CN109260747A - Production of biodiesel distills separation system with energy-saving type - Google Patents
Production of biodiesel distills separation system with energy-saving type Download PDFInfo
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- CN109260747A CN109260747A CN201811474137.5A CN201811474137A CN109260747A CN 109260747 A CN109260747 A CN 109260747A CN 201811474137 A CN201811474137 A CN 201811474137A CN 109260747 A CN109260747 A CN 109260747A
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- biodiesel
- shell
- rectifying
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- destilling tower
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- 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
- B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/10—Ester interchange
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention discloses production of biodiesel energy-saving types to distill separation system, it is unstable to solve the biodiesel quality that the prior art is isolated, it is difficult to produce the problem of being directly used in industrial industrial chemicals, the raw material and waste of energy for meeting export standard cannot be produced.The present invention includes oil-collecting plate, destilling tower, shell-and-tube heat exchanger, rectification chamber, distillation chamber, fatty acid methyl ester delivery pipe, feed inlet, the outer comb of soap component, loop heating system, the exceptionally defeated pipe of high-carbon distillation group, the exceptionally defeated pipe of rectifying group, the first cyclone hydraulic separators, industrial chemicals collecting tank, defeated pipe outside high rectifying component, the second cyclone hydraulic separators, high rectifying Fraction collection tank and high gently evaporates Fraction collection tank.Semi-finished product biodiesel can be isolated the high-carbon biodiesel finished product for meeting national Biodiesel Standards and stay in grade, the industrial chemicals for directly meeting industrial production, the high rectifying component product for directly meeting export targets and height and gently evaporate component product by energy conservation and environmental protection of the present invention.
Description
Technical field
The present invention relates to production of biodiesel energy-saving types to distill separation system.
Background technique
During production of biodiesel, from transesterification workshop section come out thick methyl esters (include fatty acid methyl ester, glycerol,
And a small amount of methanol and soap) isolate most glycerol in it after separating methanol, then using by the way of sedimentation, separation
The product obtained after glycerol be biodiesel semi-finished product (comprising fatty acid methyl ester and a small amount of water, methanol, glycerol and
Soap), to meet the standard of national biodiesel, it is also necessary to pass through last procedure ----distillation separating treatment, it is existing
The biodiesel finished color isolated of biodiesel distillation knockout tower is partially yellow, in moisture, glycerol and sulfur content wave
Move it is larger, it is exceeded to happen occasionally, influence product quality and be difficult to meet high-end requirement, be difficult to produce and may be directly applied to industrial life
The industrial chemicals of production can not produce the raw material that can meet export standard, while serious to energy waste.
Summary of the invention
Separation system is distilled with energy-saving type the technical problem to be solved by the present invention is providing production of biodiesel, is solved existing
The biodiesel quality for having technology to isolate is unstable, is difficult to produce and may be directly applied to industrial industrial chemicals,
The raw material that can meet export standard cannot be produced, and the problem of waste of energy.
To achieve the above object, The technical solution adopted by the invention is as follows:
Production of biodiesel distills separation system with energy-saving type, and the destilling tower of oil-collecting plate, the distillation are set including internal upper part
The internal upper part of tower is equipped with shell-and-tube heat exchanger, and the oil-collecting plate is located at the lower section of the shell-and-tube heat exchanger, and the shell-and-tube changes
The inner cavity of the destilling tower is separated into the rectification chamber above the shell-and-tube heat exchanger and is located at the shell-and-tube by hot device
Distillation chamber below heat exchanger, the rectification chamber and the distillation chamber are connected to by the shell side of the shell-and-tube heat exchanger, described
The tube side import of shell-and-tube heat exchanger is connected with for conveying fatty acid methyl to be distilled in the tube side for the shell-and-tube heat exchanger
The fatty acid methyl ester delivery pipe of ester, the lower part of the destilling tower are equipped with feed inlet, and the feed inlet by pipeline with it is described
The tube side of shell-and-tube heat exchanger exports connection；
The bottom of the destilling tower be connected with comb outside the soap component that is connected of distillation chamber, under the destilling tower
Portion is connected with the loop heating system for being heated for the fatty acid methyl ester to be distilled in the destilling tower, the destilling tower
Top be connected with and the exceptionally defeated pipe of high-carbon distillation group that is connected of distillation chamber, and the exceptionally defeated pipe position of the high-carbon distillation group
For the high-carbon distillation component on the oil-collecting plate is defeated outward at the oil-collecting plate；
The exceptionally defeated pipe of the rectifying group being connected with the rectification chamber, the rectifying component are connected at the top of the destilling tower
The outer end of outer defeated pipe is connected with the first cyclone hydraulic separators, and the bottom underflow opening of first cyclone hydraulic separators is connected with by pipeline
Industrial chemicals collecting tank, the top overflow port of first cyclone hydraulic separators is connected with defeated pipe outside high rectifying component, described high-precision
The outer end for evaporating the exceptionally defeated pipe of group is connected with the second cyclone hydraulic separators, and the bottom underflow opening of second cyclone hydraulic separators passes through pipeline
It is connected with high rectifying Fraction collection tank, the top overflow port of second cyclone hydraulic separators is connected with height and gently evaporates Fraction collection tank.
Further, the loop heating system includes being set to institute set on the circulating-heating outlet of the distillation tower bottom
The circulating-heating import for stating destilling tower lower part, the circulation being connected between the circulating-heating outlet and the circulating-heating import
Heating tube, and the circulating pump and recirculation heater that are respectively arranged on the circulating-heating pipe.
Further, the fatty acid methyl ester delivery pipe is equipped with for being the fat in the fatty acid methyl ester delivery pipe
The heater that sour methyl esters is heated.
Further, the exceptionally defeated pipe of the rectifying group is equipped with for being the rectifying component in the exceptionally defeated pipe of the rectifying group
Carry out cooling rectifying component condenser.
Further, defeated pipe is equipped with for being high-precision in defeated pipe outside the high rectifying component outside the high rectifying component
It evaporates component and carries out cooling high rectifying component condenser.
Further, the circulating-heating import is located at the lower section of the feed inlet.
Compared with prior art, the invention has the following advantages:
The configuration of the present invention is simple, design is scientific and reasonable, easy to use, energy conservation and environmental protection, can (include by semi-finished product biodiesel
Fatty acid methyl ester and a small amount of water, methanol, glycerol and soap) it isolates and meets national Biodiesel Standards and stay in grade
High-carbon biodiesel finished product (C18-C22Product accounts for about the 10%-15% of semi-finished product biodiesel total amount), directly to meet industry raw
Industrial chemicals (the C of production16-C18Product accounts for about the 40%-50% of semi-finished product biodiesel total amount), directly meet export targets
High rectifying component product (C12-C16Product accounts for about the 25%-30% of semi-finished product biodiesel total amount) and high gently evaporate component
Product (C6-C12Product accounts for about the 5%-25% of semi-finished product biodiesel total amount).
The present invention includes destilling tower, the first cyclone hydraulic separators and the second cyclone hydraulic separators, sets pipe shell type heat exchange in destilling tower
Device, while being connected with loop heating system, extraneous 40 DEG C of biodiesel semi-finished product (it include fatty acid methyl ester, and a small amount of
Water, methanol, glycerol and soap) via fatty acid methyl ester delivery pipe it is delivered to shell-and-tube heat exchanger, it is heated in the process via heater
To 100 DEG C or so, 100 DEG C or so of biodiesel semi-finished product are heated in the tube side of shell-and-tube heat exchanger and in its shell side
Distillation (270 DEG C -290 DEG C) exchange heat, biodiesel semi-finished product temperature be increased to 200 DEG C -220 DEG C after through by pipeline and
Feed inlet, which enters in destilling tower, participates in distillation separation.
Circulating pump in loop heating system extracts the biodiesel semi-finished product in destilling tower along circulating-heating Guan Xun out
It is entered back into destilling tower after ring, is heated in the process by recirculation heater, make the temperature one of biodiesel semi-finished product in destilling tower
270 DEG C -290 DEG C directly are maintained at, soap part in biodiesel semi-finished product is sunk, by comb outlet outside soap component, biodiesel (rouge
Fatty acid methyl esters) rise exchange heat in the shell side of shell-and-tube heat exchanger with the low-temperature biological diesel oil semi-finished product in its tube side, temperature
Degree is down to 240 DEG C -260 DEG C, high-carbon biodiesel (fatty acid methyl ester, predominantly C18-C22Product accounts for about semi-finished product biodiesel
The 10%-15% of total amount) heat exchange after fall down to oil-collecting plate and via defeated outside the exceptionally defeated pipe of high-carbon distillation group.
Rectifying component (C6-C18Product) continue to ascend into rectification chamber and under the action of the first cyclone hydraulic separators via essence
It evaporates the exceptionally defeated pipe of group and enters the first cyclone hydraulic separators, 240 DEG C -260 DEG C of rectifying component is under the condensation of rectifying component condenser
220 DEG C -240 DEG C are cooled to, the industrial chemicals (C of industrial production is directly met16-C18Product accounts for about semi-finished product biodiesel
The 40%-50% of total amount) via the bottom underflow opening and pipeline connected to it of the first cyclone hydraulic separators enter industrial chemicals receive
Collection tank is collected, high rectifying component (C6-C16Product) via the top overflow port of the first cyclone hydraulic separators and high rectifying component outside
Defeated pipe enters the second cyclone hydraulic separators, and 220 DEG C -240 DEG C of high rectifying component cools down under the condensation of high rectifying component condenser
To 160 DEG C -220 DEG C, high rectifying component (the predominantly C of export standard can be met12-C16Product accounts for about semi-finished product biodiesel
The 25%-30% of total amount) via the bottom underflow opening and pipeline connected to it of the second cyclone hydraulic separators enter high rectifying component
Collecting tank, while height gently evaporates component (C6-C12Product accounts for about the 5%-25% of semi-finished product biodiesel total amount) via the second spinning liquid
The top overflow port pipeline connected to it of separator enters height and gently evaporates Fraction collection tank.
Whole process is smooth efficiently, collects difference using two-stage rotary filter press and evaporates a section product, can effectively improve product quality,
Product quality is substantially improved, increases the scope of application of biodiesel, gained high-carbon biodiesel finished product meets national biodiesel
Standard and stay in grade, industrial chemicals may be directly applied to industrial production, and high rectifying component product and height gently evaporate component product product
Matter is high, can meet export targets；100 DEG C or so of biodiesel semi-finished product can be warming up to 200 DEG C -220 by shell-and-tube heat exchanger
DEG C, while can effectively reduce the outlet temperature of rectifying component, reduce condensing pressure and energy consumption, can the effectively save energy, benefit
In environmental protection.
Detailed description of the invention
Fig. 1 is schematic structural view of the invention.
Wherein, the corresponding title of appended drawing reference are as follows:
1- destilling tower, 2- oil-collecting plate, 3- shell-and-tube heat exchanger, 4- rectification chamber, 5- distillation chamber, the exceptionally defeated pipe of 6- rectifying group,
The first cyclone hydraulic separators of 7-, 8- fatty acid methyl ester delivery pipe, 9- feed inlet, the exceptionally defeated pipe of 10- high-carbon distillation group, 11- soap component
Outer comb, the outlet of 12- circulating-heating, the import of 13- circulating-heating, 14- circulating-heating pipe, 15- circulating pump, 16- recirculation heater,
17- heater, 18- rectifying component condenser, 19- industrial chemicals collecting tank, defeated pipe, the second spinning liquid of 21- outside 20- high rectifying component
Separator, 22- high rectifying Fraction collection tank, 23- high gently evaporate Fraction collection tank, 24- high rectifying component condenser.
Specific embodiment
The invention will be further described with embodiment for explanation with reference to the accompanying drawing, and mode of the invention includes but not only limits
In following embodiment.
As shown in Figure 1, production of biodiesel provided by the invention energy-saving type distills separation system, structure is simple, designs
Scientific and reasonable, semi-finished product biodiesel can (be included fatty acid methyl ester and a small amount of water, first by easy to use, energy conservation and environmental protection
Alcohol, glycerol and soap) isolate the high-carbon biodiesel finished product (C for meeting national Biodiesel Standards and stay in grade18-C22It produces
Product account for about the 10%-15% of semi-finished product biodiesel total amount), directly meet the industrial chemicals (C of industrial production16-C18It produces
Product account for about the 40%-50% of semi-finished product biodiesel total amount), directly meet the high rectifying component product (C of export targets12-C16
Product accounts for about the 25%-30% of semi-finished product biodiesel total amount) and high gently evaporate component product (C6-C12Product, account for about half at
The 5%-25% of product biodiesel total amount).The present invention includes the destilling tower 1 that internal upper part sets oil-collecting plate 2, the destilling tower 1 it is interior
Top is equipped with shell-and-tube heat exchanger 3, and the oil-collecting plate 2 is located at the lower section of the shell-and-tube heat exchanger 3, the shell-and-tube heat exchanger
The inner cavity of the destilling tower 1 is separated into the rectification chamber 4 above the shell-and-tube heat exchanger 3 and is located at the shell-and-tube by 3
The distillation chamber 5 of 3 lower section of heat exchanger, the rectification chamber 4 are connected to the distillation chamber 5 by the shell side of the shell-and-tube heat exchanger 3,
The tube side import of the shell-and-tube heat exchanger 3 is connected with for conveying rouge to be distilled in the tube side for the shell-and-tube heat exchanger 3
The fatty acid methyl ester delivery pipe 8 of fatty acid methyl esters, the fatty acid methyl ester delivery pipe 8 are equipped with for being that the fatty acid methyl ester is defeated
The heater 17 for sending the fatty acid methyl ester in pipe 8 to be heated, the lower part of the destilling tower 1 are equipped with feed inlet 9, and it is described into
Material mouth 9 is exported by the tube side of pipeline and the shell-and-tube heat exchanger 3 and is connected.
The lower part of destilling tower 1 of the present invention be connected with for for the fatty acid methyl ester to be distilled in the destilling tower 1 into
The loop heating system of row heating.The loop heating system includes that the circulating-heating set on 1 bottom of destilling tower exports 12,
Circulating-heating import 13 set on 1 lower part of destilling tower, be connected to circulating-heating outlet 12 and the circulating-heating into
Circulating-heating pipe 14 between mouth 13, and the circulating pump 15 and recirculation heater that are respectively arranged on the circulating-heating pipe 14
16, the circulating-heating import 13 is located at the lower section of the feed inlet 9.
The bottom of destilling tower 1 of the present invention is connected with comb 11 outside the soap component being connected with the distillation chamber 5, described
The top of destilling tower 1 is connected with the exceptionally defeated pipe 10 of high-carbon distillation group being connected with the distillation chamber 5, and the high-carbon distillation group
Exceptionally defeated pipe 10 is located at the oil-collecting plate 2 for the high-carbon distillation component on the oil-collecting plate 2 is defeated outward.
The top of destilling tower 1 of the present invention is connected with the exceptionally defeated pipe 6 of the rectifying group being connected with the rectification chamber 4, institute
The exceptionally defeated pipe 6 of rectifying group is stated to be equipped with for carrying out cooling rectifying group for the rectifying component in the exceptionally defeated pipe 6 of the rectifying group
Divide condenser 18, the outer end of the exceptionally defeated pipe 6 of the rectifying group is connected with the first cyclone hydraulic separators 7, first cyclone hydraulic separators 7
Bottom underflow opening industrial chemicals collecting tank 19 is connected with by pipeline, the top overflow port of first cyclone hydraulic separators 7 connects
It is connected to defeated pipe 20 outside high rectifying component, defeated pipe 20 is equipped with for being defeated pipe outside the high rectifying component outside the high rectifying component
High rectifying component in 20 carries out cooling high rectifying component condenser 24, the outer end connection of defeated pipe 20 outside the high rectifying component
There is the second cyclone hydraulic separators 21, the bottom underflow opening of second cyclone hydraulic separators 21 is connected with high rectifying component by pipeline and receives
Collect tank 22, the top overflow port of second cyclone hydraulic separators 21 is connected with height and gently evaporates Fraction collection tank 23.
The present invention includes destilling tower, the first cyclone hydraulic separators and the second cyclone hydraulic separators, sets pipe shell type heat exchange in destilling tower
Device, while being connected with loop heating system, extraneous 40 DEG C of biodiesel semi-finished product (it include fatty acid methyl ester, and a small amount of
Water, methanol, glycerol and soap) via fatty acid methyl ester delivery pipe it is delivered to shell-and-tube heat exchanger, it is heated in the process via heater
To 100 DEG C or so, 100 DEG C or so of biodiesel semi-finished product are heated in the tube side of shell-and-tube heat exchanger and in its shell side
Distillation (270 DEG C -290 DEG C) exchange heat, biodiesel semi-finished product temperature be increased to 200 DEG C -220 DEG C after through by pipeline and
Feed inlet, which enters in destilling tower, participates in distillation separation.
Circulating pump in loop heating system extracts the biodiesel semi-finished product in destilling tower along circulating-heating Guan Xun out
It is entered back into destilling tower after ring, is heated in the process by recirculation heater, make the temperature one of biodiesel semi-finished product in destilling tower
270 DEG C -290 DEG C directly are maintained at, soap part in biodiesel semi-finished product is sunk, by comb outlet outside soap component, biodiesel (rouge
Fatty acid methyl esters) rise exchange heat in the shell side of shell-and-tube heat exchanger with the low-temperature biological diesel oil semi-finished product in its tube side, temperature
Degree is down to 240 DEG C -260 DEG C, high-carbon biodiesel (fatty acid methyl ester, predominantly C18-C22Product accounts for about semi-finished product biodiesel
The 10%-15% of total amount) heat exchange after fall down to oil-collecting plate and via defeated outside the exceptionally defeated pipe of high-carbon distillation group.
Rectifying component (C6-C18Product) continue to ascend into rectification chamber and under the action of the first cyclone hydraulic separators via essence
It evaporates the exceptionally defeated pipe of group and enters the first cyclone hydraulic separators, 240 DEG C -260 DEG C of rectifying component is under the condensation of rectifying component condenser
220 DEG C -240 DEG C are cooled to, the industrial chemicals (C of industrial production is directly met16-C18Product accounts for about semi-finished product biodiesel
The 40%-50% of total amount) via the bottom underflow opening and pipeline connected to it of the first cyclone hydraulic separators enter industrial chemicals receive
Collection tank is collected, high rectifying component (C6-C16Product) via the top overflow port of the first cyclone hydraulic separators and high rectifying component outside
Defeated pipe enters the second cyclone hydraulic separators, and 220 DEG C -240 DEG C of high rectifying component cools down under the condensation of high rectifying component condenser
To 160 DEG C -220 DEG C, high rectifying component (the predominantly C of export standard can be met12-C16Product accounts for about semi-finished product biodiesel
The 25%-30% of total amount) via the bottom underflow opening and pipeline connected to it of the second cyclone hydraulic separators enter high rectifying component
Collecting tank, while height gently evaporates component (C6-C12Product accounts for about the 5%-25% of semi-finished product biodiesel total amount) via the second spinning liquid
The top overflow port pipeline connected to it of separator enters height and gently evaporates Fraction collection tank.
Whole process is smooth efficiently, collects difference using two-stage rotary filter press and evaporates a section product, can effectively improve product quality,
Product quality is substantially improved, increases the scope of application of biodiesel, gained high-carbon biodiesel finished product meets national biodiesel
Standard and stay in grade, industrial chemicals may be directly applied to industrial production, and high rectifying component product and height gently evaporate component product product
Matter is high, can meet export targets；100 DEG C or so of biodiesel semi-finished product can be warming up to 200 DEG C -220 by shell-and-tube heat exchanger
DEG C, while can effectively reduce the outlet temperature of rectifying component, reduce condensing pressure and energy consumption, can the effectively save energy, benefit
In environmental protection.
Above-described embodiment is only one of the preferred embodiment of the present invention, should not be taken to limit protection model of the invention
It encloses, as long as that in body design thought of the invention and mentally makes has no the change of essential meaning or polishing, is solved
The technical issues of it is still consistent with the present invention, should all be included within protection scope of the present invention.
Claims (6)
1. production of biodiesel distills separation system with energy-saving type, it is characterised in that: set the distillation of oil-collecting plate (2) including internal upper part
The internal upper part of tower (1), the destilling tower (1) is equipped with shell-and-tube heat exchanger (3), and the oil-collecting plate (2) is located at the shell-and-tube and changes
The lower section of hot device (3), the inner cavity of the destilling tower (1) is separated by the shell-and-tube heat exchanger (3) to be changed positioned at the shell-and-tube
Rectification chamber (4) above hot device (3) and the distillation chamber (5) below the shell-and-tube heat exchanger (3), the rectification chamber (4)
Be connected to distillation chamber (5) by the shell side of the shell-and-tube heat exchanger (3), the tube side of the shell-and-tube heat exchanger (3) into
Mouth is connected with for the fatty acid methyl ester conveying for conveying fatty acid methyl ester to be distilled in the tube side of the shell-and-tube heat exchanger (3)
It manages (8), the lower part of the destilling tower (1) is equipped with feed inlet (9), and the feed inlet (9) passes through pipeline and the shell-and-tube
The tube side of heat exchanger (3) exports connection；
The bottom of the destilling tower (1) is connected with the outer comb (11) of the soap component being connected with distillation chamber (5), the distillation
The lower part of tower (1) is connected with the circulating-heating system for being heated for the fatty acid methyl ester to be distilled in the destilling tower (1)
System, the top of the destilling tower (1) are connected with the exceptionally defeated pipe (10) of high-carbon distillation group being connected with distillation chamber (5), and
And the exceptionally defeated pipe (10) of the high-carbon distillation group is located at the oil-collecting plate (2) for distilling the high-carbon on the oil-collecting plate (2)
Component is defeated outward；
The exceptionally defeated pipe (6) of the rectifying group being connected with the rectification chamber (4), the essence are connected at the top of the destilling tower (1)
The outer end for evaporating the exceptionally defeated pipe (6) of group is connected with the first cyclone hydraulic separators (7), the bottom underflow of first cyclone hydraulic separators (7)
Mouth is connected with industrial chemicals collecting tank (19) by pipeline, and the top overflow port of first cyclone hydraulic separators (7) is connected with height
The exceptionally defeated pipe (20) of rectifying group, the outer end of defeated pipe (20) is connected with the second cyclone hydraulic separators (21), institute outside the high rectifying component
The bottom underflow opening for stating the second cyclone hydraulic separators (21) is connected with high rectifying Fraction collection tank (22), second rotation by pipeline
The top overflow port of liquid/gas separator (21) is connected with height and gently evaporates Fraction collection tank (23).
2. production of biodiesel according to claim 1 distills separation system with energy-saving type, it is characterised in that: the circulation
Heating system includes being set to following for the destilling tower (1) lower part set on the circulating-heating outlet (12) of the destilling tower (1) bottom
Ring heats import (13), the circulating-heating being connected between the circulating-heating outlet (12) and the circulating-heating import (13)
It manages (14), and the circulating pump (15) and recirculation heater (16) that are respectively arranged on the circulating-heating pipe (14).
3. production of biodiesel according to claim 1 distills separation system with energy-saving type, it is characterised in that: the fat
Sour methyl esters delivery pipe (8) is equipped with to be added for what is heated for the fatty acid methyl ester in the fatty acid methyl ester delivery pipe (8)
Hot device (17).
4. production of biodiesel according to claim 1 distills separation system with energy-saving type, it is characterised in that: the rectifying
The exceptionally defeated pipe (6) of group is equipped with for carrying out cooling rectifying component for the rectifying component in the exceptionally defeated pipe (6) of the rectifying group
Condenser (18).
5. production of biodiesel according to claim 1 distills separation system with energy-saving type, it is characterised in that: described high-precision
The exceptionally defeated pipe (20) of group is evaporated to be equipped with for carrying out cooling for the high rectifying component in defeated pipe (20) outside the high rectifying component
High rectifying component condenser (24).
6. production of biodiesel according to claim 1 distills separation system with energy-saving type, it is characterised in that: the circulation
Heating import (13) is located at the lower section of the feed inlet (9).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811474137.5A CN109260747A (en) | 2018-12-04 | 2018-12-04 | Production of biodiesel distills separation system with energy-saving type |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811474137.5A CN109260747A (en) | 2018-12-04 | 2018-12-04 | Production of biodiesel distills separation system with energy-saving type |
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