CN101973846A - Method for producing mixed butanol and coarse octanol by using waste liquid discharged from octanol device as raw material - Google Patents
Method for producing mixed butanol and coarse octanol by using waste liquid discharged from octanol device as raw material Download PDFInfo
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- CN101973846A CN101973846A CN2010105301098A CN201010530109A CN101973846A CN 101973846 A CN101973846 A CN 101973846A CN 2010105301098 A CN2010105301098 A CN 2010105301098A CN 201010530109 A CN201010530109 A CN 201010530109A CN 101973846 A CN101973846 A CN 101973846A
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Abstract
The invention discloses a method for producing mixed butanol and coarse octanol by using waste liquid discharged from an octanol device as a raw material, which belongs to a method for preparing acyclic monohydric alcohols, and is characterized by using a raw material fractionation unit, a hydrogenation synthesis unit and a product distillation unit, wherein the raw material fractionation unit comprises three fractionation devices: a butyraldehyde fractionation tower, a butanol fractionation tower and a C8 fractionation tower; the hydrogenation synthesis unit and the product distillation unit are suitable for hydrogenating and distilling a butyraldehyde fraction and a C8 fraction from the raw material fractionation unit alternately; and the product distillation unit comprises a light component removing tower device and a heavy component removing tower device. The method for producing the mixed butanol and coarse octanol by using the waste liquid discharged from the octanol device as the raw material, which is energy-saving and environmentally-friendly, can realize the recycling of the waste liquid discharged from the octanol device, reduce the waste water treatment cost of the octanol device and improves the technical indexes of treated water.
Description
Technical field
The present invention is that a kind of waste liquid with the butyl octanol unit discharging is the method for raw material production mixed butyl alcohol and thick octanol.The preparation method who belongs to monohydroxylic acyclic alcohols.The recycling that is particularly related to the waste liquid of butyl octanol unit discharging is handled.
Background technology
Fourth octanol low pressure carbonylic synthesis technology is that propylene is in the presence of rhodium phosphine complex catalyst, with synthetic gas (CO+H
2) reaction generation butyraldehyde-n and isobutyric aldehyde.Condensation reaction takes place and generates octenal through with after isobutyric aldehyde separates in butyraldehyde-n under the catalysis of sodium hydroxide solution, octenal hydrogenation under the effect of copper catalyst generates octanol (being 2-Ethylhexyl Alcohol); Not separated butyraldehyde-n and the direct hydrogenating reduction of mixture of isobutyraldehyde then generate propyl carbinol and isopropylcarbinol.
In a kind of waste liquid of production equipment discharging of fourth octanol, contain positive isobutyric aldehyde 3%-20%, positive isopropylcarbinol 10%-40%, C
5-C
7Contain 1%-5%, C
810%-40%, C
12-C
16Contain 15%-60%, water 0.5%-10% is valuable available stock.But because the component complexity, to its processing, the comprehensive utilization technique difficulty is bigger, and present treatment process mainly is directly discharging or only makes burning disposal, has promptly wasted the energy, has polluted environment and water source again.Waste liquid with the butyl octanol unit discharging is raw material production mixed butyl alcohol and octanol, and its technology of carrying out the recycling treatment utilization is not also seen as yet.
Summary of the invention
The objective of the invention is to avoid above-mentioned weak point of the prior art, is the method for raw material production mixed butyl alcohol and thick octanol and provide a kind of both save energy to protect the waste liquid with the butyl octanol unit discharging of environment.
The present invention also aims to by recycling, alleviate the load with the supporting Waste Water Treatment of butyl octanol unit greatly, reduce cost for wastewater treatment, improve the water-quality guideline after handling the waste liquid of butyl octanol unit discharging.
Purpose of the present invention can reach by following measure:
The present invention is to be the method for raw material production mixed butyl alcohol and thick octanol with the waste liquid that butyl octanol unit discharges, it is characterized in that by the raw material fractionation unit, hydrogenation synthesis unit and product rectification cell are formed, described raw material fractionation unit comprises butyraldehyde separation column, butanols separation column and carbon eight separation columns three cover fractionation plants, described hydrogenation synthesis unit and product rectification cell are applicable to hydrogenation and the rectifying from the butyraldehyde cut of raw material fractionation unit, also be applicable to from the hydrogenation and the rectifying of carbon eight cuts of raw material fractionation unit, intermittently use for the two; Described product rectification cell comprises that taking off light rectifying tower device weighs the rectifying tower device with taking off.
The raw material fractionation unit of the combination of the present inventor design, hydrogenation synthesis unit and product rectification cell device for the processing and the utilization of the waste liquid of butyl octanol unit discharging provides technical support, have been made outstanding contributions for finishing task of the present invention.
Waste liquid with the butyl octanol unit discharging of the present invention is the method for raw material production mixed butyl alcohol and thick octanol, it is characterized in that comprising following operation steps:
A. raw material fractionation
The waste liquid of butyl octanol unit discharging is at first by the butyraldehyde fractionation plant, the butyraldehyde component that wherein contains is come out from the fractionation of butyraldehyde cat head, then, by butanols separation column device, the butanols component that wherein contains is come out from the fractionation of butanols cat head, at last, by carbon eight separation column devices, carbon eight component octenals and the octanol that wherein contains come out from carbon eight cat head fractionation; The butyraldehyde that fractionation is come out is stored in the butyraldehyde storage tank, and the butanols that fractionation is come out is stored in carbon four storage tanks, and octenal and octanol are stored in carbon eight storage tanks;
B. hydrogenation is synthetic
Enter the hydrogenation synthesis unit from the butyraldehyde cut of step a butyraldehyde storage tank or from the octenal and the octanol cut of carbon eight storage tanks, in hydrogenator, by synthetic mixed butyl alcohol of hydrogenation or synthetic thick octanol;
C. product purification
The butanols cut that step a fractionation is come out and through step b hydrogenation synthetic mixed butyl alcohol or thick octanol through rectified purified, mixed butyl alcohol quality percentage composition 〉=95% that makes respectively; Thick octanol quality percentage composition 〉=97% that makes.
Waste liquid with the butyl octanol unit discharging of the present invention is the method for raw material production mixed butyl alcohol and thick octanol, it is characterized in that the process conditions of described operation steps is as follows:
A. raw material fractionation
1.. each constituent mass per-cent of waste liquid of butyl octanol unit discharging: positive isobutyric aldehyde 3%-20%, positive isopropylcarbinol 10%-40%, C
5-C
7Contain 1%-5%, carbon eight component 10%-40%, C
12-C
1615%-60%, water 0.5%-10%;
2.. the operational condition of butyraldehyde tower: 60 ℃-85 ℃ of tower top temperatures, 110 ℃-150 ℃ of column bottom temperatures;
3.. the operational condition of butanols tower: 85 ℃-120 ℃ of tower top temperatures, 150 ℃-175 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa;
4.. the operational condition of carbon eight towers: 120 ℃-150 ℃ of tower top temperatures, 175 ℃-195 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa.
B. hydrogenation is synthetic
1. the operational condition in the mixed butyl alcohol hydrogenator is: the reaction hot(test)-spot temperature is at 110 ℃-200 ℃, and reaction pressure is at 0.35Mpa-0.5Mpa;
The operational condition of 2. producing in the thick octanol hydrogenator is: the reaction hot(test)-spot temperature is at 140 ℃-200 ℃, and reaction pressure is at 0.35Mpa-0.5Mpa.
C. product purification
1.. the operational condition of lightness-removing column is when producing mixed butyl alcohol: 78 ℃-90 ℃ of tower top temperatures, 110 ℃-130 ℃ of column bottom temperatures, the operational condition of weight-removing column is: 100 ℃-125 ℃ of tower top temperatures, 150 ℃-180 ℃ of column bottom temperatures;
2.. the operational condition of lightness-removing column is when producing thick octanol: 85 ℃-100 ℃ of tower top temperatures, 125 ℃-135 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa, the operational condition of weight-removing column is: 105 ℃-125 ℃ of tower top temperatures, 160 ℃-180 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa.
Step b hydrogenation synthetic mixed butyl alcohol or thick octanol be through rectified purified, mixed butyl alcohol quality percentage composition 〉=95% that makes; Thick octanol quality percentage composition 〉=97% that makes.
The present invention is that the waste liquid with butyl octanol unit discharging is the disclosed technical scheme of method of raw material production mixed butyl alcohol and thick octanol, and following positively effect is arranged compared to existing technology:
1. a kind of not only save energy being provided but also having protected the waste liquid with the butyl octanol unit discharging of environment is the method for raw material production mixed butyl alcohol and thick octanol.
2. by recycling for the waste liquid of butyl octanol unit discharging, alleviate the load with the supporting Waste Water Treatment of butyl octanol unit greatly, reduce cost for wastewater treatment, improve the water-quality guideline after handling.
3. the waste liquid with the butyl octanol unit discharging is raw material production mixed butyl alcohol and thick octanol Industrial products, turns waste into wealth, and increases economic benefit of enterprises.
4. this processing unit is simple, and processing cost is low, pollutes few.
Description of drawings
Fig. 1 is the raw material separating unit process flow diagram that the waste liquid with the butyl octanol unit discharging of the present invention is the method for raw material production mixed butyl alcohol and thick octanol
Fig. 2 is the hydrogenation synthesis unit process flow diagram that the waste liquid with the butyl octanol unit discharging of the present invention is the method for raw material production mixed butyl alcohol and thick octanol
Fig. 3 is the product rectification cell process flow diagram that the waste liquid with the butyl octanol unit discharging of the present invention is the method for raw material production mixed butyl alcohol and thick octanol
Embodiment
The present invention will now be further detailed embodiment:
Embodiment 1
A. raw material fractionation
The waste liquid of butyl octanol unit discharging is at first by the butyraldehyde fractionation plant, the butyraldehyde component that wherein contains is come out from the fractionation of butyraldehyde cat head, then, by butanols separation column device, the butanols component that wherein contains is come out from the fractionation of butanols cat head, at last, by carbon eight separation column devices, carbon eight component octenals and the octanol that wherein contains come out from carbon eight cat head fractionation; The butyraldehyde that fractionation is come out is stored in the butyraldehyde storage tank, and the butanols that fractionation is come out is stored in carbon four storage tanks, and octenal and octanol are stored in carbon eight storage tanks;
B. hydrogenation is synthetic
Enter the hydrogenation synthesis unit from the butyraldehyde cut of step a butyraldehyde storage tank or from the octenal and the octanol cut of carbon eight storage tanks, in hydrogenator, by synthetic mixed butyl alcohol of hydrogenation or synthetic thick octanol;
C. product purification
The butanols cut that step a fractionation is come out and through step b hydrogenation synthetic mixed butyl alcohol or thick octanol through rectified purified, mixed butyl alcohol quality percentage composition 〉=95% that makes respectively; Thick octanol quality percentage composition 〉=97% that makes.
In conjunction with Fig. 1 raw material fractionation unit of the present invention is elaborated
The butanol and octanol waste liquid raw material is heated to 100 ℃-120 ℃ through feed preheater E-101 and enters butyraldehyde tower C-101, the heat that the material evaporation needs in the tower, E-103 provides by tower still reboiler, 110 ℃-150 ℃ of tower still service temperatures, the butyraldehyde tower is an atmospheric operation, keeps tower top temperature to be stabilized in 60 ℃-85 ℃; Cat head rising steam enters among the butyraldehyde tower return tank V-108 after overhead condenser E-102 condensation cooling, and P-101A/B partly returns stream through butyraldehyde tower backflow extraction pump, and part extraction butyraldehyde cut enters the butanols storage tank;
Butyraldehyde tower tower bottoms extraction pump P-102A/B at the bottom of tower sends into butanols tower C-104 middle part opening for feed, the heat that the material evaporation needs in the tower, and E-115 provides by tower still reboiler, 150 ℃-175 ℃ of tower still service temperatures.The butanols tower is a negative-pressure operation, and the vacuum of tower is provided by vapor jet pump J-101, and tower top pressure is-0.05Mpa--0.1Mpa.Keep tower top temperature to be stabilized in 85 ℃-120 ℃; Cat head rising steam enters among the butanols tower return tank V-101 after overhead condenser E-114 condensation cooling, partly returns stream through backflow extraction pump P-112A/B then, and part extraction butanols cut enters carbon four storage tanks;
At the bottom of the tower of butanols tower liquid by tower at the bottom of extraction pump P-113A/B, send into falling-film evaporator E-108.By regulating the heating steam amount control of E-108, make knockout drum V-104 material temperature remain on 140 ℃-160 ℃; Material is the membranaceous heating tube internal surface that flows through fast and absorbs heat, gasify than light constituent, enter knockout drum V-104 and realize gas-liquid separation, high boiling point trimer and heavier component are discharged at the bottom of jar by P-109A/B as the still raffinate, reach and take off the purpose of heavily guaranteeing follow-up rectifying normal running.
The evaporation gas phase of V-104 enters carbon eight tower C-102 middle part opening for feed.The rising vapor portion of this tower is from gas-phase feed, and part is provided by tower still reboiler E-105, and 175 ℃-195 ℃ of tower still service temperatures are controlled by the heating steam amount.Carbon eight towers are negative-pressure operation, and the vacuum of tower is provided by vapor jet pump J-102.Cat head working pressure-0.05Mpa--0.1Mpa.Keep tower top temperature to be stabilized in 120 ℃-150 ℃, cat head rising steam enters among the return tank V-102 after overhead condenser E-104 condensation cooling, partly returns stream through backflow extraction pump P-104A/B then, part extraction octenal cut and octanol cut enter carbon eight storage tanks;
In conjunction with Fig. 2 hydrogenation synthesis unit of the present invention is elaborated:
Technical process explanation when 1. producing mixed butyl alcohol
Carbon four components from the butyraldehyde storage tank, after feed preheater E-601 preheating, be sent to vaporizer T601 earlier, entered in the reaction cycle gas by gasification after the circulation gas counter current contact that carbon four components and compressor C601 come, at the vaporized material of vaporizer T601, be superheated to 110 ℃-160 ℃ through feed heater E602, enter reactor R601, carbon four components and hydrogen reaction are converted into mixed butyl alcohol in reactor, reactor is a fixed-bed shell-and-tube reactor, in adorn commercially available OXO-01 catalyzer, 110 ℃-200 ℃ of hot(test)-spot temperatures of reaction, reaction pressure 0.35Mpa-0.5Mpa.
Material from reactor R601 comes out is cooled off by hydrogenation circulation gas in hydrogenation heat exchanger E603 earlier, is cooled to 30 ℃-60 ℃ at last in hydrogenation condenser E604, and the gas phase mixed butyl alcohol is condensed into liquid phase, and mixed butyl alcohol separates with circulation gas in separating tank F602.The mixed butyl alcohol of separating tank F602 bottom is delivered to rectifying workshop section.
Technical process explanation when 2. producing thick octanol
From carbon eight components of carbon eight storage tanks after feed preheater E-601 preheating, be sent to vaporizer T601 earlier, entered in the reaction cycle gas by gasification after the circulation gas counter current contact that carbon eight components and compressor C601 come, at the vaporized material of vaporizer T601, be superheated to 150 ℃-170 ℃ through feed heater E602, enter reactor R601, carbon eight components and hydrogen reaction are converted into thick octanol in reactor, reactor is a fixed-bed shell-and-tube reactor, in adorn commercially available OXO-01 catalyzer, 140 ℃-200 ℃ of reaction hot(test)-spot temperatures, reaction pressure 0.35Mpa-0.5Mpa.
Material from reactor R601 comes out is cooled off by hydrogenation circulation gas in hydrogenation heat exchanger E603 earlier, is cooled to 30 ℃-60 ℃ at last in hydrogenation condenser E604, and the thick octanol of gas phase is condensed into liquid phase, and thick octanol separates with circulation gas in separating tank F602.The thick octanol of separating tank F602 bottom is delivered to rectifying workshop section.
In conjunction with Fig. 3 product rectification cell of the present invention is elaborated
The mixed butyl alcohol that F602 comes (thick octanol) carries out rectifying at lightness-removing column T602 and weight-removing column T603, and the light constituent in the mixed butyl alcohol (thick octanol) removes from the cat head extraction of lightness-removing column, and heavy constituent extraction at the bottom of the tower of weight-removing column removes.T602 and T603 are negative pressure tower when producing thick octanol.
1.. technical process explanation when producing mixed butyl alcohol
Pre-rectifying tower T602
From the fractionation mixed butyl alcohol of carbon four storage tanks with from the crude product mixed butyl alcohol of hydrogenation synthesis unit, under self pressure, enter lightness-removing column T602, this tower comprises a tower still reboiler E605 and an overhead condenser E606.Tower still reboiler E605 is heated by low-pressure steam, provides lightness-removing column required heat, 110 ℃-130 ℃ of column bottom temperatures, and 78 ℃-90 ℃ of tower top temperatures, cat head rising gas phase is collected in the return tank F603 after overhead condenser E606 condensation.After material among the return tank F603 is pressurizeed by backflow extraction pump P605, part material turns back to lightness-removing column T602 top as phegma, the extraction of sub-fraction material removes the light constituent in the mixed butyl alcohol, is cooled to 30 ℃-60 ℃ through the cat head water cooler and delivers to light component jar.The bottoms material is delivered to weight-removing column T603 by column bottoms pump P604A/B and is further handled.
Weight-removing column T603
The effect of weight-removing column T603 is to obtain the product mixed butyl alcohol, and removes the heavy constituent in the product.This equipment comprises a reboiler E607 and condenser E608.Reboiler E607 is heated by low-pressure steam, provides weight-removing column required heat, 150 ℃-180 ℃ of column bottom temperatures, and 100 ℃-125 ℃ of tower top temperatures, the cat head material is collected in behind overhead condensation among the return tank F604.Material among the return tank F604 is by reflux pump P607A/B pressurization, and a part is returned weight-removing column T603 cat head as backflow, and another part is delivered to the mixed butyl alcohol jar.Heavy constituent at the bottom of the weight-removing column tower are delivered to the heavy component jar by column bottoms pump P606A/B.
Mixed butyl alcohol quality percentage composition 〉=95% that makes.
2.. technical process explanation when producing thick octanol
Pre-rectifying tower T602
From the thick octanol of crude product mixed butyl alcohol of hydrogenation synthesis unit, under self pressure, enter lightness-removing column T602, this tower comprises a tower still reboiler E605 and an overhead condenser E606.Tower still reboiler E605 is heated by low-pressure steam, provides lightness-removing column required heat, 125 ℃-135 ℃ of column bottom temperatures, 85 ℃-100 ℃ of tower top temperatures, tower top pressure is-0.05Mpa--0.1Mpa that cat head rising gas phase is collected in the return tank F603 after overhead condenser E606 condensation.After material among the return tank F603 is pressurizeed by backflow extraction pump P605, part material turns back to lightness-removing column T602 top as phegma, the extraction of sub-fraction material removes the light constituent in the thick octanol, is cooled to 30 ℃-60 ℃ through the cat head water cooler and delivers to light component jar.The bottoms material is delivered to weight-removing column T603 by column bottoms pump P604A/B and is further handled.
Weight-removing column T603
The effect of weight-removing column T603 is to obtain the thick octanol of product, and removes the heavy constituent in the product.This equipment comprises a reboiler E607 and condenser E608.Reboiler E607 is heated by low-pressure steam, provides weight-removing column required heat, 160 ℃-180 ℃ of column bottom temperatures, and 105 ℃-125 ℃ of tower top temperatures, tower top pressure is-0.05Mpa--0.1Mpa that the cat head material is collected in behind overhead condensation among the return tank F604.Material among the return tank F604 is by reflux pump P607A/B pressurization, and a part is returned weight-removing column T603 cat head as backflow, and another part is delivered to thick octanol jar.Heavy constituent at the bottom of the weight-removing column tower are delivered to the heavy component jar by column bottoms pump P606A/B.
Thick octanol quality percentage composition 〉=97% that makes.
Claims (3)
1. the waste liquid with the butyl octanol unit discharging is the method for raw material production mixed butyl alcohol and thick octanol, it is characterized in that by the raw material fractionation unit, hydrogenation synthesis unit and product rectification cell are formed, described raw material fractionation unit comprises butyraldehyde separation column, butanols separation column and carbon eight separation columns three cover fractionation plants, described hydrogenation synthesis unit and product rectification cell are applicable to hydrogenation and the rectifying from the butyraldehyde cut of raw material fractionation unit, also be applicable to from the hydrogenation and the rectifying of carbon eight cuts of raw material fractionation unit, intermittently use for the two; Described product rectification cell comprises that taking off light rectifying tower device weighs the rectifying tower device with taking off.
2. the waste liquid with the butyl octanol unit discharging according to claim 1 is the method for raw material production mixed butyl alcohol and thick octanol, it is characterized in that comprising following operation steps:
A. raw material fractionation
The waste liquid of butyl octanol unit discharging is at first by the butyraldehyde fractionation plant, the butyraldehyde component that wherein contains is come out from the fractionation of butyraldehyde cat head, then, by butanols separation column device, the butanols component that wherein contains is come out from the fractionation of butanols cat head, at last, by carbon eight separation column devices, carbon eight component octenals and the octanol that wherein contains come out from carbon eight cat head fractionation; The butyraldehyde that fractionation is come out is stored in the butyraldehyde storage tank, and the butanols that fractionation is come out is stored in carbon four storage tanks, and octenal and octanol are stored in carbon eight storage tanks;
B. hydrogenation is synthetic
Enter the hydrogenation synthesis unit from the butyraldehyde cut of step a butyraldehyde storage tank or from the octenal and the octanol cut of carbon eight storage tanks, in hydrogenator, by synthetic mixed butyl alcohol of hydrogenation or synthetic thick octanol;
C. product purification
The butanols cut that step a fractionation is come out and through step b hydrogenation synthetic mixed butyl alcohol or thick octanol through rectified purified, mixed butyl alcohol quality percentage composition 〉=95% that makes respectively; Thick octanol quality percentage composition 〉=97% that makes.
3. the waste liquid with the butyl octanol unit discharging according to claim 1 is the method for raw material production mixed butyl alcohol and thick octanol, it is characterized in that the process conditions of described operation steps is as follows:
A. raw material fractionation
1.. each constituent mass per-cent of waste liquid of butyl octanol unit discharging: positive isobutyric aldehyde 3%-20%, positive isopropylcarbinol 10%-40%, C
5-C
7Contain 1%-5%, carbon eight component 10%-40%, C
12-C
1615%-60%, water 0.5%-10%;
2.. the operational condition of butyraldehyde tower: 60 ℃-85 ℃ of tower top temperatures, 110 ℃-150 ℃ of column bottom temperatures;
3.. the operational condition of butanols tower: 85 ℃-120 ℃ of tower top temperatures, 150 ℃-175 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa;
4.. the operational condition of carbon eight towers: 120 ℃-150 ℃ of tower top temperatures, 175 ℃-195 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa.
B. hydrogenation is synthetic
1. the operational condition in the mixed butyl alcohol hydrogenator is: the reaction hot(test)-spot temperature is at 110 ℃-200 ℃, and reaction pressure is at 0.35Mpa-0.5Mpa;
The operational condition of 2. producing in the thick octanol hydrogenator is: the reaction hot(test)-spot temperature is at 140 ℃-200 ℃, and reaction pressure is at 0.35Mpa-0.5Mpa.
C. product purification
1.. the operational condition of lightness-removing column is when producing mixed butyl alcohol: 78 ℃-90 ℃ of tower top temperatures, 110 ℃-130 ℃ of column bottom temperatures, the operational condition of weight-removing column is: 100 ℃-125 ℃ of tower top temperatures, 150 ℃-180 ℃ of column bottom temperatures;
2.. the operational condition of lightness-removing column is when producing thick octanol: 85 ℃-100 ℃ of tower top temperatures, 125 ℃-135 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa, the operational condition of weight-removing column is: 105 ℃-125 ℃ of tower top temperatures, 160 ℃-180 ℃ of column bottom temperatures, tower top pressure is-0.05Mpa--0.1Mpa.
Step b hydrogenation synthetic mixed butyl alcohol or thick octanol be through rectified purified, mixed butyl alcohol quality percentage composition 〉=95% that makes; Thick octanol quality percentage composition 〉=97% that makes.
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| CN2010105301098A CN101973846B (en) | 2010-11-03 | 2010-11-03 | Method for producing mixed butanol and coarse octanol by using waste liquid discharged from octanol device as raw material |
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