- 238000012856 packing Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- 239000003225 biodiesel Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 235000014113 dietary fatty acids Nutrition 0.000 description 2
- 229930195729 fatty acid Natural products 0.000 description 2
- 239000000194 fatty acid Substances 0.000 description 2
- 150000004665 fatty acids Chemical class 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 235000019482 Palm oil Nutrition 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 229930013930 alkaloid Natural products 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 239000003945 anionic surfactant Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000003093 cationic surfactant Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- -1 coatings Substances 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000008396 flotation agent Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000010794 food waste Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000007952 growth promoter Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000004702 methyl esters Chemical class 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 239000002736 nonionic surfactant Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000002540 palm oil Substances 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 230000008635 plant growth Effects 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 235000012424 soybean oil Nutrition 0.000 description 1
- 239000003549 soybean oil Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 235000015112 vegetable and seed oil Nutrition 0.000 description 1
- 239000008158 vegetable oil Substances 0.000 description 1
- 239000011782 vitamin Substances 0.000 description 1
- 229940088594 vitamin Drugs 0.000 description 1
- 229930003231 vitamin Natural products 0.000 description 1
- 235000013343 vitamin Nutrition 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4205—Reflux ratio control splitter
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol, which comprises the following steps: introducing biological waste oil hydrogenated alcohol into a deashing distillation tower, and separating refined biological waste oil hydrogenated alcohol from the bottom of the tower; introducing the refined biological waste oil hydrogenated alcohol into a first-stage rectifying tower, separating a first light component from the top of the tower, and separating a first heavy component from the bottom of the tower; introducing the first heavy component into a second-stage rectifying tower, separating hexadecanol from the top of the tower, and separating octadecanol from the bottom of the tower; introducing the first light component into a third-stage rectifying tower, separating a second light component from the top of the third-stage rectifying tower, and separating tetradecyl alcohol from the bottom of the third-stage rectifying tower; introducing the second light component into a fourth-stage rectifying tower, separating a third light component from the top of the tower, and separating dodecanol from the bottom of the tower; and (3) introducing the third light component into a fifth-stage rectifying tower, separating n-octanol from the top of the tower, and separating n-decanol from the bottom of the tower. The invention also discloses a device corresponding to the method. The method and the device can realize the high-efficiency and high-quality continuous separation of the long-chain fatty alcohol.
Description
Technical Field
The invention relates to a deep processing technology for extracting and separating long-chain fatty alcohol, in particular to a method and a device for producing long-chain fatty alcohol by continuous low-pressure rectification of biological waste oil hydrogenated alcohol.
Background
Long chain fatty alcohols generally refer to fatty alcohols having a carbon chain length of C6-C22, which carbon chain is predominantly linear and contains only one hydroxyl group, no double bond or one to more unsaturated c=c double bonds. The hydroxyl functional groups in the molecular structure can react with various substances to produce anionic, cationic and nonionic surfactants. The long-chain fatty alcohol and its derivatives can also be used in solvents, plasticizers, metal extractants and flotation agents for paints, coatings, synthetic resins, alkaloids, vitamins, etc., as well as in moisture-inhibiting agents, defoamers, plant growth promoters, etc. The long-chain fatty alcohol product has the advantages of good biodegradability, good compounding property, high solubility, good low temperature resistance and the like, is widely applied to industrial production, and plays an important role in various aspects of daily life.
At present, the production raw materials of domestic fatty alcohol mainly comprise mixed fatty acid methyl ester obtained by methyl esterification of natural vegetable oil (such as a production system for high-purity fatty alcohol disclosed in China patent publication No. CN108516924A adopts natural fatty acid, and a preparation method of natural fatty alcohol disclosed in China patent publication No. CN112661608A adopts natural oil), and the mixed fatty acid methyl ester is prepared by continuous or intermittent rectification separation and hydrogenation reaction (Liu Jianfeng. Full-process simulation and optimization of ester fractionation process in a fatty alcohol device [ D ]. Beijing university of chemical industry; lotus root, wei. Test operation of a fatty alcohol industrial rectification device [ J ]. Daily chemical science, 1981 (04): 28-31), and the preparation process mainly comprises the following steps: 1. the raw materials are soybean oil and palm oil, so that the cost is not low enough; 2. after the long-chain fatty alcohol is prepared by separating and hydrogenating fatty acid methyl ester, the product still needs to be separated and purified again, and the process is complex;
the crude fatty acid methyl ester obtained by processing the byproduct fatty acid of the edible oil refinery, nigre black horn, the byproduct grease of the lipidation factory and other grease has guaranteed supply and lower cost. The product of the project has wide variety of applications, stable market demand, good market potential and profit margin, and the biological waste oil hydrogenated alcohol prepared by hydrogenating the product is an excellent raw material source for preparing high-purity long-chain fatty alcohol.
However, the conventional method for preparing high-purity long-chain fatty alcohol by using biological waste oil hydrogenated alcohol prepared after hydrogenation at present has the following problems: 1. the energy consumption of unit product is high; 2. the biodiesel hydrogenated alcohol component is complex, and the existence of a large component product can lead to lower separation purity of a small component product.
Disclosure of Invention
The invention aims to provide a method and a device for producing long-chain fatty alcohol by continuous low-pressure rectification of waste oil hydrogenated alcohol, which can realize high-efficiency and high-quality continuous separation of long-chain fatty alcohol.
The invention provides the following technical scheme:
a method for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol, which comprises the following steps:
s1: introducing biological waste oil hydrogenated alcohol into a deashing distillation tower, separating micromolecular volatile substances from the tower top, and separating refined biological waste oil hydrogenated alcohol from the tower bottom; the refined waste bio-oil hydrogenated alcohol is a mixture containing C8, C10, C12, C14, C16 and C18 alkanols;
s2: introducing the refined biological waste oil hydrogenated alcohol into a first-stage rectifying tower, separating a first light component from the top of the tower, and separating a first heavy component from the bottom of the tower; the first light component is a mixture comprising C8, C10, C12, C14 alkanols; the first heavy component is a mixture comprising C16, C18 alkanols;
s3: introducing the first heavy component into a second-stage rectifying tower, separating hexadecanol from the top of the tower, and separating octadecanol from the bottom of the tower;
s4: introducing the first light component into a third-stage rectifying tower, separating a second light component from the top of the third-stage rectifying tower, and separating tetradecyl alcohol from the bottom of the third-stage rectifying tower; the second light component is a mixture containing C8, C10 and C12 alkanols;
s5: introducing the second light component into a fourth-stage rectifying tower, separating a third light component from the top of the tower, and separating dodecanol from the bottom of the tower; the third light component is a mixture containing C8 and C10 alkanols;
s6: and (3) introducing the third light component into a fifth-stage rectifying tower, separating n-octanol from the top of the tower, and separating n-decanol from the bottom of the tower.
Wherein, in the step S1, small-molecule volatile substances such as methanol and the like are separated from the top of the tower.
The working pressure of the first-stage rectifying tower is 100-300Pa, the bottom temperature is 148-180 ℃, the top temperature is 114-145 ℃, and the reflux ratio is 1:0.4 to 1:3, a step of;
the working pressure of the second-stage rectifying tower is 100-300Pa, the bottom temperature is 164-215 ℃, the top temperature is 135-175 ℃, and the reflux ratio is 1:1 to 1:5, a step of;
the working pressure of the third-stage rectifying tower is 100-300Pa, the bottom temperature is 135-175 ℃, the top temperature is 65-100 ℃, and the reflux ratio is 1: 2-1: 10;
the working pressure of the fourth-stage rectifying tower and the fifth-stage rectifying tower is 100 Pa to 300Pa, the temperature of the bottom of the tower is 120 ℃ to 170 ℃, the temperature of the top of the tower is 55 ℃ to 80 ℃, and the reflux ratio is 1: 2-1: 10.
the biological waste oil hydrogenated alcohol comprises 1-3% of methanol, 1-5% of n-octanol, 1-5% of n-decanol, 5-15% of dodecanol, 15-30% of tetradecanol, 35-65% of hexadecanol and 5-15% of octadecanol by mass fraction.
The biological waste oil hydrogenated alcohol is prepared by hydrogenating nigre black corners, grease byproducts of a grease chemical plant and other grease.
Preferably, in the step S1, the biological waste oil hydrogenated alcohol is preheated to 60-80 ℃ and then is introduced into a deashing distillation tower; in step S2, the feeding rate of the refined biological waste oil hydrogenated alcohol into the first-stage rectifying tower is 50-100kg/hr.
The method for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol provided by the invention adopts the multistage rectification-rectification tower T01-T05 to treat cheap biological waste oil hydrogenated alcohol under high vacuum to produce long-chain fatty alcohol, and has the advantages of low energy consumption in the production process, high product purity and simple flow, and is suitable for large-scale production.
The invention also provides a device for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol, which comprises: a first-stage rectifying tower, a second-stage rectifying tower, a third-stage rectifying tower, a fourth-stage rectifying tower and a fifth-stage rectifying tower; the bottom of the first-stage rectifying tower is connected with the second-stage rectifying tower, and the top of the tower is connected with the third-stage rectifying tower; the top of the third-stage rectifying tower is connected with a fourth-stage rectifying tower; the top of the fourth-stage rectifying tower is connected with a fifth-stage rectifying tower;
preferably, the number of the tower plates of the first-stage rectifying tower is 15-25; the number of the tower plates of the second-stage rectifying tower is 15-25; the number of tower plates of the third-stage rectifying tower is 15-25; the number of the tower plates of the fourth-stage rectifying tower is 12-20; the number of the fifth-stage rectifying tower plates is 12-20.
Preferably, a first condenser is arranged at the top of the first-stage rectifying tower and is connected with a first reflux tank and a first reflux pump; the top of the second-stage rectifying tower is provided with a second condenser which is connected with a second reflux tank and a second reflux pump; a third condenser is arranged at the top of the third-stage rectifying tower and is connected with a third reflux tank and a third reflux pump; the top of the fourth-stage rectifying tower is provided with a fourth condenser which is connected with a fourth reflux tank and a fourth reflux pump; the top of the fifth-stage rectifying tower is provided with a fifth condenser, and the fifth condenser is connected with a fifth reflux tank and a fifth reflux pump.
Preferably, the device comprises a first metering pump, wherein the first metering pump is connected with the first-stage rectifying tower; the bottom of the first-stage rectifying tower is connected with a first reboiler; the reboiler is also connected with the bottom of the first-stage rectifying tower through a first circulating pump.
Preferably, the bottom of the second-stage rectifying tower is provided with a first receiving tank, and the top of the second-stage rectifying tower is provided with a second receiving tank; the bottom of the second-stage rectifying tower is also connected with the bottom of the second-stage rectifying tower through a second circulating pump, and a second reboiler is arranged between the second circulating pump and the bottom of the second-stage rectifying tower;
preferably, a third receiving tank is arranged at the bottom of the third-stage rectifying tower; the bottom of the third-stage rectifying tower is also connected with the bottom of the third-stage rectifying tower through a third circulating pump, and a third reboiler is arranged between the third circulating pump and the bottom of the third-stage rectifying tower;
preferably, a fourth receiving tank is arranged at the bottom of the fourth-stage rectifying tower; the bottom of the fourth-stage rectifying tower is also connected with the bottom of the fourth-stage rectifying tower through a fourth circulating pump, and a fourth reboiler is arranged between the fourth circulating pump and the bottom of the fourth-stage rectifying tower;
preferably, a fifth receiving tank is arranged at the bottom of the fifth rectifying tower, and a sixth receiving tank is arranged at the top of the fifth rectifying tower; the bottom of the fifth-stage rectifying tower is also connected with the bottom of the fifth-stage rectifying tower through a fifth circulating pump, and a fifth reboiler is arranged between the fifth circulating pump and the bottom of the fifth-stage rectifying tower.
The device for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol provided by the invention realizes continuous rectification through the combination of rectification towers T01-T05; the high vacuum condition required by the rectifying towers T01-T05 is realized through a vacuum pump; then the top cooling and the bottom heating of the rectifying towers T01-T05 are realized through condensed water and a reboiler; and the purpose of reflux is realized by the circulating water pump, so that the utilization of biological waste oil with high value is fully realized, the energy consumption in the production process is greatly reduced, and the purity and the yield of the product are improved.
The advantages of the present invention compared to the prior art are represented in the following aspects:
(1) The biological waste oil hydrogenated alcohol is a fatty alcohol mixture prepared by hydrogenating nigre black corners, grease byproducts of a grease chemical plant and other grease, has low cost and large raw material quantity, and provides a scheme for treating food and biological waste oil;
(2) According to the invention, the mixed biological waste oil hydrogenated alcohol is directly subjected to rectification separation at one time, so that the conventional technical scheme of methyl ester separation, hydrogenation and separation is simplified;
(2) The continuous rectification process realizes full-automatic control, and the quality stability of the product is greatly improved;
(3) The components in the continuous rectification process are stable in composition, the system stability is high, and bad conditions such as flooding, entrainment and the like can be effectively prevented;
(4) The separation between different components can adopt different column plate numbers to meet the respective separation requirements, so that the high-purity separation of each component is realized, the purity of the product can reach more than 95%, and the product is higher than that of the conventional continuous low-pressure rectification;
(5) The components are thoroughly separated in the continuous rectification process, and the yield of each component is more than 90 percent and is higher than that of the conventional continuous low-pressure rectification;
(6) The total energy consumption of the low-pressure continuous rectification route is about 0.25kwh/kg, which is lower than that of the conventional continuous low-pressure rectification.
Drawings
In order to more clearly illustrate the technical solution of the embodiments of the present invention, the drawings that are needed in the description of the embodiments will be briefly described.
FIG. 1 is a block diagram of an apparatus for producing long-chain fatty alcohols by low-pressure continuous rectification of biological waste oil hydrogenated alcohols provided in the embodiments of the present invention;
FIG. 2 is a block diagram of an apparatus for producing long-chain fatty alcohols by low-pressure continuous rectification of biological waste oil hydrogenated alcohols provided in the comparative example of the present invention;
the figure identifies the description:
t01 is a first-stage rectifying tower, P01 is a first metering pump, E01 is a first condenser, V01 is a first reflux tank, P02 is a first reflux pump, E02 is a first reboiler, and P03 is a first circulating pump;
t02 is a second-stage rectifying tower, E03 is a second condenser, V02 is a second reflux tank, P05 is a second reflux pump, E04 is a second reboiler, P04 is a second circulating pump, and V04 and V03 are a first second collecting tank;
t03 is a third-stage rectifying tower, E05 is a third condenser, V05 is a third reflux tank, P06 is a third reflux pump, E06 is a third reboiler, P07 is a third circulating pump, and V06 is a third collecting tank;
t04 is a fourth-stage rectifying tower, E07 is a fourth condenser, V07 is a fourth reflux tank, P08 is a fourth reflux pump, E08 is a fourth reboiler, P09 is a fourth circulating pump, and V08 is a fourth collecting tank;
t05 is a fifth-stage rectifying tower, E09 is a fifth condenser, V09 is a fifth reflux tank, P10 is a fifth reflux pump, E10 is a fifth reboiler, P11 is a fifth circulating pump, and V11 and V10 are fifth and sixth collecting tanks.
Detailed Description
Specific embodiments may be exemplified by plural ones, and the detailed description will be made with reference to the accompanying drawings, in which the use cases, experimental comparison cases, etc. such as performance tests, etc. can be written, and test conditions and results are attached to each example.
The following describes in detail the embodiments of the present invention, which are implemented on the premise of the technical solution of the present invention, and detailed embodiments and specific operation procedures are given, but the scope of protection of the present invention is not limited to the following embodiments.
As shown in fig. 1, a continuous low-pressure rectification device for the biological waste oil hydroalcohol separation process comprises a first-stage rectification tower T01, a second-stage rectification tower T02, a third-stage rectification tower T03, a fourth-stage rectification tower T04 and a fifth-stage rectification tower T05; the bottom of the first-stage rectifying tower T01 is connected with the second-stage rectifying tower T02, and the top of the tower is connected with the third-stage rectifying tower T03; the top of the third-stage rectifying tower T03 is connected with a fourth-stage rectifying tower T04; the top of the fourth-stage rectifying tower T04 is connected with a fifth-stage rectifying tower T05.
The number of tower plates of the first-stage rectifying tower T01 is 15-25, and a first condenser E01 is arranged at the top of the tower; the number of tower plates of the second-stage rectifying tower T01 is 15-25, and a second condenser E02 is arranged on the top of the tower; the number of tower plates of the third-stage rectifying tower T03 is 15-25, and a third condenser E03 is arranged on the top of the tower; the number of tower plates of the fourth-stage rectifying tower T04 is 12-20, and a fourth condenser E04 is arranged on the top of the tower; the number of tower plates of the fifth-stage rectifying tower T05 is 12-20, and a fifth condenser E05 is arranged on the top of the tower.
The bottoms of the rectifying towers T01-T05 are respectively provided with circulating pumps, and the circulating pumps are respectively as follows: a first circulation pump P03, a second circulation pump P04, a third circulation pump P07, a fourth circulation pump P09, and a fifth circulation pump P11; the bottoms of the rectifying towers T01-T05 are respectively provided with a reboiler, and the reboilers are respectively: the first reboiler E02, the second reboiler E04, the third reboiler E06, the fourth reboiler E08 and the fifth reboiler E10 are used for heating and circulating the stillage liquid of the tower, and the reboiling ratio of the bottom of the tower can be controlled.
Specifically, the bottom of the first-stage rectifying tower T01 is connected with a first reboiler E02; the reboiler is also connected with the bottom of the first-stage rectifying tower through a first circulating pump P03;
the bottom of the second-stage rectifying tower T02 is provided with a first receiving tank V04, and the top of the second-stage rectifying tower T02 is provided with a second receiving tank V03; the bottom of the second-stage rectifying tower T02 is also connected with the bottom of the second-stage rectifying tower through a second circulating pump P04, and a second reboiler E04 is arranged between the second circulating pump P04 and the bottom of the second-stage rectifying tower;
a third receiving tank V06 is arranged at the bottom of the third-stage rectifying tower T03; the bottom of the third-stage rectifying tower T03 is also connected with the bottom of the third-stage rectifying tower through a third circulating pump P07, and a third reboiler E06 is arranged between the third circulating pump P07 and the bottom of the third-stage rectifying tower;
a fourth receiving tank V08 is arranged at the bottom of the fourth-stage rectifying tower T04; the bottom of the fourth-stage rectifying tower T04 is also connected with the bottom of the fourth-stage rectifying tower through a fourth circulating pump P09, and a fourth reboiler E08 is arranged between the fourth circulating pump P09 and the bottom of the fourth-stage rectifying tower;
a fifth receiving tank V11 is arranged at the bottom of the fifth-stage rectifying tower, and a sixth receiving tank V10 is arranged at the top of the fifth-stage rectifying tower; the bottom of the fifth-stage rectifying tower T05 is also connected with the bottom of the fifth-stage rectifying tower through a fifth circulating pump P11, and a fifth reboiler E10 is arranged between the fifth circulating pump P11 and the bottom of the fifth-stage rectifying tower;
meanwhile, the first-stage rectifying tower T01 is also connected with a first metering pump P01 for metering the amount of the hydrogenated alcohol of the raw material biological waste oil, and the feeding speed is controlled.
The biological waste oil hydrogenated alcohol is prepared from nigre black corners, grease byproducts of a lipidation factory and other grease through hydrogenation, and is sent into a deashing distillation tower after being heated and melted.
The first, second and third stage rectification towers T01, T02 and T03 can be selected as packed towers, specifically, the height of the packing is 1.5-2.5m, and the number of tower plates is 15-25.
The fourth and fifth rectifying towers T04 and T05 can be selected as packing towers, specifically, the packing height is 1.2-2.0m, and the number of tower plates is 12-20.
The device for the process for producing the long-chain fatty alcohol by continuously rectifying the biological waste oil hydrogenated alcohol at low pressure comprises the following steps:
s1: the biological waste oil hydrogenated alcohol preheated to 60-80 ℃ passes through a deashing distillation tower, the tower bottom temperature is 80-100 ℃, the tower top temperature is 60-65 ℃, the distillation tower is kept at normal pressure, small molecules such as methanol and the like are separated from the tower top, and the refined biological waste oil hydrogenated alcohol is separated from the tower bottom.
S2: the refined biological waste oil hydrogenated alcohol is pumped into a first-stage rectifying tower T01 through a first metering pump P01, and the flow is 50-100kg/hr; controlling the heat power of the first reboiler E02 and the cooling water flow of the first condenser E01 to control the reboiling ratio and the reflux ratio of the first-stage rectifying tower T01; the working pressure of the first-stage rectifying tower is 100-300Pa, the bottom temperature is 148-180 ℃, the top temperature is 114-145 ℃, and the reflux ratio is 1:0.4 to 1:3. separating a first heavy component from the bottom of the first-stage rectifying tower T01, wherein the first heavy component is a mixture containing C16 and C18 alkanol, and flowing the mixture into a connected second-stage rectifying tower T02 for continuous rectification; the first light component is separated from the top of the tower, and the first light component is a mixture containing C8, C10, C12 and C14 alkanol, and flows into a third-stage rectifying tower T03 for continuous rectification.
S3: controlling the heat power of the second reboiler E07 and the cooling water flow of the second condenser E02 to control the reboiling ratio and the reflux ratio of the second-stage rectifying tower T02; the working pressure of the second-stage rectifying tower T02 is 100-300Pa, the bottom temperature is 164-215 ℃, the top temperature is 135-175 ℃, and the reflux ratio is 1:1 to 1:5. the stearyl alcohol is separated from the bottom of the second-stage rectifying tower T02, part of the stearyl alcohol flows into the first receiving tank V04 for storage, and the other part of stearyl alcohol flows back to the second-stage rectifying tower T02 through the second circulating pump P04 and the second reboiler E04 for continuous rectification; cetyl alcohol is separated from the top of the tower, part of cetyl alcohol flows into the second receiving tank V03 to be stored, and the other part of cetyl alcohol flows back into the second-stage rectifying tower T02 through the second reflux pump P05.
S4: controlling the heat power of the third reboiler E06 and the cooling water flow of the third condenser E05 to control the reboiling ratio and the reflux ratio of the third rectifying tower T03; the working pressure of the third-stage rectifying tower T03 is 100-300Pa, the bottom temperature is 135-175 ℃, the top temperature is 65-100 ℃, and the reflux ratio is 1: 2-1: 10. tetradecyl alcohol is separated from the bottom of the third-stage rectifying tower T03, part of the tetradecyl alcohol flows into a third receiving tank V06 for storage, and the other part of the tetradecyl alcohol flows back into the third-stage rectifying tower T03 through a third circulating pump P07 and a third reboiler E06 for continuous rectification; and separating a second light component from the top of the tower, wherein the second light component is a mixture containing C8, C10 and C12 alkanol, part of the second light component flows into the fourth-stage rectifying tower T04 for continuous rectification, and the other part of the second light component flows back into the third-stage rectifying tower T03 through a third reflux pump P06.
S5: controlling the heat power of the fourth reboiler E08 and the cooling water flow of the fourth condenser E07 to control the reboiling ratio and the reflux ratio of the fourth-stage rectifying tower T04; the working pressure of the fourth-stage rectifying tower T04 is 100-300Pa, the bottom temperature is 120-170 ℃, the top temperature is 55-80 ℃, and the reflux ratio is 1: 2-1: 10. the dodecanol is separated from the bottom of the fourth-stage rectifying tower T04, part of the dodecanol flows into a fourth receiving tank V08 for storage, and the other part of the dodecanol flows back to the fourth-stage rectifying tower T04 through a fourth circulating pump P09 and a fourth reboiler E08 for continuous rectification; and separating a third light component from the top of the tower, wherein the second light component is a mixture containing C8 and C10 alkanol, part of the mixture flows into a fifth-stage rectifying tower T05 for continuous rectification, and the other part of the mixture flows back into a third-stage rectifying tower T03 through a fourth reflux pump P08.
S6: controlling the heat power of the fifth reboiler E10 and the cooling water flow of the fifth condenser E09 to control the reboiling ratio and the reflux ratio of the fifth-stage rectifying tower T05; the working pressure of the fifth-stage rectifying tower T05 is 100-300Pa, the bottom temperature is 120-170 ℃, the top temperature is 55-80 ℃, and the reflux ratio is 1: 2-1: 10. the bottom of the fifth-stage rectifying tower T05 is separated to obtain the n-decyl alcohol, part of the n-decyl alcohol flows into a fifth receiving tank V11 for storage, and the other part of the n-decyl alcohol flows back to the fifth-stage rectifying tower T05 through a fifth circulating pump P11 and a fifth reboiler E10 for continuous rectification; n-octanol is separated from the top of the tower, part of the n-octanol flows into a sixth receiving tank V10 for storage, and the other part of n-octanol flows back into a fifth rectifying tower T05 through a fifth reflux pump P10.
The biological waste oil hydrogenated alcohol is separated into six high-purity long-chain fatty alcohols through a five-stage low-pressure rectifying tower, and the products comprise n-octanol, n-decanol, dodecanol, tetradecanol, hexadecanol and octadecanol with the mass purity of more than 98 percent.
Example 1
The biological waste oil hydrogenated alcohol (2.0% methanol, 2.7% n-octanol, 3.4% n-decanol, 8.5% dodecanol, 20.6% tetradecanol, 53.5% hexadecanol, 9.2% octadecanol) with the following mass composition is preheated to 80 ℃, and is fed into a deashing distillation column at a feed rate of 50kg/hr, the bottom temperature of the deashing distillation column is 90 ℃, the top temperature is 65 ℃, the pressure is normal pressure, methanol is collected at the top of the column, and refined biological waste oil hydrogenated alcohol (C8, C10, C12, C14, C16, C18 alkanol) is collected at the bottom of the column
The refined biological waste oil hydrogenated alcohol is pumped into a first-stage rectifying tower T01 through a first metering pump P01, the number of the tower plates of the first-stage rectifying tower is 20, the feeding position is the 11 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.43:1, controlling the temperature of the top of the tower to be 85-90 ℃ and the temperature of the bottom of the tower to be 150-160 ℃ by controlling the condensation water amount of the first condenser E01 and the heat power of the first reboiler E02. At this time, the first light component (C8, C10, C12, C14 alkanol) was collected at the top of the column and the first heavy component (C16, C18 alkanol) was collected at the bottom of the column.
The first heavy component enters a second-stage rectifying tower T02, the number of tower plates of the second-stage rectifying tower is 20, the feeding position is 11 th tower plates, the working pressure is 200Pa, and the reflux ratio is 0.63:1, controlling the temperature of the top of the tower to be 135-140 ℃ and the temperature of the bottom of the tower to be 160-170 ℃ by controlling the condensation water amount of the second condenser E03 and the heat power of the second reboiler E04. At this time, cetyl alcohol was collected at the top of the column and stearyl alcohol was collected at the bottom of the column.
The first light component enters a third-stage rectifying tower T03, the number of tower plates of the third-stage rectifying tower is 19, the feeding position is the 9 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.5:1, controlling the temperature of the top of the tower to be 65-70 ℃ and the temperature of the bottom of the tower to be 125-130 ℃ by controlling the condensation water amount of the third condenser E05 and the heat power of the third reboiler E06. At this time, the second light component (C8, C10, C12 alkanol) was collected at the top and tetradecanol was collected at the bottom.
The second light component enters a fourth-stage rectifying tower T04, the number of tower plates of the fourth-stage rectifying tower is 15, the feeding position is a 7 th tower plate, the working pressure is 200Pa, and the reflux ratio is 1:1, controlling the temperature of the top of the tower to be 60-65 ℃ and the temperature of the bottom of the tower to be 120-125 ℃ by controlling the condensation water amount of the fourth condenser E07 and the heat power of the fourth reboiler E08. At this time, the third light component (C8, C10 alkanol) was collected at the top and dodecanol was collected at the bottom.
The third light component enters a fifth-stage rectifying tower T05, the number of tower plates of the fourth-stage rectifying tower is 15, the feeding position is a 7 th tower plate, the working pressure is 200Pa, and the reflux ratio is 1:1, controlling the temperature of the top of the tower to be 55-63 ℃ and the temperature of the bottom of the tower to be 115-120 ℃ by controlling the condensation water amount of the fifth condenser E09 and the heat power of the fourth reboiler E10. At this time, n-octanol was collected at the top of the column and n-decanol was collected at the bottom of the column.
The yields, purities and yields of the 5 components obtained are shown in Table 1.
Table 1 example 1 low pressure rectification separation product parameters
Example 2
The biological waste oil hydrogenated alcohol (2.2% methanol, 3.0% n-octanol, 3.3% n-decanol, 8.2% dodecanol, 23.1% tetradecanol, 55.7% hexadecanol, 4.5% octadecanol) with the following mass composition is preheated to 80 ℃, and is fed into a deashing distillation column at a feed rate of 50kg/hr, the bottom temperature of the deashing distillation column is 90 ℃, the top temperature is 65 ℃, the pressure is normal pressure, methanol is collected at the top of the column, and refined biological waste oil hydrogenated alcohol (C8, C10, C12, C14, C16, C18 alkanol) is collected at the bottom of the column
The refined biological waste oil hydrogenated alcohol is pumped into a first-stage rectifying tower T01 through a first metering pump P01, the number of the tower plates of the first-stage rectifying tower is 20, the feeding position is the 11 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.5:1, controlling the temperature of the top of the tower to be 85-90 ℃ and the temperature of the bottom of the tower to be 150-160 ℃ by controlling the condensation water amount of the first condenser E01 and the heat power of the first reboiler E02. At this time, the first light component (C8, C10, C12, C14 alkanol) was collected at the top of the column and the first heavy component (C16, C18 alkanol) was collected at the bottom of the column.
The first heavy component enters a second-stage rectifying tower T02, the number of tower plates of the second-stage rectifying tower is 20, the feeding position is 11 th tower plates, the working pressure is 200Pa, and the reflux ratio is 1:1, controlling the temperature of the top of the tower to be 135-140 ℃ and the temperature of the bottom of the tower to be 160-170 ℃ by controlling the condensation water amount of the second condenser E03 and the heat power of the second reboiler E04. At this time, cetyl alcohol was collected at the top of the column and stearyl alcohol was collected at the bottom of the column.
The first light component enters a third-stage rectifying tower T03, the number of tower plates of the third-stage rectifying tower is 19, the feeding position is the 9 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.7:1, controlling the temperature of the top of the tower to be 65-70 ℃ and the temperature of the bottom of the tower to be 125-130 ℃ by controlling the condensation water amount of the third condenser E05 and the heat power of the third reboiler E06. At this time, the second light component (C8, C10, C12 alkanol) was collected at the top and tetradecanol was collected at the bottom.
The second light component enters a fourth-stage rectifying tower T04, the number of tower plates of the fourth-stage rectifying tower is 15, the feeding position is a 7 th tower plate, the working pressure is 200Pa, and the reflux ratio is 1:1, controlling the temperature of the top of the tower to be 60-65 ℃ and the temperature of the bottom of the tower to be 120-125 ℃ by controlling the condensation water amount of the fourth condenser E07 and the heat power of the fourth reboiler E08. At this time, the third light component (C8, C10 alkanol) was collected at the top and dodecanol was collected at the bottom.
The third light component enters a fifth-stage rectifying tower T05, the number of tower plates of the fourth-stage rectifying tower is 15, the feeding position is a 7 th tower plate, the working pressure is 200Pa, and the reflux ratio is 1.5:1, controlling the temperature of the top of the tower to be 55-63 ℃ and the temperature of the bottom of the tower to be 115-120 ℃ by controlling the condensation water amount of the fifth condenser E09 and the heat power of the fourth reboiler E10. At this time, n-octanol was collected at the top of the column and n-decanol was collected at the bottom of the column.
The yields, purities and yields of the 5 components obtained are shown in Table 2.
TABLE 2 example 2 Low pressure rectification separation product parameters
Comparative example 1
The biological waste oil hydrogenated alcohol (2.0% methanol, 2.7% n-octanol, 3.4% n-decanol, 8.5% dodecanol, 20.6% tetradecanol, 53.5% hexadecanol, 9.2% octadecanol) with the following mass composition is preheated to 80 ℃, and is fed into a deashing distillation column at a feed rate of 50kg/hr, the bottom temperature of the deashing distillation column is 90 ℃, the top temperature is 65 ℃, the pressure is normal pressure, methanol is collected at the top of the column, and refined biological waste oil hydrogenated alcohol (C8, C10, C12, C14, C16, C18 alkanol) is collected at the bottom of the column
The refined biological waste oil hydrogenated alcohol is pumped into a first-stage rectifying tower T01 through a first metering pump P01, the number of the tower plates of the first-stage rectifying tower is 20, the feeding position is the 11 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.63:1, the temperature of the top of the tower is controlled to be 135-140 ℃ and the temperature of the bottom of the tower is controlled to be 160-170 ℃ by controlling the condensation water amount of the first condenser E01 and the heat power of the first reboiler E02. At this point, the first light fraction (C8, C10, C12, C14, C16 alkanol) was collected at the top and stearyl alcohol was collected at the bottom.
The first light component enters a second-stage rectifying tower T02, the number of tower plates of the second-stage rectifying tower is 20, the feeding position is the 11 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.45:1, controlling the temperature of the top of the tower to be 130-135 ℃ and the temperature of the bottom of the tower to be 150-160 ℃ by controlling the condensation water amount of the first condenser E03 and the heat power of the first reboiler E04. At this point, the second light fraction (C8, C10, C12, C14 alkanol) was collected at the top and cetyl alcohol was collected at the bottom.
The second light component enters a third-stage rectifying tower T03, the number of tower plates of the third-stage rectifying tower is 19, the feeding position is the 9 th tower plate, the working pressure is 200Pa, and the reflux ratio is 0.5:1, controlling the temperature of the top of the tower to be 65-70 ℃ and the temperature of the bottom of the tower to be 125-130 ℃ by controlling the condensation water amount of the third condenser E05 and the heat power of the third reboiler E06. At this time, the second light component (C8, C10, C12 alkanol) was collected at the top and tetradecanol was collected at the bottom.
The second light component enters a fourth-stage rectifying tower T04, the number of tower plates of the fourth-stage rectifying tower is 15, the feeding position is a 7 th tower plate, the working pressure is 200Pa, and the reflux ratio is 1:1, controlling the temperature of the top of the tower to be 60-65 ℃ and the temperature of the bottom of the tower to be 120-125 ℃ by controlling the condensation water amount of the fourth condenser E07 and the heat power of the fourth reboiler E08. At this time, the third light component (C8, C10 alkanol) was collected at the top and dodecanol was collected at the bottom.
The third light component enters a fifth-stage rectifying tower T05, the number of tower plates of the fourth-stage rectifying tower is 15, the feeding position is a 7 th tower plate, the working pressure is 200Pa, and the reflux ratio is 1:1, controlling the temperature of the top of the tower to be 55-63 ℃ and the temperature of the bottom of the tower to be 115-120 ℃ by controlling the condensation water amount of the fifth condenser E09 and the heat power of the fourth reboiler E10. At this time, n-octanol was collected at the top of the column and n-decanol was collected at the bottom of the column.
The yields, purities and yields of the 5 components obtained are shown in Table 3.
TABLE 3 comparative example 1 product parameters for conventional low pressure rectification separation
In combination with tables 1 to 3, the conventional low pressure rectification separation provided in comparative example 1 is slightly lower in total yield and lower in unit energy consumption by about 10% than that of examples, compared with examples 1 and 2. In addition, in the hydrogenated alcohol of the biodiesel, the proportion of tetradecyl alcohol and hexadecyl alcohol is the largest, and the two large components are separated in advance, so that the gas and liquid amount load of a subsequent rectifying tower can be reduced, the possibility of bad phenomena such as flooding and the like is reduced, and the purity of a small component product is improved.
The foregoing detailed description of the preferred embodiments and advantages of the invention will be appreciated that the foregoing description is merely illustrative of the presently preferred embodiments of the invention, and that no changes, additions, substitutions and equivalents of those embodiments are intended to be included within the scope of the invention.
Claims (10)
1. A method for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol, which is characterized by comprising the following steps:
s1: introducing biological waste oil hydrogenated alcohol into a deashing distillation tower, separating micromolecular volatile substances from the tower top, and separating refined biological waste oil hydrogenated alcohol from the tower bottom; the refined waste bio-oil hydrogenated alcohol is a mixture containing C8, C10, C12, C14, C16 and C18 alkanols;
s2: introducing the refined biological waste oil hydrogenated alcohol into a first-stage rectifying tower, separating a first light component from the top of the tower, and separating a first heavy component from the bottom of the tower; the first light component is a mixture comprising C8, C10, C12, C14 alkanols; the first heavy component is a mixture comprising C16, C18 alkanols;
s3: introducing the first heavy component into a second-stage rectifying tower, separating hexadecanol from the top of the tower, and separating octadecanol from the bottom of the tower;
s4: introducing the first light component into a third-stage rectifying tower, separating a second light component from the top of the third-stage rectifying tower, and separating tetradecyl alcohol from the bottom of the third-stage rectifying tower; the second light component is a mixture containing C8, C10 and C12 alkanols;
s5: introducing the second light component into a fourth-stage rectifying tower, separating a third light component from the top of the tower, and separating dodecanol from the bottom of the tower; the third light component is a mixture containing C8 and C10 alkanols;
s6: and (3) introducing the third light component into a fifth-stage rectifying tower, separating n-octanol from the top of the tower, and separating n-decanol from the bottom of the tower.
2. The method for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol according to claim 1, wherein the working pressure of the first-stage rectifying tower is 100-300Pa, the bottom temperature is 148-180 ℃, the top temperature is 114-145 ℃, and the reflux ratio is 1:0.4 to 1:3, a step of;
the working pressure of the second-stage rectifying tower is 100-300Pa, the bottom temperature is 164-215 ℃, the top temperature is 135-175 ℃, and the reflux ratio is 1:1 to 1:5, a step of;
the working pressure of the third-stage rectifying tower is 100-300Pa, the bottom temperature is 135-175 ℃, the top temperature is 65-100 ℃, and the reflux ratio is 1: 2-1: 10;
the working pressure of the fourth-stage rectifying tower and the fifth-stage rectifying tower is 100 Pa to 300Pa, the temperature of the bottom of the tower is 120 ℃ to 170 ℃, the temperature of the top of the tower is 55 ℃ to 80 ℃, and the reflux ratio is 1: 2-1: 10.
3. the method for producing long-chain fatty alcohols by low-pressure continuous rectification of biological waste oil hydrogenated alcohol according to claim 1, wherein the biological waste oil hydrogenated alcohol comprises 1% -3% methanol, 1% -5% by weight of n-octanol, 1% -5% by weight of n-decanol, 5% -15% by weight of dodecanol, 15% -30% by weight of tetradecanol, 35% -65% by weight of hexadecanol, 5% -15% by weight of octadecanol by mass fraction.
4. The method for producing long-chain fatty alcohols by low-pressure continuous rectification of biological waste oil hydrogenated alcohols according to claim 3, wherein said biological waste oil hydrogenated alcohols are produced by hydrogenation of nigre black corners, grease as a byproduct of a lipidation plant, and other grease.
5. The method for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol according to claim 1, wherein in the step S1, the biological waste oil hydrogenated alcohol is preheated to 60-80 ℃ and then is introduced into a deashing distillation tower; in step S2, the feeding rate of the refined biological waste oil hydrogenated alcohol into the first-stage rectifying tower is 50-100kg/hr.
6. An apparatus for producing long chain fatty alcohols by low pressure continuous rectification of waste bio-oil hydroalcohols for carrying out the process of any one of claims 1 to 5, said apparatus comprising: a first-stage rectifying tower, a second-stage rectifying tower, a third-stage rectifying tower, a fourth-stage rectifying tower and a fifth-stage rectifying tower; the bottom of the first-stage rectifying tower is connected with the second-stage rectifying tower, and the top of the tower is connected with the third-stage rectifying tower; the top of the third-stage rectifying tower is connected with a fourth-stage rectifying tower; the top of the fourth-stage rectifying tower is connected with a fifth-stage rectifying tower;
the number of the tower plates of the first-stage rectifying tower is 15-25; the number of the tower plates of the second-stage rectifying tower is 15-25; the number of tower plates of the third-stage rectifying tower is 15-25; the number of the tower plates of the fourth-stage rectifying tower is 12-20; the number of the fifth-stage rectifying tower plates is 12-20.
7. The device for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol according to claim 6, wherein the top of the first-stage rectifying tower is provided with a first condenser, and the first condenser is connected with a first reflux tank and a first reflux pump; the top of the second-stage rectifying tower is provided with a second condenser which is connected with a second reflux tank and a second reflux pump; a third condenser is arranged at the top of the third-stage rectifying tower and is connected with a third reflux tank and a third reflux pump; the top of the fourth-stage rectifying tower is provided with a fourth condenser which is connected with a fourth reflux tank and a fourth reflux pump; the top of the fifth-stage rectifying tower is provided with a fifth condenser, and the fifth condenser is connected with a fifth reflux tank and a fifth reflux pump.
8. The apparatus for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol according to claim 6, wherein the apparatus comprises a first metering pump, and the first metering pump is connected with a first-stage rectifying tower; the bottom of the first-stage rectifying tower is connected with a first reboiler; the reboiler is also connected with the bottom of the first-stage rectifying tower through a first circulating pump.
9. The device for producing long-chain fatty alcohol by low-pressure continuous rectification of waste oil hydrogenated alcohol according to claim 6, wherein the bottom of the second-stage rectification tower is provided with a first receiving tank, and the top of the second-stage rectification tower is provided with a second receiving tank; the bottom of the second-stage rectifying tower is also connected with the bottom of the second-stage rectifying tower through a second circulating pump, and a second reboiler is arranged between the second circulating pump and the bottom of the second-stage rectifying tower;
a third receiving tank is arranged at the bottom of the third-stage rectifying tower; the bottom of the third-stage rectifying tower is also connected with the bottom of the third-stage rectifying tower through a third circulating pump, and a third reboiler is arranged between the third circulating pump and the bottom of the third-stage rectifying tower.
10. The apparatus for producing long-chain fatty alcohol by low-pressure continuous rectification of biological waste oil hydrogenated alcohol according to claim 6, wherein a fourth receiving tank is arranged at the bottom of the fourth-stage rectification tower; the bottom of the fourth-stage rectifying tower is also connected with the bottom of the fourth-stage rectifying tower through a fourth circulating pump, and a fourth reboiler is arranged between the fourth circulating pump and the bottom of the fourth-stage rectifying tower;
a fifth receiving tank is arranged at the bottom of the fifth-stage rectifying tower, and a sixth receiving tank is arranged at the top of the fifth-stage rectifying tower; the bottom of the fifth-stage rectifying tower is also connected with the bottom of the fifth-stage rectifying tower through a fifth circulating pump, and a fifth reboiler is arranged between the fifth circulating pump and the bottom of the fifth-stage rectifying tower.
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