Ethyl 2-ethylhexanoate

Colorless clear liquid; fresh orris, fruity, herbal, cumin aroma.

Ethyl 2-ethylhexanoate is a fatty acid ester.

use chart 2 shown in a tubular reactor and tower type reactor containing a continuous flow reaction device for ester-interchange reaction. Will use with synthetic example 5 the method for manufacturing the same 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) composition of the second tin high (of the above-mentioned composition (active ingredient contains a) tin atom concentration: 2.76mol/kg) via the supply line 33 to possess used for heating of the water purifier and SUS316 systems catalyst pot 230 adding about 20 kg. Then via the supply line 21 to the raw material tank 210 by adding 2-ethyl hexanoic acid 3-methyl-butyl, via the supply line 22 to the raw material tank 220 by adding 2-methyl propane acid ethyl ester. The tank and piping, etc., in order to maintain fluidity, heat tracing of steam. The 2-ethyl hexanoic acid 3-methyl-n-butyl via transporting the pipeline 23, embedded mixer 241 and the conveying pipeline 25 to about 12 kg/H the flow rate of the slit of the tubular reactor used for heating 240 in, the 2-methyl propane acid ethyl ester via transporting the pipeline 24, embedded mixer 241 and the conveying pipeline 25 to about 10 kg/H the flow rate of the slit of the tubular reactor used for heating 240 in. On the other hand, for the catalyst pot 230, in order to maintain the fluidity of the content, using steam for heating, in this state, the 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) b tin high via the conveying pipeline composition 34, embedded mixer 241, conveying pipeline 25 to 0.9 kg/H to give liquid. In embedding the mixer 241 will be in the 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) b tin composition high, 2-ethyl hexanoic acid 3-methyl-n-butyl and 2-methyl propane acid ethyl ester mixing and heating. The 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) as a catalyst the second tin high, the tubular reactor to the slit 240 in the 2-ethyl hexanoic acid 3-methyl-n-butyl and 2-methyl propane acid ethyl ester exchange reaction occurs, by the conveying pipeline 26 to the stream of the tower reactor 250 in, to carry out further reaction. With 30 mesh SUS316 level of the inner diameter of 130 mm, effective length 4500 mm tower type reactor 250 with the heating heater, reboiler 253 and the liquid-feeding pump, the heater and a reboiler in the reactor 253 control at about 160 °C. In tower reactor 250 by an ester exchange reaction to the upper portion of the generating comprising 2-propionic acid 3-methyl-n-butyl and the unreacted 2-methyl propane acid ethyl ester using the fraction condenser 251 to condense, via condensate tank 252 by the recovery pipe line 27 for recycling. Comprising the reaction product to 2-ethyl hexanoic acid ethyl ester and unreacted 2-ethyl hexanoic acid 3-methyl-butyl mixture from the tower reactor 250 via the conveying pipeline the lower part of the 28 is set as the temperature of the stream 180 °C, pressure about 30kPaA of the state of thin film evaporation device 260 in, via the delivery pipeline 29 will include 2-ethyl hexanoic acid ethyl ester with unreacted 2-ethyl hexanoic acid 3-methyl-butyl low boiling point into a dispensing onto the distillation tower 270 (inside diameter 83 mm, effective length 2800 mm, filled with filler MetalGauzeCY the distilling tower) in, to purify. On the other hand, comprises 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) composition of the second tin high via the delivery line of the high-boiling-point component 30 stream to the catalyst pot 230 in, via the delivery line 34, the embedded mixer 241, conveying pipeline 25 in the continuous circulation of the reaction device. Before reach a steady state inside the reactor, according to the need to reduce or interrupt from stock tank and catalyst pot the supply of to the tubular reactor. To continue to operate, after the reach a steady state in the reactor, from the tower type reactor 250 bottom collecting mixture, quantitative analysis by gas chromatography, as a result 2-ethyl hexanoic acid in the yield of ethyl 2-ethyl hexanoic acid 3-methyl-n-butyl reference count 35.1percent. Continuing the state about 15 days, once again from the tower type reactor 250 bottom collecting mixture, quantitative analysis by gas chromatography, as a result 2-ethyl hexanoic acid 2-ethyl ester in the yield of 34.1percent.use chart 2 shown in a tubular reactor and tower type reactor containing a continuous flow reaction device for ester-interchange reaction. Will use with synthetic example 5 the method for manufacturing the same 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) composition of the second tin high (of the above-mentioned composition (active ingredient contains a) tin atom concentration: 2.76mol/kg) via the supply line 33 to possess used for heating of the water purifier and SUS316 systems catalyst pot 230 adding about 20 kg. Then via the supply line 21 to the raw material tank 210 by adding 2-ethyl hexanoic acid 3-methyl-butyl, via the supply line 22 to the raw material tank 220 by adding 2-methyl propane acid ethyl ester. The tank and piping, etc., in order to maintain fluidity, heat tracing of steam. The 2-ethyl hexanoic acid 3-methyl-n-butyl via transporting the pipeline 23, embedded mixer 241 and the conveying pipeline 25 to about 12 kg/H the flow rate of the slit of the tubular reactor used for heating 240 in, the 2-methyl propane acid ethyl ester via transporting the pipeline 24, embedded mixer 241 and the conveying pipeline 25 to about 10 kg/H the flow rate of the slit of the tubular reactor used for heating 240 in. On the other hand, for the catalyst pot 230, in order to maintain the fluidity of the content, using steam for heating, in this state, the 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) b tin high via the conveying pipeline composition 34, embedded mixer 241, conveying pipeline 25 to 0.9 kg/H to give liquid. In embedding the mixer 241 will be in the 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) b tin composition high, 2-ethyl hexanoic acid 3-methyl-n-butyl and 2-methyl propane acid ethyl ester mixing and heating. The 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) as a catalyst the second tin high, the tubular reactor to the slit 240 in the 2-ethyl hexanoic acid 3-methyl-n-butyl and 2-methyl propane acid ethyl ester exchange reaction occurs, by the conveying pipeline 26 to the stream of the tower reactor 250 in, to carry out further reaction. With 30 mesh SUS316 level of the inner diameter of 130 mm, effective length 4500 mm tower type reactor 250 with the heating heater, reboiler 253 and the liquid-feeding pump, the heater and a reboiler in the reactor 253 control at about 160 °C. In tower reactor 250 by an ester exchange reaction to the upper portion of the generating comprising 2-propionic acid 3-methyl-n-butyl and the unreacted 2-methyl propane acid ethyl ester using the fraction condenser 251 to condense, via condensate tank 252 by the recovery pipe line 27 for recycling. Comprising the reaction product to 2-ethyl hexanoic acid ethyl ester and unreacted 2-ethyl hexanoic acid 3-methyl-butyl mixture from the tower reactor 250 via the conveying pipeline the lower part of the 28 is set as the temperature of the stream 180 °C, pressure about 30kPaA of the state of thin film evaporation device 260 in, via the delivery pipeline 29 will include 2-ethyl hexanoic acid ethyl ester with unreacted 2-ethyl hexanoic acid 3-methyl-butyl low boiling point into a dispensing onto the distillation tower 270 (inside diameter 83 mm, effective length 2800 mm, filled with filler MetalGauzeCY the distilling tower) in, to purify. On the other hand, comprises 1, 1, 3, 3-tetra (3-methyl-butyl) - 1, 3-bis (3-methyl-butoxy) composition of the second tin high via the delivery line of the high-boiling-point component 30 stream to the catalyst pot 230 in, via the delivery line 34, the embedded mixer 241, conveying pipeline 25 in the continuous circulation of the reaction device. Before reach a steady state inside the reactor, according to the need to reduce or interrupt from stock tank and catalyst pot the supply of to the tubular reactor. To continue to operate, after the reach a steady state in the reactor, from the tower type reactor 250 bottom collecting mixture, quantitative analysis by gas chromatography, as a result 2-ethyl hexanoic acid in the yield of ethyl 2-ethyl hexanoic acid 3-methyl-n-butyl reference count 35.1percent. Continuing the state about 15 days, once again from the tower type reactor 250 bottom collecting mixture, quantitative analysis by gas chromatography, as a result 2-ethyl hexanoic acid 2-ethyl ester in the yield of 34.1percent.

< 25,000 lb

Molecular Weight:172.26
XLogP3:3.3
Hydrogen Bond Acceptor Count:2
Rotatable Bond Count:7
Exact Mass:172.146329876
Monoisotopic Mass:172.146329876
Topological Polar Surface Area:26.3
Heavy Atom Count:12
Complexity:121
Undefined Atom Stereocenter Count:1
Covalently-Bonded Unit Count:1
Compound Is Canonicalized:Yes