Introduction of Design Methanol and MTEB plant

A large petrochemical company considered, for many years now from its crude oil whose petroleum production as well as refinery separation the bottom residue has been combusting vacuum distillation as additional fuel as well as land filling any balance. In environmental regulations due to recent change, though, this option is no longer be available. Consequently, to convert this crude oil vacuum residue into methyl-t-butyl ether (MTBE) the engineering department division will be investigating. Oxygenated hydrocarbons are methyl-t-butyl ether as a gasoline which is extremely valuable under the new air pollution control regulations. To form carbon monoxide as well as hydrogen using partial oxidation of the residue this is the first process.. (Huang, 2007)

1.1) Statements of problem of Design Methanol and MTEB plant

In this project, synthesis the optimum flow sheet for the methanol production process, and calculate the cost along with the cost of the equipments with the manufacturing cost.

1.2). Background of Design Methanol and MTEB plant

The desired reaction for the design plant of MTBE is given below,

CH3OH + (CH3)2C=CH2  (CH3)3C-O-CH3

Must have 20% overload methanol in a feed stream.

There are two various feed sources

23% of isobutene

40% of isobutene

Now the background of Methanol plant design is that, Methanol is clear, flammable liquid through the slightly alcoholic smell. Fuel ,Solvent along with a feedstock on behalf of a manufacturing of different chemicals with the adhesive foams as well as medicine.

1.3) Objective of Design Methanol and MTEB plant

In the project design the objective of this project is that to design the plant which produces the 100,000 metric ton/ year MTBE, along with the analysis of the methanol synthesis.

2).Discussion of Design Methanol and MTEB plant

On the final phase of production your general assignment would focus, which includes the conversion of methanol as well as isobutylene to MTBE. To an MTBE reactor methanol product must be fed in order to do this, to form an MTBE where methanol as well as isobutylene is reacted with conversion of single phase methanol 85.3%. In the MTBE separation column in order to facilitate the removal of MTBE in an 8% molar excess methanol is fed. In a stream of mixed hydrocarbons to the MTBE reactor the isobutylene feed; 30% mole of the hydrocarbons stream in which isobutylene makes up. The average molecular weight of hydrocarbons assumed to have 60. In a pressure distillation column the product stream from MTBE reactor is then separated in the bottom steam where 99% of MTBE is recovered. Liquid -0liquid extractor contains 5% hydrocarbons, MTBE 1%, as well as 2% isobutylene fed to the extractor. Into the organic stream 3 % of water absorbed.

In the flash drum water methanol extract stream is cooled. Leaving vapor in flash drum contain the entering of water 2.5 percent as well as entering of methanol 3.5%. In an atmospheric distillation column at last, the methanol and water is separated; that contains 99% of methanol fed which is combined with the fresh methanol to the MTBE reactor. In the liquid-liquid extraction unit in order to make up the water lost as well as the flash drum to this recycle stream a small stream of water is added. (Van-Dal & et.al, 2013)

2.1). Calculation of Design Methanol and MTEB plant

Rate of reaction: of Design Methanol and MTEB plant

3). Conclusion of Design Methanol and MTEB plant

In this study as we discuss in above it is possible to generate 100,000 tons per year of MTBE at a conversion of 96 % with a purity regarding 95 percent. The design of the selected parameter is shown in the flow diagram. For the process the specification of the reactor needed such as volume, height as well as diameter. To make methanol these intermediate products are used upon the addition of isobutylene later it is transformed to methyl-t-butyl ether.

4). Recommendations  of Design Methanol and MTEB plant

For the MTBE plant design the 405 of the isobutene is chosen to desire the original location for the production facility of MTBE. The profitability metrics is greater even the revenues are the same. For the inability price of the vacuum distillation the profitability is higher than the actual.

5). Attachments

Figure 1: Flow diagram (Methanol By partial oxidation of vacuum distillation residue

Figure 2: Major Equipment Cost of Methanol plant design 

Figure 3: Manufacturing Cost of Methanol plant design

5.1) References of Design Methanol and MTEB plant

Huang, K. (2007). Design and Control of a Methyl Tertiary Butyl Ether (MTBE) DecompositionReactive Distillation Column.

Van-Dal, S. É., & et.al. (2013). Design and simulation of a methanol production plant from CO2 hydrogenation.