Considerations for Upgrading Light Cycle Oil with Hydroprocessing Technologies

CATEGORY: LCO - LIGHT CYCLE OIL 
Considerations for Upgrading Light Cycle Oil with Hydroprocessing Technologies

Type	Journal Article
Author	Deepak Bisht
Author	John Petri
URL	http://dx.doi.org/10.1080/00194506.2014.927179
Pages	1-15
Publication	Indian Chemical Engineer
Date	August 15, 2014
Abstract	The need for more diesel fuel far outpaces gasoline growth, while demand for heavy fuel oil is actually declining. Light cycle oil (LCO) is a diesel boiling range product from fluid catalytic cracking units. Unfortunately, LCO is a poor diesel fuel blending component without further processing. Authors describe various ways of economically upgrading LCO, including hydrotreating, high pressure hydrocracking for full conversion of LCO into naphtha and a more optimized partial conversion hydrocracking process. The optimized partial conversion hydrocracking process provides an effective and flexible process to process LCO into such products as very-low sulphur diesel and high-octane high-aromatics naphtha.

Considerations for Upgrading Light Cycle Oil with Hydroprocessing Technologies

CATEGORY: LCO - LIGHT CYCLE OIL
Considerations for Upgrading Light Cycle Oil with Hydroprocessing Technologies

Type	Journal Article
Author	Deepak Bisht
Author	John Petri
URL	http://dx.doi.org/10.1080/00194506.2014.927179
Pages	1-15
Publication	Indian Chemical Engineer
Date	August 15, 2014
Abstract	The need for more diesel fuel far outpaces gasoline growth, while demand for heavy fuel oil is actually declining. Light cycle oil (LCO) is a diesel boiling range product from fluid catalytic cracking units. Unfortunately, LCO is a poor diesel fuel blending component without further processing. Authors describe various ways of economically upgrading LCO, including hydrotreating, high pressure hydrocracking for full conversion of LCO into naphtha and a more optimized partial conversion hydrocracking process. The optimized partial conversion hydrocracking process provides an effective and flexible process to process LCO into such products as very-low sulphur diesel and high-octane high-aromatics naphtha.

Molecule-based kinetic Monte Carlo modeling of hydrotreating processes applied to Light Cycle Oil gas oils

CATEGORY: LCO – LIGHT CYCLE GAS OIL
Bulletin of the American Physical Society, APS March Meeting 2013, Volume 58, Number 1, Monday–Friday, March 18–22, 2013; Baltimore, Maryland
Molecule-based kinetic Monte Carlo modeling of hydrotreating processes applied to Light Cycle Oil gas oils
Max Kolb
Laboratoire de Chimie, Ecole Normale Sup\'erieure de Lyon, F-69364 Lyon, France
Luis Pereira de Oliveira
Luis.Pereiradeoliveira@gmail.com
Jan J. Verstraete
IFP Energies nouvelles, BP 3, 69360 Solaize, France
Abstract
Authors present an innovative kinetic modeling strategy for refining processes for heavy petroleum fractions. Their approach makes it possible to overcome the lack of molecular details in describing the petroleum fractions. The simulation of the reactions process is comprised of a two-step procedure.
Step one involves generation of a mixture of molecules representing the feedstock of the process using two sucessive molecular reconstruction algorithms. The first algorithm is a stochastic reconstruction which generates an equimolar set of molecules with the appropriate analytical properties via a Monte Carlo method. The second algorithm is a reconstruction by entropy maximization which adjusts the molar fractions of the generated molecules in order to further improve the properties of the mixture. Step two employs a kinetic Monte Carlo method to simulate the effect of the refining reactions on the previously generated set of molecules. The full two-step methodology was applied to the hydrotreating of LCO gas oils and to the hydrocracking of vacuum residues from different origins.
Full Text Source (Subscription or Fee): http://meetings.aps.org/Meeting/MAR13/Session/Q1.221

Method For Producing Aromatic Hydrocarbons, And Aromatic Hydrocarbon Production Plant (Chiyoda Corp.; JX Nippon Oil & Energy Corp.)

CATEGORY: LCO – LIGHT CYCLE OIL
PATENT
Method For Producing Aromatic Hydrocarbons, And Aromatic Hydrocarbon Production Plant (Chiyoda Corp.; JX Nippon Oil & Energy Corp.)
European Patent Application EP2554635
Inventors:
Minami, Hideki; Sugi, Yoshishige; Fukui, Atsushi; Nagumo, Atsuro; and Yasui, Susumu
c/o CHIYODA CORPORATION4-6-2 (MinatomiraiNishi-ku, Yokohama-shi Kanagawa 220-8765, JP)
Yanagawa, Shinichiro (c/o JX Nippon Oil&Energy Corporation8 Chidori-choNaka-ku, Yokohama-shi Kanagawa 231-0815, JP)
Application Number:
EP20110759554
Publication Date:
02/06/2013
Assignee:
Chiyoda Corporation (4-6-2 Minatomirai, Nishi-ku Yokohama-shi, Kanagawa 220-8765, JP)
JX Nippon Oil & Energy Corporation (6-3, Otemachi 2-chome, Chiyoda-ku Tokyo 100-8162, JP)
Abstract:
A method for producing aromatic hydrocarbons, the method including: (a) bringing a feedstock oil such as an LCO into contact with an aromatic production catalyst to obtain a reaction product containing aromatic hydrocarbons, (b) separating the reaction product into a tower top fraction and a tower bottom fraction using a distillation tower, (c) separating the tower top fraction into a crude aromatic fraction containing an LPG fraction, and an off-gas containing hydrogen, (d) separating the crude aromatic fraction containing an LPG fraction into an LPG fraction and a crude aromatic fraction, (e) separating the off gas containing hydrogen into hydrogen and an off-gas, and (f) using the hydrogen obtained in step (e) to hydrotreat the crude aromatic fraction, thereby obtaining an aromatic fraction.
Description:
TECHNICAL FIELD
The present invention relates to a method and a production plant for producing aromatic hydrocarbons by a catalytic aromatic production reaction.
Priority is claimed on Japanese Patent Application No.
2010-72373, filed March 26, 2010, the content of which is incorporated herein by reference.
BACKGROUND ART
Methods for producing aromatic hydrocarbons such as BTX (benzene, toluene and xylene) from a feedstock oil such as a light cycle oil (hereinafter also abbreviated as "LCO") obtained from a fluid catalytic cracking (hereinafter also abbreviated as "FCC") apparatus, or a light naphtha or heavy naphtha or the like obtained from a crude oil distillation apparatus, using a catalytic aromatic production reaction that employs an aromatic production catalyst are already well known. These production systems generally employ a fixed bed system (see Patent Document 1), a moving bed system (see Patent Document 2) or a fluidized bed system (see Patent Document 3).
However, feedstock oil such as an LCO obtained from an FCC apparatus, or a light naphtha or heavy naphtha obtained from a crude oil distillation apparatus usually contain a sulfur fraction, and therefore the feedstock oil must be subjected to a preliminary hydrotreatment. Also, the produced crude aromatic fraction including a large amount of BTX contains a sulfur fraction and olefins, and therefore the crude aromatic fraction must be subjected to a hydrotreatment.
However, because hydrogen is required for this type of hydrotreatment, a separate hydrogen production plant must be provided in addition to the aromatic hydrocarbon production plant. As a result, the overall system containing the aromatic hydrocarbon production plant becomes more complex, increasing the production costs for the aromatic hydrocarbons.
SUMMARY OF INVENTION
TECHNICAL PROBLEM
The present invention provide a production method and a production plant that does not require the provision of a separate hydrogen production plant for performing hydrotreatment, and can therefore provide aromatic hydrocarbons at low cost.
SOLUTION TO PROBLEM
A method for producing aromatic hydrocarbons according to the present invention includes: (a) bringing one or more feedstock oils selected from the group consisting of light cycle oil obtained from a fluid catalytic cracking apparatus, hydrotreated light cycle oil, and naphtha and straight-run gas oil obtained from a crude oil distillation apparatus into contact with an aromatic production catalyst to obtain a reaction product containing aromatic hydrocarbons, (b) separating the reaction product into a tower top fraction and a tower bottom fraction using a distillation tower, (c) separating the tower top fraction into a crude aromatic fraction containing an LPG fraction, and an off-gas containing hydrogen, (d) separating the crude aromatic fraction containing an LPG fraction into an LPG fraction and a crude aromatic fraction, (e) separating the off-gas containing hydrogen into hydrogen and an off-gas, and (f) using the hydrogen obtained in step (e) to hydrotreat the olefins and sulfur fraction contained within the crude aromatic fraction, thereby obtaining an aromatic fraction.
In step (a), at the same time that the feedstock oil is brought into contact with the aromatic production catalyst, which is in a fluidized bed state inside the fluidized bed reactor, thereby obtaining the reaction product containing aromatic hydrocarbons, a heating fuel that is supplied from externally is preferably combusted in the presence of an oxygen-containing gas, thereby heating the aromatic production catalyst that is extracted from the fluidized bed reactor.
The method for producing aromatic hydrocarbons according to the present invention may also include (g) hydrotreating the tower bottom fraction using the hydrogen obtained in step (e).
An aromatic hydrocarbon production plant according to the present invention includes an aromatic production unit that brings one or more feedstock oils selected from the group consisting of light cycle oil obtained from a fluid catalytic cracking apparatus, hydrotreated light cycle oil, and naphtha and straight-run gas oil obtained from a crude oil distillation apparatus into contact with an aromatic production catalyst to obtain a reaction product containing aromatic hydrocarbons, a first separator that separates the reaction product into a tower top fraction and a tower bottom fraction using a distillation tower, a second separator that separates the tower top fraction into a crude aromatic fraction containing an LPG fraction, and an off-gas containing hydrogen, a third separator that separates the crude aromatic fraction containing an LPG fraction into an LPG fraction and a crude aromatic fraction, a fourth separator that separates the off-gas containing hydrogen into hydrogen and an off-gas, a first hydrotreating unit that hydrotreats the crude aromatic fraction to obtain an aromatic fraction, and a first hydrogen supply unit that supplies the hydrogen obtained in the fourth separator to the first hydrotreating unit.
The aromatic production unit preferably has a fluidized bed reactor, in which the feedstock oil is brought into contact with a fluidized bed-state aromatic production catalyst to obtain the reaction product containing aromatic hydrocarbons, and a heating tank in which the aromatic production catalyst extracted from the fluidized bed reactor is heated by combusting, in the presence of an oxygen-containing gas, a heating fuel that is supplied from externally.
The aromatic hydrocarbon production plant according to the present invention may also include a second hydrotreating unit that hydrotreats the tower bottom fraction, and a second hydrogen supply unit that supplies the hydrogen obtained in the fourth separator to the second hydrotreating unit.
ADVANTAGEOUS EFFECTS OF INVENTION
The method for producing aromatic hydrocarbons and the production plant of the present invention do not require the provision of a separate hydrogen production plant for performing hydrotreatment, and can therefore produce aromatic hydrocarbons at low cost.
Free Full Text Source: http://www.freepatentsonline.com/EP2554635.html

Monitoring and treatment to maximize light cycle oil

CATEGORY: LCO – LIGHT CYCLE OIL
PTQ - Petroleum Technology Quarterly, Q3 2012
Monitoring and treatment to maximize light cycle oil
Greg Savage, Nalco
Current global trends in product demand favour the increasing production of diesel fuel over motor gasoline because the demand growth for middle distillate fuels has exceeded the demand growth for gasoline for some time.2 In fact, the US is now a net exporter of refined petroleum products (mostly middle distillates) for the first time since 1949.3 Furthermore, the demand for gasoline from refineries has declined due to increases in the average fuel economy and the use of renewable fuels.
Decline in gasoline demand in the US resulted in a reduction in refinery capacity, particularly in PADD I (East Coast), which increased cost sensitivities throughout the US refining market. US demand for propylene continues to rise at a rapid pace because steam crackers are switching to ethane feeds, and propylene and diesel continue to command a price premium over most other refined products.8 These changes in product demand mix and market over-capacity have resulted in refiners focusing on increasing middle distillate production with minimal additional capital and operational costs.
The question many refiners are now facing is how can existing refinery assets be used to economically increase diesel and propylene production. Refiners have many options to increase middle distillate and propylene production. Unfortunately, many of the options have significant negative consequences or additional capital costs. Changes in operation are often constrained by existing equipment limitations, and changing the product mix can reveal new bottlenecks.
Capital investment options
Crude distillation units and delayed coker units have some flexibility to increase distillate production, but are constrained by feed slate and mechanical limitations. Most US refineries only have two to five trays between the flash zone and the distillate draw, which results in less precise distillate cuts. In contrast, European refineries that are historically optimised for diesel production may have 10 to 14 trays in the same zone to ensure good separation. Some US refiners are now adding distillate draws on vacuum towers to maximise distillate production and limit the amount of distillate sent to the FCC unit, which is chiefly designed for the production of gasoline and will convert middle distillate-range feed to lighter products.
Most US refiners have invested in a FCC unit as their main conversion technology. Changes in operation, catalyst and feed can optimise the FCC unit for distillate production. Increasing diesel in a FCC unit is challenging, in part because FCC light cycle oil (LCO) has limited value as a blend stock for diesel fuel due to its aromatic, sulphurous character and because it requires further hydrotreating before blending.6 Construction of new hydrocrackers, which provide increased flexibility over FCC units and better-quality gasoline and distillate products, is ongoing but slow due to relatively high capital costs and the resulting increased hydrogen demand. Tighter sulphur specifications along with the increased processing of higher-sulphur feeds and the rise in production of high-sulphur intermediate products such as LCO are increasing the demand on hydrodesulphurisation units
Free Full Text Source: http://www.digitalrefining.com/data/articles/file/483503599.pdf  

LCO processing to improve refinery product value and diesel yield

CATEGORY: LCO - LIGHT CYCLE OIL
MOL Group Scientific Magazine, 2012/2
LCO processing to improve refinery product value and diesel yield
István Valkai, Ilona Wahlné Horváth, Mária Balassa, Bence Nagy,
ivalkai@mol.hu
whi@mol.hu
mbalassa@mol.hu
bnagy@mol.hu
Richárd Sági, PhD
risagi@mol.hu
MOL Group, Downstream Business Support
Abstract
Seeking a solution to the diesel imbalance of regional markets, MOL’s Downstream Technology Development has made significant efforts to research and apply new methods for upgrading low value refinery streams into the middle distillate pool. Amongst these the yield and quality improvement of the Fluid Catalytic Crackers’ light cycle oil (FCC LCO) product have been a primary focus, in line with worldwide refining trends.
Bench scale laboratory reactor experiments and test runs on real process units have been carried out to analyse the technical requirements, determine product yields and qualities, optimise the process parameters and operating costs of LCO production and processing. These revealed new opportunities that have been implemented at Duna Refinery (Százhalombatta) and have been proposed in all refineries of MOL Group.
Free Full Text Source: http://www.moltempodiesel.hu/repository/804932.pdf