Process for extraction of aromatics from petroleum streams

a petroleum stream and aromatic technology, applied in the field of improved extraction of aromatics from petroleum streams, can solve the problems of high capital cost of process compared to solvent extraction, affecting hydrogen yield, and occasional failure of atf produced by this process, so as to reduce operating cost, save capital cost, and save utilities.

Inactive Publication Date: 2004-09-23
COUNCIL OF SCI & IND RES
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

[0020] Yet another object of the invention is to provide a process wherein savings in capital cost are achieved by eliminating raffinate-re-extraction solvent fractionator.
[0021] Still another object of the invention is to reduce operating cost by saving in utilities by using heat integration of hot and cold stream.

Problems solved by technology

While in the case of fertiliser industry, limitation of aromatics (<10%) in naphtha feedstock is due to higher carbon to hydrogen ratio, which in turn affects hydrogen yield.
However, severe operating conditions such as high partial pressure of hydrogen and high hydrogen consumption are required for high aromatic feed stocks, which make the process highly capital cost intensive compared to solvent extraction.
(2) There is occasional failure of ATF produced by this process.
(3) The number of columns used for solvent recovery from raffinate and extract phases is too large.
However, this process consumes significant energy for the recovery of hydrocarbons, due to requirement of stringent operating conditions.
Moreover, processing of feeds having wide boiling range e.g. naphtha to gas oil in the same unit using block out operations is not feasible due to over lapping of boiling points with the solvent.
Handling of low thermal stability solvent is the main drawback of this process.
Difficulty in maintaining the extraction solvent composition
Re-extraction solvent such as n-hexane & n-heptane being pure hydrocarbons are costly

Method used

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  • Process for extraction of aromatics from petroleum streams

Examples

Experimental program
Comparison scheme
Effect test

example 2

[0060] For the extraction step the model mixture of propyl benzene-decane with 6.0 wt. % propyl benzene, was admixed with an equal weight of NMP p 20% sulpholane at 40.degree. C. Two liquid phases under equilibrium were formed. Each phase, as separated, made solvent-free and analysed. The extract phase contained 2.2 wt % propyl benzene, while its concentration reduced to 4.8 wt. % in the raffinate phase with 94.5 wt. % yield.

example 3

[0061] 3.3 kgs / hr of heavy naphtha fraction (100-200.degree. C.) from Assam crude, containing 30.2 wt. % aromatic is fed to packed extractor-A. It as counter-currently contacted with the selective solvent (NMP+10% water) at 40.degree. C. entering the column at a rate of 7.7 kgs / hr. The extract phase produced at a rate of about 8.6 kgs hr. 4.1 kgs hr of extract phase produced as above containing 0.54 kgs / hr of total hydrocarbons is fed it packed extractor-B and counter currently contacted with C.sub.6-C.sub.7 paraffinic petroleum fraction entering at a rate of 6.1 kgs / hr. Phase produced at a rate of 7.0 kgs / hr from the top of extractor-B contains 0.49 kgs / hr of NMP. The phase is water washed and fractionated shielding 0.55 kgs / hr of naphtha extract containing 77.2 w of aromatics. The recovered C.sub.6-C- paraffinic petroleum fraction is circulated back to extractor-B The bottom of the extractors contains 3.15 kgs / hr of lean solvent and 0.011 kgs / hr of naphtha hydrocarbons. 2.3 kgs / hr...

example 4

[0062] 2.0 kgb / hr of gas oil fraction (240-400.degree. C.) from Assam crude, containing 39.2 wt. % aromatic is fed to packed extractor-A. It was counter-currently contacted with the selective solvent (NMP+10% water) at 40.degree. C. entering the column at a rate of 7.4 kgs / hr. The extract phase produced at a rate of about 8.2 kgs / hr. 4.7 kgs / hr of extract phase produced as above containing 0.377 kgs / hr of total hydrocarbons is fed to packed extractor-B and counter currently contacted with C.sub.6-C.sub.7 paraffinic petroleum fraction entering at a rate of 6.8 kgs / hr Phase produced at a rate of 7.6 kgs / hr from the top of extractor-B contains 0.56 kgs / hr of NMP. The phase is water washed and fractionated yielding 0.345 kgs / hr of gas oil extract containing 86.9 wt % of aromatics. The recovered C.sub.6-C.sub.7 paraffinic petroleum fraction is circulated back to extractor-B. The bottom of the extractor-B contains 4.07 kgs / hr of lean solvent and 0.02 kgs / hr of gas oil hydrocarbons. 1.38 k...

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Abstract

The present invention provides a process for the extraction of aromatics from petroleum fractions i.e. naphtha, kerosene and gas oil, using re-extraction route for recovery of solvent.

Description

[0001] The present invention relates to an improved process for the extraction of aromatics from petroleum streams. The invention particularly relates to the extraction of aromatics from heavy naphtha, kerosene and gas oil range petroleum fractions with the aid of a suitable polar organic solvent and re-extracting the extract phase with a C.sub.6-C.sub.7 paraffinic solvent.[0002] Different petroleum fractions obtained in crude distillation unit contain varying concentration of aromatics depending upon crude oil source. These aromatics are required to be removed to produce various end products meeting the specifications with respect to aromatics. For example, naphtha used as feedstock in petrochemical industry for the production of olefins should not contain more than 5% of aromatics due to refractory nature of aromatics. While in the case of fertiliser industry, limitation of aromatics (<10%) in naphtha feedstock is due to higher carbon to hydrogen ratio, which in turn affects hy...

Claims

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Application Information

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Patent Type & Authority Applications(United States)
IPC IPC(8): C10G21/02C10G53/04
CPCC10G53/04C10G21/02
Inventor KHANNA, MOHAN KRISHANNANOTI, SHRIKANT MADHUSUDANPRASAD, GURUNAUTIYAL, BHAGAT RAMPAUL, DHARAMRAWAT, BACHAN SINGHGARG, MADHUKAR ONKARNATHSAXENA, ALOK K.KUMAR, PRADEEP
Owner COUNCIL OF SCI & IND RES
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