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Journal Of Economics, Technology, and Business (JETBIS)

Volume 2, Number 11 November 2023

Indonesia, ethanol has a high octane value and can be obtained through the fermentation

process by distillation process. The process usually uses fungi, yeast, or bacteria that have a

high enough selectivity to produce ethanol (Dhaniswara et al., 2016).

8.5 percent by weight) or as fuel with an ethanol concentration of at least 92.5-93.8 percent by

weight or food grade ethanol which in addition to its relatively high ethanol content also does

not contain impurities such as fuel oil, vinegar acid, acetaldehyde, and others which are by-

products of fermentation. To produce products with a high enough ethanol concentration, a

separation process is needed. Generally, the separation process used is using a distillation

process (Greetham et al., 2020).

The distillation process is a process of separating mixtures based on their boiling point

and relative volatility. Substances with high relative volatility will rise upwards and will be

condensed to obtain distillate, while those that fail to evaporate will be taken as residues.

Distillation usually uses two stages, namely evaporating and condensing without reflux and the

When a liquid mixture of two components is heated, the steam that comes out will contain

more volatile components that are greater than the liquid in the boiler. Conversely, when steam

is cooled, materials with higher boiling points tend to condense more easily than components

with lower boiling points (Parhi et al., 2019).

The distillation process can be divided into two types: batch distillation and continuous

distillation. This batch distillation is widely used in pharmaceuticals, essential oils, and some

petroleum products. In the batch distillation column, the feed is first poured into the boiler and

no more ingredients are added until the end of the process. The difference that stands out from

these two distillation processes is that the material for continuous distillation, the feed is flowed

into the column continuously and thus makes the process in steady state condition. For batch

combustion engines (Soputra et al., 2015).

In this study, ethanol purification will be carried out using batch distillation directly from

the fermentation mash and new process optimization will be carried out to get answers to how

much purity is produced by batch distillation and how much energy efficiency can be done

(Suharto et al., 2020).

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chromatograph) tool to obtain content composition data from the mash fermenter, which later

the data obtained is later used to be tested on ASPEN plus software (Wibowo et al., 2018).

In research, in particular simulation, to approach simulation conditions with field

conditions it is necessary to select the most accurate thermodynamic model. In modeling the

ethanol purification system from the fermenter mash, the selection of thermodynamic models

For the selection of a proper thermodynamic model in this simulation, it is considered

that the distillation system operates at absolute pressure and is ideal in Peng-robinson's

thermodynamic model (Sodeifian et al., 2021).

In researching the distillation of batch mash fermenters, a predestinate distillate scenario

model was made using Aspen Plus software. The model consists of a feed, a distillation batch

tower, and a condenser. The purpose of predestinate distillate is to get the best ethanol results

in the component separation process. Based on the results obtained, economic calculations

were carried out in terms of energy consumption, distillation duration, and price for ethanol

obtained (Asadollahzadeh et al., 2017).

This simulation uses the Peng-Robinson thermodynamic model because the feed used in

the system in this study is the result of fermentation, which has a fairly diverse component

content and is usually distinguished based on the boiling point of the components.

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Based on the results above, the decrease in isoamyl mass flow and water contained in B2

distillate compared to the results of B1 distillate is quite high, isoamyl mass flow from 5621.9

The results of the B3 distillation mole fraction (B2 re-distillate) showed a significant

increase in the graph below, especially in the ethanol component that rose and did not decrease

for 3 hours of distillation duration. While the water component has increased but decreased

levels at distillation time for 2.5 hours, and for the isoamyl component there was no increase in

levels during the distillation process. Here is a plot of the yield of the B2 mole fraction:

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The mass rate of the B3 distillation results can be seen in the picture above. For ethanol

decreased by 15.1%, from 2564.07 kg/hr to 2176.95 kg/hr. While water decreased by 24.5%,

from 763,724 kg/hr to 576,959 kg/hr and isoamyl can be said to have no increase in flow rate

at the top (distillate). So that the content contained in B3 distillate is only water and ethanol.

In the results obtained distillate it is very difficult to obtain ethanol content up to 99% because

there is an azeotrope between water and ethanol at the point of ethanol at 79% and water at

21%. Therefore, an entrainer or the addition of a third component is needed to overcome the

the bottom result in distillation, while the top result (distillate) will contain rich water and ethyl

acetate, then the distillation process can be carried out. The results obtained can be seen in the

graph below:

levels obtained in B1.2 distillation can be seen in the figure below:

Based on the picture above, ethanol levels in the mole fraction and mass have met the

achievement, which is 99%, because ethyl acetate binds water so that the boiling point of the

mixture becomes 70 so it is more volatile than ethanol. So the ethanol mass flow is 1826.2

Kg/hr.

the water component, there was a decrease of 64%, and isoamyl alcohol by 74.45%.

in B2 isoamyl mass flow from 5621.9 kg/hr to 1085 kg/hr, there was a decrease of 80.8%,

Water mass flow from 5106.26 kg/hr to 763.723 there was a decrease in mass flow by 85.05%

while in ethanol mass flow from 3822.47 kg/hr to 2564.07 kg/hr, there was a decrease of 32.93

%. However, because ethanol levels still have not reached the target of 99%, the B3 Mass rate

on the results of B3 distillation can be seen in the picture above. For ethanol decreased by

15.1%, from 2564.07 kg/hr to 2176.95 kg/hr. While water decreased by 24.5%, from 763,724

kg/hr to 576,959 kg/hr and isoamyl can be said to have no increase in flowrate at the top

(distillate). So that the content contained in B3 distillate is only water and ethanol, in B4 the

addition of an entrainer is carried out to achieve the target of 99% because this is very difficult

to do because there is azeotrope. After adding the entrainer, the mole fraction and mass were

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Asadollahzadeh, M. T., Ghasemian, A., Saraeian, A. R., Resalati, H., Lennartsson, P. R., &

Taherzadeh, M. J. (2017). Ethanol And Biomass Production From Spent Sulfite Liquor

By Filamentous Fungi. International Journal Of Biotechnology And Bioengineering,

11(10), 718–724.

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Terhadap Pressure Drop Didalam Packed Bed Column Pada Distilasi Campuran Etanol-

Amil-Alkohol-Air. Journal Of Research And Technology, 2(1), 56–61.

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Marnoto, T., Budiaman, I. G. S., Hapsari, C. R., Prakosa, R. A. Y., & Arifin, K. (2019).

Sari, N. K. (2018). Pembuatan Bioetanol Dari Rumput Gajah Dengan Distilasi Batch. Jurnal

Teknik Kimia Indonesia, 8(3), 94–103.

Sodeifian, G., Alwi, R. S., Razmimanesh, F., & Tamura, K. (2021). Solubility Of Quetiapine

Hemifumarate (Antipsychotic Drug) In Supercritical Carbon Dioxide: Experimental,

Modeling And Hansen Solubility Parameter Application. Fluid Phase Equilibria, 537,

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Soputra, A., Siregar, P., & Ekawati, E. (2015). Perancangan Sistem Simulasi Hysys & Integrasi