CN212128033U - Equipment for fractionating mixed fatty acid butyl ester - Google Patents
Equipment for fractionating mixed fatty acid butyl ester Download PDFInfo
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- CN212128033U CN212128033U CN202020307615.XU CN202020307615U CN212128033U CN 212128033 U CN212128033 U CN 212128033U CN 202020307615 U CN202020307615 U CN 202020307615U CN 212128033 U CN212128033 U CN 212128033U
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Abstract
The utility model relates to a device for fractionating mixed fatty acid butyl ester, including the coarse ester storage tank of second, coarse ester measuring pump, coarse ester heater, fractionating tower is connected with the vacuum pump, be equipped with the butyl palmitate condenser from top to bottom in proper order in fractionating tower, butyl palmitate receiver, first silk screen filler, coarse ester distributor, second silk screen filler, butyl palmitate heater, wherein coarse ester distributor and coarse ester heater intercommunication, the fractionating tower lower part is communicated in proper order through the flash distillation pipe has the circulating pump, falling liquid film heater, the flash column, be equipped with the butyl oleate condenser from top to bottom in proper order in the flash column, butyl oleate receiver, third silk screen filler, the intercommunication mouth between falling liquid film heater and the flash column is located third silk screen filler below; the method comprises the steps of material selection, material preparation and fractionation. Compared with the prior art, the utility model discloses the monomer purity that fractionates out is high, of high quality, still has operation automation, efficient, output is high, a great deal of advantage such as with low costs.
Description
Technical Field
The utility model relates to a fractionate mixed fatty acid butyl ester technical field, in particular to an equipment for mixing fatty acid butyl ester.
Background
The butyl ester product of monomer fatty acid (oleic acid, palmitic acid, stearic acid and the like) is a finished product obtained by esterification of fatty acid (such as oleic acid) and butanol and then deacidification and decoloration; specifically, the conventional production process of butyl oleate (including other fatty acid butyl esters) comprises the steps of heating commercial industrial oleic acid and butanol to 120-140 ℃ under an acid catalyst by using the conventional equipment, reacting for 4-8 hours to reach an esterification end point, neutralizing, washing with water, removing the catalyst, dehydrating, deodorizing and decolorizing to obtain a finished product; therefore, the production process based on the existing equipment has the defects of long flow, intermittent production, low yield, high cost and the like.
At present, the domestic refined edible rice bran oil is about 100-200 ten thousand tons, the byproduct rice bran oil mixed fatty acid generated in the refining process is about 5-10 ten thousand tons, and the byproduct is mainly used for soap making industry and extraction of industrial rice bran oleic acid; an apparatus is conceived, crude ester semi-finished product (mixed fatty acid butyl ester) obtained by esterifying rice bran oil mixed fatty acid and butanol is fractionated to obtain butyl palmitate and butyl oleate, and the butyl oleate is flashed and condensed to obtain a finished product.
In order to solve the prior art problem, the utility model provides an equipment for fractionating mixed fatty acid butyl ester possesses operation automation, of high quality, purity height, efficient, output, a great deal of advantage such as with low costs.
SUMMERY OF THE UTILITY MODEL
The utility model provides an equipment for fractionating mixed fatty acid butyl ester possesses a great deal of advantages such as operation automation, of high quality, purity height, efficient, output is high, with low costs.
The technical scheme of the utility model is realized like this:
the utility model provides an equipment for fractionating mixed fatty acid, includes the second coarse ester storage tank, coarse ester measuring pump, coarse ester heater, the fractionating tower that communicate in proper order through the fractionating tube, the fractionating tower is connected with the vacuum pump, is equipped with butyl palmitate condenser, butyl palmitate receiver, first silk screen filler, coarse ester distributor, second silk screen filler, butyl palmitate heater from top to bottom in proper order in the fractionating tower, wherein coarse ester distributor and coarse ester heater intercommunication, the fractionating tower lower part has circulating pump, falling liquid film heater, flash column through the flash tube intercommunication in proper order, is equipped with butyl oleate condenser, butyl oleate receiver, third silk screen filler in the flash column from top to bottom in proper order, the intercommunication mouth between falling liquid film heater and the flash column is located third silk screen filler below.
The utility model discloses equipment is used for fractionating and cutting and obtains butyl palmitate and butyl oleate, wherein the effect of vacuum pump makes in the fractionating tower keep negative pressure state, and the boiling point of butyl oleate reduces to about 200 ℃ under the vacuum, can distill out through heating like this; specifically, a crude ester metering pump pumps the crude ester (after catalyst washing) in a second crude ester storage tank, the crude ester sequentially passes through a crude ester heater and a crude ester distributor to enable the crude ester to enter a fractionating tower, wherein butyl palmitate is in a vapor state, butyl oleate is in a liquid state, the vapor butyl palmitate rises upwards and sequentially enters a first wire mesh filler, passes through a butyl palmitate receiver and enters a butyl palmitate condenser, the condensed vapor butyl palmitate is in a liquid state and flows downwards into the butyl palmitate receiver and then flows out of the fractionating tower, the unvaporized liquid butyl palmitate downwards flows through the second wire mesh filler and the butyl palmitate heater, the unvaporized liquid butyl palmitate is vaporized and rises until the butyl palmitate condenser, the butyl oleate liquid downwards flows through the second wire mesh filler and the butyl palmitate heater (the boiling point of butyl oleate is higher than that of butyl palmitate, therefore, butyl oleate is not vaporized), then sequentially enters a falling film heater (for heating the butyl oleate into a vapor state) and a flash tower through a circulating pump, the vapor-state butyl oleate sequentially rises in the flash tower, passes through a third wire mesh filler, a butyl oleate receiver and enters a butyl oleate condenser, the condensed vapor-state butyl oleate is in a liquid state, downwards flows into the butyl oleate receiver and then flows out of the fractionating tower, and unvaporized impurities and plant asphalt flow out of the bottom of the tower; adopt oleic acid to add butanol to make butyl oleate at present, and the utility model discloses an equipment obtains butyl oleate, butyl palmitate monomer through the separation that the fractionation mode is applied to mixed fatty acid butyl ester, and is very rare, and the utility model discloses the monomer purity that fractionates out is high, of high quality, still has operation automation, efficient, output a great deal of advantage such as high, with low costs.
Preferably, the crude ester distributor comprises a feeding main pipe and a plurality of branch pipes connected to two sides of the feeding main pipe, the feeding main pipe is communicated with the branch pipes, and the feeding main pipe and the branch pipes are respectively provided with a distribution hole.
The crude ester (liquid butyl oleate, vapor butyl palmitate and impurities) enters the main feeding pipe and the branch pipes, then flows out of the distribution holes and further enters the fractionating tower.
Preferably, the distribution holes include an upper distribution hole with an upward opening and a lower distribution hole with a downward opening.
The upper distribution holes flow out of the vaporous butyl palmitate, and the lower distribution holes flow out of the liquid butyl oleate and impurities, so that the efficiency is high.
Preferably, the circulating pump is a water vapor injection circulating pump, and the lower part of the flash tower is communicated with the circulating pump through a vapor recovery pipe.
After entering a circulating pump, the water vapor is violently expanded under negative pressure (the fractionating equipment is vacuumized by a vacuum pump) to drive the butyl oleate liquid to enter a falling film type heater, the water vapor provides power to repeatedly and circularly heat the liquid butyl oleate to convert the liquid butyl oleate into a vapor state, and impurities in the liquid butyl oleate cannot be converted into the vapor state to form residue impurities.
Preferably, the tube side of the falling film heater is communicated with the flash evaporation tube, and heat conducting oil is arranged in the shell side of the flash evaporation tube.
The liquid butyl oleate flowing into the falling film heater is vaporized.
Preferably, the butyl palmitate receiver and the butyl oleate receiver both comprise receiver discs, through pipes are connected to the receiver discs in a penetrating manner, the side walls of the upper parts of the through pipes are provided with steam inlets, the upper ends of the through pipes are connected with caps, retaining rings extending upwards are arranged at the upper peripheries of the receiver discs, and discharge grooves are formed in the retaining rings.
The vapor-liquid separation is effectively realized, wherein vapor-state (butyl palmitate and butyl oleate) materials rise to enter the through pipe and the vapor inlet and then enter the corresponding condensers (butyl palmitate condenser and butyl oleate condenser) to be condensed into liquid-state materials (butyl palmitate and butyl oleate) which flow downwards into the material receiving disc and flow out of the equipment through the discharge chute, and the liquid-state materials cannot flow into the through pipe due to the arrangement of the cover cap; high efficiency and high purity of the separated finished product.
Preferably, the butyl palmitate receiver is connected with a butyl palmitate storage tank, and the butyl oleate receiver is connected with a butyl oleate storage tank.
And (4) enabling the butyl palmitate finished product to enter a butyl palmitate storage tank, and enabling the butyl oleate finished product to enter a butyl oleate storage tank.
Preferably, the bottom of the flash tower is provided with a residue outlet, and the residue outlet is connected with an asphalt storage tank.
Preferably, the side wall of the crude ester heater is provided with heat conduction oil.
Heating the crude ester, and separating out vaporous butyl palmitate, liquid butyl oleate and residues.
Preferably, the butyl palmitate heater is a heat-conducting oil heating coil.
The butyl palmitate is in a liquid state without vaporization, so that the purity is improved by vaporizing the butyl palmitate.
Adopted above-mentioned technical scheme the beneficial effects of the utility model are that:
the utility model provides an equipment for fractionating mixed fatty acid butyl ester possesses a great deal of advantages such as operation automation, of high quality, purity height, efficient, output is high, with low costs. Adopt oleic acid to add butanol to make butyl oleate at present, and the utility model discloses an equipment obtains butyl oleate, butyl palmitate monomer through the separation that the fractionation mode is applied to mixed fatty acid butyl ester, and is very rare, and the utility model discloses the monomer purity that fractionates out is high, of high quality, still has operation automation, efficient, output a great deal of advantage such as high, with low costs. The separated butyl palmitate and butyl oleate are widely applied to the plastic industry and the lubricating oil industry, wherein the butyl oleate is light in color and high in purity, the flash point reaches over 180 ℃, the technical indexes of lubricating oil additives are completely met, and the impurity vegetable asphalt can be used as fuel or a casting binder.
Drawings
FIG. 1 is a schematic view of the overall configuration of an esterification apparatus according to an embodiment;
FIG. 2 is an enlarged view of portion A of FIG. 1;
FIG. 3 is a schematic view of the overall configuration of a fractionation apparatus according to an embodiment;
FIG. 4 is a schematic view of the structure of the material receiving tray of the butyl palmitate material receiver and the butyl oleate material receiver;
FIG. 5 is a schematic diagram of the distributor structures of the acid mixing distributor, the butanol distributor and the crude ester distributor;
reference numerals:
Detailed Description
The specific implementation manner of the utility model is as follows:
the utility model discloses a fractionation equipment is to fractionate mixed fatty acid butyl ester and obtains butyl oleate, butyl palmitate, puts the thing pitch, and this embodiment esterifies mixed fatty acid through a device of esterifying and obtains mixed fatty acid butyl ester, then combines fractionation equipment to realize fractionating.
As shown in FIGS. 1 to 5, an esterification apparatus 100 and a fractionation facility 200.
The esterification device 100 comprises a mixed acid storage tank 102, a mixed acid metering pump 103, a heat exchanger 104, a mixed acid heater 105 and an esterification tower 106 which are sequentially communicated through an acid mixing pipe 101, wherein 2 under-tower esterification kettles 107 which can be alternately communicated with the lower part of the esterification tower 106 are arranged at the bottom of the esterification tower 106.
Further, a demisting wire mesh 1061 (a steam outlet 1062 is arranged above or beside the demisting wire mesh 1061, the steam outlet 1062 is communicated with the heat exchanger 104), an acid mixing distributor 1063 communicated with the acid mixing heater 105, and 3 corrugated packings 1064 arranged up and down are sequentially arranged in the esterification tower 106 from top to bottom, and an in-tower heater 1065 (a shell-and-tube heater is adopted to facilitate the flow of the materials in the esterification tower 106) is arranged between every two adjacent corrugated packings 1064 arranged up and down; one end of an inner tube pass of the heat exchanger 104 is connected with the mixed acid metering pump 103 through the mixed acid tube 101, the other end of the inner tube pass of the heat exchanger 104 is connected with the mixed acid heater 105 through the mixed acid tube 101, one end of an inner shell pass of the heat exchanger 104 is connected with the steam outlet 1062, the other end of the inner shell pass of the heat exchanger 104 is connected with the alcohol-water separator 108, the alcohol-water separator 108 is specifically an alcohol-water separation tower and comprises an alcohol outlet end 1081 and a water outlet end 1082, wherein the alcohol outlet end 1081 is communicated with a butanol storage tank 112, and the water outlet end 1082 is communicated with the water storage. The esterification column 106 is connected to a pressure self-regulating valve 110 for automatically controlling the pressure in the column.
A liquid pipe 1071 and a gas pipe 1072 are connected between each esterification kettle 107 and the esterification tower 106, one end of the liquid pipe 1071 is connected with the bottom of the esterification tower 106, the other end is connected with the upper part of the esterification kettle 107, one end of the gas pipe 1072 is connected with the top of the esterification kettle 107, the other end is connected with the lower part of the esterification tower 106, in the esterification tower 106, the pipe orifice of the gas pipe 1072 is higher than the pipe orifice of the liquid pipe 1071, a liquid level meter linkage valve 1071A is connected on the liquid pipe 1071, a check valve 1072A is connected on the gas pipe 1072 (wherein the linkage valve in the liquid level meter linkage valve 1071A is in linkage control with the liquid level meter on the esterification kettle under the tower, when the crude ester liquid level in the esterification kettle under the tower rises to a preset position, the liquid level meter sends a signal to the linkage valve to automatically close the crude ester to stop feeding, the check valve 1072A is a one-way valve, the vapor butanol in the esterification kettle under the tower rises to enter the esterification tower through the check, when the rising of the vaporous butanol stops, the check valve is automatically closed, and the vaporous butanol in the esterification tower cannot flow back to the esterification kettle below the tower).
In order to facilitate the examination of the content index of the crude ester mixed acid in the esterification kettle 107 under the tower, the esterification kettle 107 under the tower is provided with a sampling port which can be opened and closed. In addition, a crude ester regulating valve 1132 is connected to the crude ester pipe 113 between the crude ester discharge pump 1131 and the outside of the esterification reactor 107 under the tower, so as to control the discharge of the crude ester to the first crude ester storage tank.
Specifically, regarding the esterification apparatus 100, the mixed acid (rice bran oil mixed fatty acid) in the mixed acid storage tank 102 is pumped by the mixed acid metering pump 103, the mixed acid sequentially passes through the heat exchanger 104, the mixed acid heater 105 and the mixed acid distributor 1063, so that the mixed acid enters the esterification tower 106 and flows down along the surface of the corrugated packing 1064, meanwhile, the butanol metering pump 1111 pumps butanol in the butanol storage tank 112, the butanol passes through the butanol heater 1112 to become vaporous butanol, the vaporous butanol passes through the butanol distributor 1113 to enter the bottom of the esterification kettle, the vaporous butanol on one hand and the unreacted rice bran oil mixed fatty acid flowing into the esterification kettle 107 under the tower are subjected to esterification reaction under the stirring of the stirring rod 1073 (so that the content of the fatty acid in the crude ester is reduced to be within 0.2%), on the other hand, the unreacted vaporous butanol rises into the esterification tower 106 through the vaporous pipe 1072 and is fully mixed with the mixed acid flowing down along the surface of the corrugated packing 1064, Repeatedly contacting, carrying out esterification reaction under the action of a catalyst (wherein a heater 1065 in the tower provides reaction temperature for the esterification reaction), enabling the generated crude ester to flow into an esterification kettle 107 below the tower through a liquid pipe 1071, repeatedly circulating to realize continuous esterification, wherein the generated vaporous water and unreacted vaporous butanol continuously rise to the upper part of the esterification tower 106 and enter an alcohol-water separator 108 through a demisting wire 1061, a vaporous outlet 1062 and a heat exchanger 104, discharging the water out of the device, and enabling the liquid butanol to flow back into a butanol storage tank 112 to participate in the esterification reaction; when the amount of the crude ester in the esterification kettle under one tower reaches a certain amount, closing the corresponding liquid pipe and butanol pipe to stop the crude ester and the vaporous butanol from entering the esterification kettle under the tower (because the check valve on the vapor pipe is a one-way valve, the vaporous butanol in the esterification kettle under the tower rises through the check valve to enter the esterification tower, and when the vaporous butanol stops rising, the check valve is automatically closed, and the vaporous butanol in the esterification tower cannot flow back to the esterification kettle under the tower); and simultaneously opening a liquid pipe and a butanol pipe corresponding to the other esterification kettle under the tower, the inner part of which is empty, so that the esterification kettle under the tower is communicated with the esterification tower, the esterification continuity is ensured, the production stop is not needed, simultaneously, the content index of the mixed acid of the crude ester in the esterification kettle under the tower is detected, if the mixed acid content index does not reach the standard, the vaporous butanol is continuously introduced into the esterification kettle under the tower to continue the esterification reaction, and when the mixed acid content index reaches the standard, the crude ester flows into the first crude ester storage tank 114 for standby.
The fractionating apparatus 200 comprises a second crude ester storage tank 202, a crude ester metering pump 203, a crude ester heater 204 and a fractionating tower 205 which are sequentially communicated through a fractionating pipe 201, the fractionating tower 205 is connected with a vacuum pump (not shown) for maintaining a negative pressure state in the fractionating tower 205, a butyl palmitate condenser 2051, a butyl palmitate receiver 2052 (connected with the butyl palmitate storage tank 2053), a first wire mesh filler 2054, a crude ester distributor 2055, a second wire mesh filler 2056 and a butyl palmitate heater 2057 are sequentially arranged in the fractionating tower 205 from top to bottom, wherein the crude ester distributor 2055 is communicated with the crude ester heater 204, the lower part of the fractionating tower 205 is sequentially communicated with a circulating pump 206 (specifically a water vapor injection circulating pump), a falling film heater 207 and a flash tower 208 through a flash pipe 211, a butyl oleate condenser 2081, a butyl oleate receiver 2082 (connected with the butyl oleate storage tank 2083) are sequentially arranged in the flash tower 208 from top to bottom, A third wire mesh packing 2084, wherein a communication port 2071 between the falling film heater 207 and the flash tower 208 is positioned below the third wire mesh packing 2084; wherein the lower portion of the flash column 208 is in communication with the circulation pump 206 through a vapor recovery pipe 209.
The butyl palmitate receiver 2052 and the butyl oleate receiver 2082 are both of a receiver structure, and specifically, as shown in fig. 4, the butyl palmitate receiver 2052 and the butyl oleate receiver 2082 comprise a receiver 401, a through pipe 402 is connected to the receiver 401 in a penetrating manner, the upper side wall of the through pipe 402 is provided with an air inlet 403, the upper end of the through pipe 402 is connected with a cap 404 (cap-shaped structure) which prevents purified liquid butyl palmitate and liquid butyl oleate from flowing into the through pipe 402, the upper periphery of the receiver 401 is provided with an upwardly extending retaining ring 405, and the retaining ring 405 is provided with a discharge chute 406 which is communicated with a butyl palmitate storage tank and a butyl oleate storage tank; taking the butyl palmitate receiver 2052 as an example, the vaporous butyl palmitate rises through the through pipe and the steam inlet and enters the butyl palmitate condenser, the formed liquid butyl palmitate flows into the receiver, and the liquid butyl palmitate cannot flow into the through pipe due to the blocking of the cap 404.
A cleaning storage tank (not shown) is connected between the butyl palmitate receiver 2052 and the butyl oleate receiver first crude ester storage tank 114 and the second crude ester storage tank 202, a feeding pipe is connected between the cleaning storage tank and the second crude ester storage tank 202, and a feeding pump (used for pumping the crude ester in the cleaning storage tank into the second crude ester storage tank 202) is arranged on the feeding pipe.
And a residue outlet is formed at the bottom of the flash tower and is connected with an asphalt storage tank 210.
The first wire mesh packing 2054 and the second wire mesh packing 2056 are stainless wire mesh packing, and have the functions of realizing vapor-liquid exchange and separating different components; the third wire mesh packing 2084 is also a stainless wire mesh packing and is used for separating impurities in the butyl oleate; in addition, butyl oleate is fed in the tube pass of the falling film heater 207, and heat conducting oil is fed outside the tube pass (shell pass), so that the liquid butyl oleate is heated and changed into vapor butyl oleate, and the vapor butyl oleate enters the flash tower 208.
In the fractionation apparatus 200, the crude ester (catalyst-washed crude ester) in the second crude ester storage tank 202 is pumped by the crude ester metering pump 203, and the crude ester passes through the crude ester heater 204 and the crude ester distributor 2055 in sequence to enter the fractionation tower 205, wherein the butyl palmitate is in a vapor state and the butyl oleate is in a liquid state, the vapor butyl palmitate rises upward and enters the first wire mesh packing 2054, passes through the butyl palmitate receiver 2052, enters the butyl palmitate condenser 2051, the condensed vapor butyl palmitate is in a liquid state and flows downward into the butyl palmitate receiver 2052 and then flows out of the fractionation tower 205, wherein the unvaporized butyl palmitate passes downward and passes through the second wire mesh packing 2056 and the butyl palmitate heater 2057, and is vaporized and rises to the butyl palmitate condenser 2051 by the butyl palmitate heater 2057, and the butyl oleate liquid flows downward and passes through the second wire mesh packing 2056, the butyl oleate distributor 2056, the butyl oleate liquid, A butyl palmitate heater 2057 (the boiling point of butyl oleate is higher than that of butyl palmitate, so that butyl oleate is not vaporized) and then sequentially enters the falling film heater 207 (for heating butyl oleate into a vapor state) and the flash tower 208 through the circulating pump 206, the vapor-state butyl oleate sequentially rises in the flash tower 208, passes through the third wire mesh filler 2084, passes through the butyl oleate receiver 2082, enters the butyl oleate condenser 2081, the condensed vapor-state butyl oleate becomes a liquid state, flows downwards into the butyl oleate receiver 2082, then flows out of the fractionating tower 205, enters the butyl oleate storage tank, and the plant asphalt flows out of the tower and enters the asphalt storage tank 210.
The side wall of the mixed acid heater 105, the side wall of the butanol heater 1112 and the side wall of the crude ester heater 204 in the embodiment are all provided with heat conduction oil; the external kettle heater 1075 and the butyl palmitate heater 2057 are heat-conducting oil heating coils.
The acid mixing distributor 1063, the butanol distributor 1113, and the crude ester distributor 2055 in this embodiment are all pressure-type distributors, and specifically include a feeding main pipe 301 connected to a corresponding material and a plurality of branch pipes 302 connected to both sides of the feeding main pipe 301, as shown in fig. 5, the feeding main pipe 301 is communicated with the branch pipes 302, and the feeding main pipe 301 and the branch pipes 302 are both provided with distribution holes 303 for the material to flow out; wherein the acid mixing distributor 1063 and the butanol distributor 1113 only comprise downward-facing distribution holes, and the crude ester distributor 2055 comprises both upward-facing distribution holes and downward-facing distribution holes.
The parameters of the esterification column 106, the in-column heater 1065, the under-column esterification reactor 107, the fractionating column 205, and the flash column 208 in this embodiment are as follows:
esterification column 106:
the diameter DN is 0.3-2 m, preferably DN1.2m; the height is 10-30 m, preferably 20m, the height is divided into three sections, each section is 6m (the corrugated packing is 1064 sections are 5m), and the height of each section is 1m at the top and the bottom of the tower; the wall thickness of the tower body is 8-12 mm, preferably 10mm, the tower body is made of 316L stainless steel lining polytetrafluoroethylene plates, and the corrugated packing 1064 is made of ceramic; the pressure resistance of the tower body is more than or equal to 2.5MPa, and the operating pressure is 0.1-0.35 MPa; the diameter size of esterifying tower 106 is with being related to output, and under the prerequisite of esterifying tower 106 high definite, its diameter is big more, and the feed volume is more, but the diameter is big, and the material distributes inequality easily, and contact, reaction number of times descend, and the esterification rate reduces on the contrary, consequently, the utility model discloses a diameter is comparatively suitable for 0.3 ~ 2m, guarantees the esterification rate.
In-tower heater 1065:
the diameter DN is matched with the diameter DN1.2m of the esterification tower 106, and the material is 316L stainless steel coated with polytetrafluoroethylene;
esterification kettle under column 107:
comprises an esterification kettle A under the tower and an esterification kettle B under the tower, each of which has a volume of 10m3The kettle body is made of 316L stainless steel lined polytetrafluoroethylene, the pressure resistance of the kettle body is more than or equal to 2.5MPa, and the operating pressure is 0.1-0.35 MPa;
fractionating column 205:
the diameter DN is 0.6-2.5 m, preferably 1.5 m; the height is 8-15 m, preferably 14m, and the device is divided into two sections, wherein the upper section is a fractionation section of 6m, and the lower section is a stripping section of 8 m; the wall thickness is 8-10 mm, preferably 8mm, the material is 304L stainless steel, and the first wire mesh filler 2054 and the second wire mesh filler 2056 are stainless steel; negative pressure of-0.1 MPa in vacuum state; the temperature of the top of the fractionating tower 205 is controlled at 190 ℃, and the temperature of the bottom of the fractionating tower is controlled at 230 ℃;
the flash column 208:
the diameter DN 1-3 m, preferably 2 m; a height of 3 m; the wall thickness is 8-10 mm, preferably 10mm, and the material is 304L stainless steel; negative pressure of-0.1 MPa in vacuum state; the falling film heater 207 is a square meter of 90 square meters and is made of 304L stainless steel; the butyl oleate condenser 2081 is a square meter of 60 square meters and is made of 304L stainless steel.
A process method for synthesizing butyl oleate and butyl palmitate based on the esterification device and the fractionation equipment,
esterification:
fractional distillation:
the method specifically comprises the following steps:
s1: selection of raw materials
Rice bran oil mixed fatty acid: acid value mgKOH/g: not less than 190
Iodine value gI2/100g：95-105
N-butanol: national standard, alcohol content ≧ 99.5
The catalyst is p-toluenesulfonic acid: sulfuric acid (H) with a content of more than or equal to 95%2SO4)％≤3
S2: stock preparation
a. Adding p-toluenesulfonic acid into the rice bran oil mixed fatty acid, uniformly stirring, pumping into a mixed acid storage tank 102 for later use, and keeping the temperature at 60 ℃;
b. n-butanol is kept in the butanol storage tank 112 for standby (normal temperature);
s3: feeding of the feedstock
a. Preheating the mixed fatty acid of rice bran oil with a mixed acid metering pump 103 at the uniform speed of 1000 kg per hour to 130 ℃ through a heat exchanger 104 and a mixed acid heater 105, and pumping the mixture into an esterification tower 106;
b. preheating n-butanol to 160 ℃ by a butanol heater 1112 at an even speed of 530 kg per hour by a butanol metering pump 1111, and pumping the n-butanol into the lower part of the esterification kettle 107 under the tower;
s4: esterification reaction
a. The mixed fatty acid of the rice bran oil is uniformly distributed on the surface of a corrugated filler 1064 through an acid mixing distributor 1063, and flows downwards along the surface of the corrugated filler 1064 under the action of gravity, n-butanol is pumped into the bottom in an esterification kettle in the tower through a butanol heater 1112 through a butanol metering pump 1111, liquid n-butanol is heated to 160 ℃ through the butanol heater 1112 to be in a vapor state, the vapor state n-butanol rises to enter the lower part of the esterification tower 106 and then rises along the corrugated filler 1064 in the esterification tower 106 to be contacted with the mixed fatty acid of the rice bran oil on the corrugated filler 1064 to carry out esterification reaction, wherein the reaction temperature is between 130 and 150 ℃ (the heat required by the esterification reaction is provided by two heaters 1065 in the tower), the crude ester generated by the reaction flows downwards along the surface of the corrugated filler 1064 to enter the esterification kettle 107 in the tower and is repeated continuously, and the redundant vapor state n-butanol and vapor state water are discharged from a, The alcohol-water separator 108, wherein the liquid butanol flows back to the butanol storage tank 112 to continuously participate in the esterification reaction, and the liquid water is discharged out of the device;
b. if the crude ester flowing into the esterification kettle 107 under the tower contains unreacted rice bran oil mixed fatty acid, the steam n-butanol and the rice bran oil mixed fatty acid are subjected to esterification reaction under the stirring of the stirring rod 1073, wherein the unreacted steam n-butanol rises to enter the esterification tower 106;
c. when the amount of the crude ester in the esterification kettle 107 under the tower reaches a certain amount and reaches the standard, pumping the crude ester into a first crude ester storage tank 114;
d. the esterification kettle under the tower 107 comprises 2, when the crude ester amount in the esterification kettle under the tower A in use reaches a certain amount (for example, 80 percent of the volume), the corresponding liquid pipe and butanol pipe are closed, the crude ester and the vaporous n-butanol stop entering the esterification kettle under the tower A, and the liquid pipe and butanol pipe of the esterification kettle B under the other tower are opened, the crude ester and the vaporous n-butanol enter the esterification kettle B under the tower, so that the automatic switching between the esterification kettle A under the tower and the esterification kettle B under the tower is realized (the check valve on the vapor pipe is a one-way valve, the vaporous butanol in the esterification kettle under the tower rises and enters the esterification tower through the check valve, but when the vaporous butanol stops rising, the check valve is also automatically closed, the vaporous butanol in the esterification tower cannot flow back to the esterification kettle under the tower, simultaneously the mixed acid content index of the crude ester in the esterification kettle A under the tower is detected, if the mixed acid content index reaches the standard, the crude ester is pumped into the first crude ester storage, at the moment, the esterification kettle A under the tower is emptied for standby and is continuously repeated; if the standard is not met, continuously introducing the vaporous n-butanol into the esterification kettle A under the tower, continuously carrying out the esterification reaction for 1-2 hours under stirring, and continuously carrying out the esterification reaction until the standard is met; (generally, each kettle works for about 8 hours, and the total time of the supplementary esterification of the esterification kettle 107 below the tower is not more than 3 hours)
S5: the crude ester in the first crude ester storage tank 114 is washed by clean water to remove the catalyst and then pumped into a second crude ester storage tank 202 for standby;
s6: fractional distillation
a. Pumping the crude ester in the second crude ester storage tank 202 into a fractionating tower 205 by a crude ester metering pump 203 at a uniform speed of 1200L per hour through a crude ester heater 204, controlling the temperature of the crude ester heater 204 at 210 ℃, and separating out vaporous butyl palmitate, liquid butyl oleate and plant asphalt;
b. the vaporous butyl palmitate rises upwards and enters a butyl palmitate condenser to be condensed into liquid, the liquid butyl palmitate flows out of the fractionating tower and then flows into a butyl palmitate receiver 2052, then the liquid butyl palmitate enters a butyl palmitate storage tank, the monomer purity is not less than 95 percent, and the liquid butyl oleate and the plant asphalt flow out of the lower part of the distillation tower;
c. the effluent liquid butyl oleate and the plant asphalt pass through a circulating pump 206 and a falling film heater 207 and then enter a flash tower 208; the falling film heater 207 controls the temperature to 240 ℃, the vacuum residual pressure of the flash tower 208 is less than 1 mm Hg, so that the liquid butyl oleate is vaporized,
the vaporous butyl oleate rises upwards and enters a butyl oleate condenser 2081 to be condensed into liquid, the liquid butyl oleate flows out of the flash tower 208 and then flows into a butyl oleate receiver, and then enters a butyl oleate storage tank 2083, and unvaporized plant asphalt flows out of the bottom of the tower and enters an asphalt storage tank 210.
d. Within the fractionator, the unvaporized liquid butyl palmitate passes down through a second wire mesh packing 2056, a butyl palmitate heater 2057, the butyl palmitate heater 2057 vaporizing the liquid butyl palmitate.
Further explaining the content index of mixed acid in S4, when the esterification rate is required to reach 99.5% (the acid value index of the product is less than 0.1), further supplementary esterification is needed, in general, the esterification rate of the crude ester flowing out from the bottom of the esterification tower 106 is about 99% and not less than 98.5%, and after refining, the crude ester meets the requirements of conventional products, and when the acid value index is less than 0.1, further supplementary esterification is needed, so that the esterification rate of the crude ester reaches about 99.5%.
The products obtained by the above process are shown in table 1 below;
TABLE 1
The butyl palmitate (about 15 percent), the butyl oleate (about 80 percent) and the plant asphalt are obtained by fractionating and cutting through a fractionating tower, the butyl palmitate and the butyl oleate are widely applied in the plastic industry and the lubricating oil industry, wherein the butyl oleate has light color and high purity, the flash point reaches over 180 ℃, the technical index of a lubricating oil additive is completely met, and the plant asphalt can be used as fuel or a casting binder.
In addition, the following tables 2 to 5 are used to respectively illustrate the influence of the mass ratio of the mixed fatty acid of rice bran oil and n-butanol on the esterification rate, the influence of the esterification temperature on the esterification rate, the influence of the catalyst dosage on the esterification rate, and the influence of the height of the esterification tower section on the esterification rate, so as to facilitate the realization of a better esterification reaction scheme.
Table 2: influence of mass ratio of mixed fatty acid of rice bran oil and butanol on esterification rate
Catalyst (based on the mass of the mixed acid): 0.5%, esterification temperature: 140 ℃, esterification column height: 15m
| Alcohol: acid(s) | 100:26.5 | 100:40 | 100:53 | 100:64 | 100:74 | 100:83 | 100:95 |
| Esterification rate% | 73.5 | 92.7 | 98.3 | 98.5 | 98.7 | 98.9 | 98.9 |
TABLE 2
Table 3: effect of esterification temperature on esterification Rate
Mixed acid: butanol 100:53, catalyst: 0.5%, esterification column height: 15m
| Esterification temperature C | 125 | 130 | 135 | 140 | 145 | 150 | 155 |
| Esterification rate% | 61.5 | 82.3 | 92.1 | 98.2 | 98.5 | 98.6 | 98.6 |
TABLE 3
Table 4: effect of catalyst amount on esterification Rate
Acid: alcohol 100:53, esterification temperature: 140 ℃, esterification column height: 15m
TABLE 4
Table 5: effect of esterification column height on esterification Rate
Acid mixing: alcohol 100:53, esterification temperature: 140 ℃, catalyst: 0.5 percent
TABLE 5
Claims (10)
1. An apparatus for fractionating mixed fatty acid butyl esters, characterized by: the device comprises a second crude ester storage tank, a crude ester metering pump, a crude ester heater and a fractionating tower which are sequentially communicated through a fractionating pipe, wherein the fractionating tower is connected with a vacuum pump, a butyl palmitate condenser, a butyl palmitate receiver, a first wire mesh filler, a crude ester distributor, a second wire mesh filler and a butyl palmitate heater are sequentially arranged in the fractionating tower from top to bottom, the crude ester distributor is communicated with the crude ester heater, the lower part of the fractionating tower is sequentially communicated with a circulating pump, a falling film heater and a flash tower through a flash evaporation pipe, a butyl oleate condenser, a butyl oleate receiver and a third wire mesh filler are sequentially arranged in the flash tower from top to bottom, and a communication port between the falling film heater and the flash tower is positioned below the third wire mesh filler.
2. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: the coarse ester distributor comprises a feeding main pipe and a plurality of branch pipes connected to two sides of the feeding main pipe, the feeding main pipe is communicated with the branch pipes, and the feeding main pipe and the branch pipes are provided with distribution holes.
3. An apparatus for fractionating mixed fatty acid butyl esters according to claim 2, wherein: the distribution holes comprise an upper distribution hole with an upward opening and a lower distribution hole with a downward opening.
4. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: the circulating pump is a water vapor injection circulating pump, and the lower part of the flash tower is communicated with the circulating pump through a vapor recovery pipe.
5. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: the tube pass of the falling film heater is communicated with the flash evaporation tube, and heat conducting oil is arranged in the shell pass of the falling film heater.
6. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: butyl palmitate receiver, butyl oleate receiver all include the receiving disc, wear to establish on the receiving disc and be connected with the siphunculus, and the upper portion lateral wall of siphunculus is opened has the steam inlet, is connected with the block lid in the upper end of siphunculus, is equipped with the retaining ring that upwards extends at the upper periphery department of receiving disc, and it has a blown down tank to open in retaining ring department.
7. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1 or 6, characterized in that: the butyl palmitate receiver is connected with a butyl palmitate storage tank, and the butyl oleate receiver is connected with a butyl oleate storage tank.
8. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: and a residue outlet is formed at the bottom of the flash tower and is connected with an asphalt storage tank.
9. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: and heat conducting oil is arranged on the side wall of the crude ester heater.
10. An apparatus for fractionating mixed fatty acid butyl esters according to claim 1, wherein: the butyl palmitate heater is a heat-conducting oil heating coil.
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