Extractive distillation controls

• US 9,026,252 B2
• Filed: 11/21/2012
• Issued: 05/05/2015
• Est. Priority Date: 12/30/2011
• Status: Expired due to Fees

• Current Assignee: ExxonMobil Chemical Patents Inc. (Exxon Mobil Corporation)
• Original Assignee: ExxonMobil Chemical Patents Inc. (Exxon Mobil Corporation)
• Inventors: Schaefer, Robert Alan, Monson, John J.
• Primary Examiner(s): Sasaki, Shogo
• Application Number:
  US13/683,588
• Publication Number:
  US 20130173061A1
• Time in Patent Office: 895 Days
• Field of Search: 700/266, 700/17, 700/18, 700/83, 700/268, 700/269, 700/270, 700271-273, 702/22, 702/31, 702/32
• US Class Current: 700/270
• CPC Class Codes: C07C 15/02 Monocyclic hydrocarbons
• CPC Class Codes: C07C 7/08 by extractive distillation
• CPC Class Codes: C07C 7/10 by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
• CPC Class Codes: C07C 7/11 by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
• CPC Class Codes: G05B 11/01 electric

Abstract

The invention concerns an improvement in the monitoring and control systems used in a liquid-liquid extraction unit or an extractive distillation unit for the separation of aromatic hydrocarbons from non-aromatic hydrocarbons.

Claims

1. In a process for separating aromatics from a hydrocarbon mixture feed comprising aromatics and non-aromatics by use of a solvent which preferentially absorbs aromatics, in a system comprising a liquid-liquid extraction (LLE) unit or an extractive distillation (ED) unit, wherein said solvent is mixed with said hydrocarbon mixture and said solvent preferentially absorbs said aromatics to provide a first aromatics-depleted hydrocarbon stream, relative to said hydrocarbon mixture feed, and a first aromatics-enriched solvent stream, relative to said hydrocarbon mixture, and wherein both said first aromatics-depleted hydrocarbon stream and said first aromatics-enriched solvent stream are further processed in said LLE unit or ED unit to produce a final aromatics-depleted stream and a product comprising at least one of the aromatics selected from the group consisting of benzene, toluene, and xylene, the improvement comprising:

(a) monitoring the amount of hydrocarbon feed entering an extractor tower of said LLE unit or ED unit, the amount of hydrocarbon recycled to said extractor tower from a stripper tower of said LLE unit or ED unit, the amount of hydrocarbon removed from said LLE unit or ED unit, and the amount of lean solvent entering said extractor tower, wherein said amounts are monitored by flow measuring devices and conveyed to a controller;

(b) calculating the hydrocarbon loading of the LLE unit or ED unit in said controller by the following equation;

% HC Loading=(EFF+Rec−

Raf)*100/(EFF+Rec−

Raf+LS)

wherein “

EFF”

is the amount of hydrocarbon feed entering said extractor tower, “

Rec”

is the amount of hydrocarbon recycled to said extractor tower from said stripper tower, “

Raf”

is the amount of hydrocarbon removed from said LLE unit or ED unit, and “

LS”

is the amount of lean solvent entering said extractor tower; and

(c) sending a signal from said controller to flow metering devices to control the amount of lean solvent and/or feed based on whether the HC loading is above or below a predetermined set value to adjust the lean solvent to feed ratio in said extractor tower to manage the amount of non-aromatics in the aromatics product, the amount of aromatics in the aromatics depleted hydrocarbon stream, flow rates, and energy usage and to improve reliability for the LLE unit or ED unit.

2. The process of claim 1, wherein said extractive distillation unit is a liquid-liquid extraction distillation unit.

3. The process of claim 1, wherein when said HC loading is greater than 25 wt % or 35 vol %, said controller sends a signal to the flow metering devices to either increase the amount of lean solvent or decrease the amount of feed introduced to said extractor tower.

4. The process of claim 1, wherein when said HC loading is less than 20 wt % or 30 vol %, said controller sends a signal to the flow metering devices to either decrease the amount of lean solvent or increase the amount of feed introduced to said extractor tower.