Controlling fractionation using dynamic competing economic objectives

Patent metadata

Field	Value
Publication number	US-11707698-B2
Application number	US-202218060308-A
Country	US
Kind code	B2
Filing date	Nov 30, 2022
Priority date	Dec 22, 2021
Publication date	Jul 25, 2023
Grant date	Jul 25, 2023

Abstract

Processes and systems for controlling operation of a commercial refinery distillation column and/or splitter operable to separate hydrocarbons. An automated process controller (APC) receives signal from at least one analyzer that provides information about the concentration of at least a first chemical in a first fraction and a second chemical in a second fraction obtained from the distillation column. The APC comprises programming in the form of an algorithm that calculates real-time monetary values for the first chemical and the second chemical and alters the operation of the distillation column to change either the percentage of the first chemical in the second fraction or the percentage of the second chemical in the first fraction, thereby maximizing overall operational profit for the distillation column.

First claim

I claim:

1. A process for operating a refinery distillation unit, comprising:
(a) directing a feed stream comprising a mixture of hydrocarbons, the hydrocarbons having a boiling point that is in the range from 45° C. to 85° C. (at 1 atm) into a distillation unit that separates hydrocarbons according to their boiling point to produce at least a first fraction that leaves the distillation unit via first outlet and a second fraction that leaves the distillation unit via second outlet,
wherein the first fraction has an average boiling point (at 1 atm) that is less than the average boiling point (at 1 atm) of the second fraction,
wherein the first fraction comprises at least a first chemical that comprises a first monetary value (per unit) and the second fraction comprises at least a second chemical comprising a second monetary value (per unit),
wherein the first chemical does not completely segregate into the first fraction and the monetary value of the percentage (mol %) of the first chemical that does not segregate into the first fraction is zero,
wherein the second chemical does not completely segregate into the second fraction and the monetary value of the percentage (mol %) of the second chemical that does not segregate into the second fraction is zero;

(b) separating the feed stream in the distillation unit to produce the first fraction and the second fraction;
(c) determining the percentage (mol %) of the first chemical that leaves the distillation unit in the first fraction and the percentage (mol %) of the second chemical that leaves the distillation unit in the second fraction;
(d) calculating a total profit obtained from the separating by multiplying a first chemical price consisting of the monetary value (per unit) of the first chemical by the percentage (mol %) of the first chemical in the first fraction, then adding to this the product of a second chemical price consisting of the monetary value (per unit) of the second chemical multiplied by the percentage (mol %) of the second chemical in the second fraction,
wherein the first chemical price is selected from one of: 1) a first chemical commercial price and 2) a first product commercial price multiplied by the conversion efficiency from the first chemical to the first product, wherein the first product is derived from the first chemical;
wherein the second chemical price is selected from one of: 1) a second chemical commercial price and 2) a second product commercial price multiplied by the conversion efficiency from the second chemical to the second product, wherein the second product is derived from the second chemical;

(e) intermittently performing the calculating of (d) with an algorithm to find a solution cut point temperature that produces a maximum total profit from the separating at the time the calculating is performed, wherein the solution cut point temperature corresponds to known operating settings for the distillation unit, wherein the first chemical price and the second chemical price are variable and can change between iterations of the calculating
(f) adjusting the known operating settings of (e) to the distillation unit, wherein the adjusting comprises altering one or more operating parameters to change the distillation unit cut point temperature to the solution cut point temperature,
wherein the operating parameters are selected from one or more of: the temperature of the heated feed stream entering the distillation unit, quantity of heat input to the reboiler and flow rate of the light fraction leaving the distillation unit,
wherein the adjusting alters at least one of: the percentage of the first chemical that exits the distillation unit in the first fraction and the percentage (mol %) of the second chemical that exits the distillation unit in the second fraction.

2. The process of claim 1 , wherein parts (d) and (e) are performed by a model predictive control algorithm.

3. The process of claim 1 , wherein intermittently performing the calculating occurs in a range from once per 0.01 sec to once per day.

4. The process of claim 1 , wherein the intermittently calculating occurs in a range from once per minute to once per hour.

5. The process of claim 1 , wherein the first chemical is a class of chemical selected from C6 isoparaffins and n-paraffins and the second chemical is a class of chemical selected from at least one of C6 naphthenes and benzene.

6. The process of claim 1 , wherein the feed stream is selected from a straight run light naphtha stream derived from an atmospheric distillation unit, a naphtha stream derived from a hydrocracker and a naphtha stream derived from a hydrotreater.

7. The process of claim 1 , wherein the feed stream additionally comprises a third chemical that segregates into the second fraction and comprises a third monetary value (per unit),
wherein the third chemical does not completely segregate into the second fraction and the monetary value of the percentage (mol %) of the third chemical that does not segregate into the second fraction is zero,
wherein the determining of (c) additionally finds the percentage (mol %) of the third chemical that leaves the distillation unit in the second fraction,
wherein the calculating of the total profit in (d) additionally comprises adding the product of a third chemical price consisting of the monetary value (per unit) of the third chemical multiplied by the percentage (mol %) of the third chemical in the second fraction,
wherein the third chemical price is determined by one of 1) a commercial price for the third chemical or 2) a commercial price for a third product derived from the third chemical multiplied by the conversion efficiency from the third chemical to the third product,
wherein the third chemical price is a variable and can change between iterations of the calculating.

Assignees

• Phillips 66 Co

Inventors

• Pan Yangdong

Classifications

• B01D3/4211

  of columns · CPC title

• B01D3/4233

  Head- and feed stream · CPC title

• C10G7/12 Primary

  Controlling or regulating · CPC title

• G05B13/048

  using a predictor · CPC title

• C10G2300/104

  Light gasoline having a boiling range of about 20 - 100 °C · CPC title