0.111 Topsoe Hydrocracking Processes 2011

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    Hydrocracking processes

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    Haldor Topse A/S Nymllevej 552800 Kgs. Lyngby - Denmark

    Topse HC processes 1 / 16

    JEOM/PZ/PEVB/MKJ 20 August 2010

    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Contents

    1 Topse hydrocracking processes 2

    2 Hydrogen optimisation 5

    3 Hydrocracking technology experience 5

    4 Energy conservation in hydroprocessing units 8

    5 Cat feed hydrotreater license references 11

    6 Hydrocracking catalysts 12

    7 Catalyst references 15

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    1 Topse hydrocracking processes

    Haldor Topse has licensed five hydrocrackers including full conversion single-stage

    and two-stage hydrocracking processes and a partial conversion hydrocracking

    process. For partial conversion hydrocracking, we offer once-through hydrocracking,

    mild hydrocracking (MHC) with integral diesel post treatment, and our patented staged

    partial conversion (SPC) process. A simplified process diagram illustrating the MHC

    process with integral diesel post treatment and SPC are shown in the below figures.

    Topsoe MHC Process with Distillate Post Treatment

    VGO

    NAPHTHA

    FCC FEED

    MHC

    REACTOR

    H2S

    HYDROGEN

    FRACTIONATOR

    LGO

    NAPHTHA

    HGO

    ULSD

    STRIPPER

    HGO POST-TREAT

    REACTOR

    MHCEFFLUENT

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Topsoe Staged Partial Conversion Process

    FEED

    NAPHTHA

    DIESEL

    FCC FEED

    GAS

    HDS

    REACTOR

    H2S

    HYDROGEN

    HDC

    STRIPPER FRACTIONATOR

    HDC

    REACTOR

    HDS

    STRIPPER

    For the Topse MHC process with integral diesel post treatment, the reaction section

    operates at medium pressure (60 to 100 barg) to produce the desired FCC feed quality.

    The post treatment stage upgrades the heavy gas oil product from the MHC by

    hydrotreating or hydrocracking to produce the desired ULSD quality. A comparison of a

    MHC process with a high pressure partial conversion and Topse MHC with post

    treatment is shown below:

    Configuration MHC

    (Base)

    High pressure

    HDC

    MHC with

    post treat

    Reactor pressure barg 80 160 80

    Gross conversion %vol. 30 30 30

    Diesel yield %vol. 29 30 28

    Diesel sulphur wppm 50 10 10

    Diesel density kg/m3 875 845 845

    Diesel cetane no. D-613 40 51 51

    Total installed cost Base 1.4*Base 1.3*Base

    Capex savings

    (relative to HP HDC)

    / TPD

    $/BPD

    2400

    400

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Hydrogen demand Base 2.2*Base 1.4*Base

    Hydrogen savings

    (relative to HP HDC)

    Nm3/m3

    SCFB

    50 - 80

    300 - 500

    The SPC process incorporates a staged reaction system in which a portion of the

    heavy gas oil product from the lead hydrodesulphurisation (HDS) reactor is bypassed

    on flow control reducing the net charge rate to the second series flow hydrocracking

    (HDC) reactor. This allows the net conversion level in the second reactor to besubstantially higher than the overall gross conversion requirement for producing FCC

    feed. Increased conversion dramatically improves the middle distillate product. Severity

    in the lead reactor is controlled independently based on the minimum HDS requirement

    for the FCC feed to make ultra low sulphur gasoline. Severity in the lag reactor is

    controlled based on meeting ultra low sulphur kerosene and diesel fuel requirements

    including smoke point, density and cetane quality.

    The separation of gas and liquid in the bottom of the lead reactor vessel is achieved

    without the need for any complex internals arrangement and uses a minimum of

    reactor height. Simple flow control is utilised to split the liquid phase from the bottom of

    the lead reactor.

    A comparison between a MHC process, a high pressure partial conversion process,

    and the SPC process is shown in the table below:

    Configuration MHC

    (Base)

    High pressure

    HDC

    Topse

    SPC

    Reactor pressure barg 100 160 100

    Gross conversion %vol. 30 30 30

    Diesel yield %vol. 31.0 31.5 28.0

    Diesel sulphur wppm 10 10 10

    Diesel density kg/m3 875 845 845

    Diesel cetane index D-4737 46 52 47

    Total installed cost Base 1.3*Base 1.1*Base

    Capex savings MM/TPD 3000

    Hydrogen demand Base 1.8*Base 1.3*Base

    Hydrogen savings Nm

    3

    /tonne 50

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Haldor Topse has constructed a pilot plant to demonstrate the SPC process and

    performed substantial testing and different feedstocks to provide an application

    database for the new technology.

    2 Hydrogen optimisation

    Haldor Topse optimises the hydrogen usage in a hydrocracker to achieve the processand product objectives by:

    - Using high selectivity hydrocracking catalysts to reduce light ends make andmaximise middle distillates to reduce hydrogen consumption.

    - Using different families of hydrocracking catalysts tailored to achieve desiredproduct properties. For example, one family of catalysts is used to maximisehydrogen uptake to produce high viscosity index unconverted oil used for lubeproduction, while another catalyst family is used to reduce mono-aromaticsaturation in the unconverted oil used as FCC feed.

    - Incorporating process features for the recovery of the soluble hydrogen from the

    off gases of the hydrocracker.

    3 Hydrocracking technology experience

    Topse has licensed five hydrocrackers two revamps and three grass-roots units in

    the last five years. Four of the licensed units were won in the last two years. The

    reasons why Topse was chosen as the hydrocracking licensor by our clients are:

    - Topse has hired engineers with vast experience in the design, start-up andoperation of hydrocracking units.

    - Topse has developed a family of commercially demonstrated pre-treating and

    hydrocracking catalysts. Our latest BRIMTMhydrotreating catalysts are the bestperforming hydrocracker pretreat catalysts on the market today. Topse offerscommercially proven hydrocracking catalysts for maximum middle distillateservice and for flexible co-production of naphtha and middle distillate.

    - Our maximum middle distillate hydrocracking catalysts produce distillates withexcellent cold flow properties due to enhanced isomerisation activity.

    - Topse has developed commercially proven reactor internals forhydroprocessing units to maximize utilization of the catalysts activities.

    - Topse can confirm operating conditions, yields and product properties in ourstate-of-the-art pilot plants.

    - Topse can provide customer focussed technical services using experiencedhydrocracking experts.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    The scope of supply for all five licensed units consists of hydrocracking technology

    license, engineering, catalysts, reactor internals, and technical services. In addition,

    scoping studies were performed for three projects to help the client better define the

    project scope prior to start of engineering.

    Below is a summary of the hydrocracking units licensed by Topse.

    OMV/Petrom, Petrobrazi Refinery, Romania

    OMV/Petrom licensed Topses hydrocracking technology for a 34,000 bpsd grass-

    roots hydrocracking unit at the Petrobrazi Refinery in Romania. The unit will provide a

    high conversion of a mixture of heavy vacuum gasoil and heavy coker gas oil into high

    quality diesel and jet fuel products. The new hydrocracker forms part of an overall

    project for expanding the capacity of the Petrobrazi Refinery to 6 million tonnes of

    crudes per year.

    The hydrocracker feed contains 2000 wppm nitrogen. It is a blend of 80 wt% heavy

    vacuum gas oil (HVGO) and 20 wt% heavy coker gas oil (HCGO). Topse was one of

    three licensors that competed in a paid study and was chosen as the licensor by OMVafter a thorough evaluation. Topse presented study cases covering 55% and 75%

    conversion to ULSD and lighter. The study deliverables includes PFD and sized

    equipment to allow independent cost estimates to be done by the clients contractor.

    During the study phase, the client ran tests in their hydrocracker pilot plant which

    confirmed Topses technical performance predictions.

    Topse produced an engineering design package for this unit and participated in FEED

    development with the clients selected contractor. The client awarded the project to

    Topse in November 2007.

    Undisclosed Refinery A

    This refinery has licensed a grass-roots 42,000 bpsd single stage full conversion

    hydrocracking unit from Topse. The unit is designed to maximise diesel production

    from converting vacuum gas oil. Start up is expected to be in 2015.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Undisclosed Refinery B

    An undisclosed refinery has licensed a Topse hydrocracker for a 65,000 bpsd grass-

    roots full conversion hydrocracker unit with a post-cracking reactor for maximising light

    naphtha yield by cracking heavy naphtha and kerosene. Topses hydrocracking

    technology was selected based on an innovative and cost-efficient solution for

    maximising the production of diesel and light naphtha. The unit is expected to start up

    in 2016.

    Preem AB, Gothenburg, Sweden - Revamp to mild hydrocracking unit

    In 2002, Preem AB in Gothenburg, Sweden awarded a license to Topse for the

    revamp of an existing AKZO Makfining unit for partial conversion hydrocracking of

    heavy atmospheric gas oil. A secondary revamp objective was to increase unit capacity

    by 27% to 9,100 bpsd. The reactor was revamped with Topse internals, and a full

    load of partial conversion hydrocracking catalysts was installed in this unit. The product

    fractionation system was revamped to allow withdrawal of middle distillate blend

    streams with optimum endpoints to maximise diesel pools.

    Preem increased the middle distillate yield with Topse high mid-distillate NiW

    hydrocracking catalysts. The diesel product fulfilled the project objectives, meeting witha good margin cloud point and colour specifications with a very low sulphur level of < 2

    wppm. The excellent cloud point obtained allowed an increase in diesel endpoint and

    yield.

    Following a study phase including pilot plant work, the revamp project was completed

    on time with a short schedule and was successfully started up in July 2003 after a

    normal refinery turn-around. Topse and Preem engineers co-authored a paper

    presented in the July 2005 issue of Hydrocarbon Engineering.

    Slovnaft Bratislava Refinery, Slovakia

    Topse was awarded a hydrocracker license to revamp the 24,000 bpsd Slovnafthydrocracker in 2007 (original licensor is UOP) in Bratislava Refinery in Slovakia. The

    scope of supply is license, catalyst, reactor internals, and engineering. A revamp study

    was done by Topse to achieve the following goals:

    - Change the catalyst and define the equipment revamp scope required to shiftfrom co-production of naphtha and middle distillate to maximum middle distillateoperation

    - Determine the maximum feed rate feasible without modifications of majorequipment

    - Provide new process simulation of the entire the hydrocracking unit (including

    fractionation section) for new operating mode

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    - Define the impact of adding LCO as a feed component- Recommend latest operating and maintenance best practices- Define the benefit of reactor internals replacement using Topses new

    internals- Recommend HPNA management strategy- Recommend improvement in unit safety and reliability- Recommend improvement in energy and on stream efficiency- Recommend solutions to a list of current operating constraints and bottlenecks-

    Provide size and cost estimate for new or modified equipment.

    Based on the study results, Slovnaft obtained management approval for the revamp

    project. Topse delivered a process design package for the revamp in 2008. The

    process design included detail design of the revamped reactor internals for three

    reactors. The main catalyst system used in the revamp was TK-605 BRIM for

    hydrocracker feed pretreat and TK-951, TK931, and TK-926 hydrocracking catalysts.

    The combination of these catalysts offers flexibility of product slate and superior

    product quality. The revamped unit started up successfully in 2009 and met all

    guarantees.

    4 Energy conservation in hydroprocessing units

    Energy consumption in hydroprocessing units is related in large part to the pumping

    and compression of process fluids to reaction pressures, heating reactants to reaction

    temperatures, and the separation and final cooling of refined products. This energy is

    supplied to the process through the use of utilities such as electrical power, fuel for

    combustion heat and steam and represents substantial operating costs for

    hydroprocessing facilities.

    Reactor and catalyst technologyHaldor Topse designs hydroprocessing units to achieve the required reaction

    performance at the optimum conditions of temperature, pressure, and gas circulation

    rate and thereby minimising the associated capex and energy consumption. This

    detailed knowledge of how the catalyst performance can be optimised leads to the

    lowest possible capital cost in addition to the most energy efficient design.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Substantial energy is consumed to overcome the hydraulic pressure drop associated

    with the operation of fixed catalyst bed hydroprocessing reactors. Topse catalysts are

    manufactured in a variety of shapes and sizes to both minimise pressure drop and

    prevent the increase in pressure drop associated with the build up of deposits within

    the catalyst bed. The use of state of the art reactor internals insures that the distribution

    and temperature control required for optimum catalyst performance can be achieved

    without the need for high catalyst bed pressure drop and corresponding energy

    consumption.

    Heat integration

    The reactions associated with hydroprocessing are exothermic and release substantial

    amounts of heat. This energy can be recovered by heat exchange and used to

    minimise the need for utility heating by fuel gas or steam. The feed to the reactor is

    preheated by exchange with the product exiting the reactor at higher temperature. The

    heat content of the reactor product can also be utilised to off-set a portion of the heat

    input required for product separation by distillation. Though it is not a preferred design

    approach, in some cases the reactor product heat can also be used for steam

    generation and thereby achieve increased efficiency by reducing the need for steam

    production outside the hydroprocessing unit.

    Maximising the use of process heat integration in a hydrocracking unit can reduce the

    required heat input to the fractionation section by 30 to 50 percent. In a modern facility,

    the capital cost associated with the large heat exchanger surface area required for

    such integration is easily justified by energy conservation and reduction of carbon

    emission.

    Power recovery turbines

    Some of the energy content of liquids at high pressure can be recovered through the

    use of hydraulic power recovery turbines. These turbines recover power when the fluid

    is expanded from high pressure to low pressure and can be used to drive mechanicalequipment directly or can be coupled to an electrical generator. Most commonly in

    hydroprocessing units, a turbine on the hydrocarbon product fluid is used to help drive

    the hydrocarbon feed pump. If the unit is equipped with a high pressure amine

    absorber, a turbine on the rich amine fluid can provide power to the lean amine booster

    pump. As much as 50 to 70 percent of the electrical pumping power can be saved in

    these applications.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    High efficiency process heaters

    High level process heat is generally supplied to hydroprocessing units by fuel gas

    combustion in fired heaters. High energy efficiency can be achieved through the use of

    steam generation and combustion air preheat by the hot flue gas generated in the

    heater. Such a heater configuration is illustrated in the below sketch. Air preheat

    reduces the amount of flue gas combustion needed to supply the process heat

    requirements. Steam generation can in many cases fully produce all the steam needed

    within the hydroprocessing unit and even export steam for general purpose use in the

    refinery. The extra cost associated with such systems is justified by energy

    conservations and the reduction of carbon emission.

    Process heat can also be supplied in conjunction with electrical power through the use

    of a gas turbine co-generation scheme. The hot flue gas from the gas turbine is used to

    supply the process heat while also producing steam and electricity. Such schemes are

    considerably more expensive than conventional high efficiency heater systems and

    therefore much more difficult to justify.

    High Efficiency Process Heater Configuration

    REACTOR

    CHARGEHEATER

    FRACTIONATOR

    CHARGEHEATER

    COMBUSTIONAIR

    STACK

    REFIN ERY

    STEAM

    BFW

    BOILERSUPERHEATER

    AIR

    PREHEATERATM

    STEAM

    DRUM

    FLUE GAS

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    5 Cat feed hydrotreater license references

    Marathon/Ashland Petroleum (MPC) - revamp of Catlettsburg FCC pretreating

    units

    Topse licensed two FCC pretreating unit revamps to MPC. One is a 35,000 BPD low

    pressure VGO (LPVGO) hydrotreater and the other is a 60,000 BPD high pressure

    VGO (HPVGO) hydrotreater. The processing objective for these units is to reduce the

    sulphur content in the feedstock from the two FCC pretreating units to approximately500 wppm and 750 wppm respectively. The combined FCC feed allows the refinery to

    produce gasoline meeting the 40 wppm EPA specification without FCC gasoline post

    treatment. Topse supplied license, engineering, reactor internals, and catalyst for

    these two units.

    Topse delivered the engineering packages for the revamps in July 2001. Two new

    lead reactors and two new lag reactors were designed and fabricated for the HPVGO

    unit, and four existing reactors were relocated to the LPVGO unit and fitted with

    Topse reactor internals. The new reactors plus internals for this project were shipped

    in August, 2002. The HPVGO unit started up successfully in June 2003 and met all

    guarantees. The LPVGO unit started up in February 2004 and met all guarantees.

    Undisclosed Refinery A 1stFCC pretreating unit

    In November 2001, Topse executed an alliance agreement with Refinery A to use

    Topse hydroprocessing technology for the design of new and/or revamped cat feed

    hydrotreaters (CFHT) within its refining system. The initial project under this alliance is

    a grass-roots 33,000 BPD CFHT. Topse delivered a process design package for the

    unit in May 2002. The processing objective for this project is to reduce the sulphur in

    the FCC feed to approximately 700 wppm, which will enable the FCC to produce full

    range naphtha with a sulphur content less than 50 wppm. Topse supplied license,engineering, reactor internals, and catalysts for this unit.

    The unit started up successfully in November 2005 meeting all guarantees. A process

    study has been prepared for increasing the feed capacity to 39,000 bpsd while

    processing much tougher Canadian crudes. These recommended revamp

    requirements are currently being implemented.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    Undisclosed Client A 2ndFCC pretreating unit

    The second unit to be included under the alliance is the revamp of a 29,000 bpd CFHT

    unit. The first phase of this project was installation of a new top distribution tray for an

    existing reactor in the VGO hydrotreater in October, 2002. The second phase of this

    project includes the revamp and tie-in of a second reactor with Topse internals, to

    enable the unit to produce a low sulphur FCC feed. Topses supply for this unit is

    license, engineering, reactor internals, and catalysts. The unit started up in April 2006

    and has met all guarantees.

    6 Hydrocracking catalysts

    A hydrocracker is one of the most profitable units in a refinery, partly due to the volume

    swell, and partly because it converts heavy feedstocks to lighter and more valuable

    products such as naphtha, jet-fuel, kerosene and diesel. The unconverted oil may be

    used as feedstock for FCC units, lube oil plants and ethylene plants. Any improvement

    in the hydrocracking unit operation significantly improves overall refinery economics.

    The proper selection of hydrocracking catalysts offers a great potential for enhancingthe performance of the hydrocracking unit with respect to yield structure, product

    properties, throughput and cycle length.

    For optimum performance of a hydrocracking catalyst, it is important to have a high-

    activity hydrotreating catalyst in front of it to convert organic nitrogen and heavy

    aromatic compounds to low levels. Topse offers a complete catalyst solution,

    comprising hydrotreating and hydrocracking catalysts as well as grading and guard

    catalysts.

    Maximum middle distillate hydrocracking catalysts

    For hydrocracking catalysts, there is often a trade-off between catalyst activity and

    product selectivity. There can furthermore be a trade-off between the various product

    properties such as the smoke point of the jet fraction, the cetane number and cold flow

    properties of the diesel fraction and the viscosity index of the unconverted oil.

    At the same time, the refiner is often interested in limiting hydrogen consumption. The

    tools that catalyst developers have at hand to address these various requirements are

    balancing the hydrogenation function with the acidic function and modifying the two

    functions.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    As a result of extensive R&D efforts, Topse has developed and commercialised two

    series of hydrocracking catalysts which in combination with the appropriate Topse

    pretreater catalysts from the BRIM series have shown to provide a step-out

    performance compared to existing hydrocracking catalysts in the industry.

    The red hydrocracking catalyst series provides exceptional middle distillate yields

    combined with excellent product properties including high cetane number for diesel,

    high smoke point for kerosene and high viscosity index for unconverted oil:

    The blue hydrocracking catalyst series provides an even better middle distillate yield

    with superior cold flow product properties compared to the red series.

    The red series

    TK-925 is a maximum distillate catalyst. Its main objective is to maximise high-quality

    diesel yield while producing unconverted oil with excellent qualities for lube oil plants or

    for FCC units.

    TK-931is a middle distillate catalyst designed to produce very high yields of premium-

    quality diesel, jet-fuel and lube oil base stocks. Specifically, this catalyst gives a highsmoke point for jet, an excellent cetane number for diesel fraction and a high viscosity

    index (VI) for lube base oils.

    TK-941 and TK-951are the recommended catalysts when both high activity and high

    yield are important. TK-951 is more active than TK-941, and both provide excellent

    middle distillate yields with efficient hydrogen utilisation.

    TK-947 is optimised for units at high space velocity and/or low unit pressure. TK-947

    has shown excellent performance in both catalyst activity and stability and in product

    yields and properties.

    The blue series

    TK-926 has a high selectivity for diesel production. The acid function of TK-926 has

    been modified to enhance the isomerisation reactions and improve the cold flow

    properties of the products.

    TK-933 and TK-943 are medium-activity catalysts to be used in services, where very

    high middle distillate yields, very good cold flow properties and optimised hydrogen

    consumption are a must. The diesel cloud point is typically 10-20C (18-36F) lower

    than that obtained with other catalysts.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    A special acid function modification is used to improve the isomerisation activity and

    the middle distillate selectivity. TK-943 is more active than TK-933.

    Mild hydrocracking applications

    Many hydrocrackers in the refineries operate in mild hydrocracking mode. For these

    units, the main objectives are to obtain a certain minimum conversion as well as to

    meet specific product properties such as sulphur content, density and cetane number.

    Typical pressures are in the 60-110 bar (850-1560 psig) range. Typical conversion is

    10-20% for lower pressure units and 30-50% for higher pressure units.

    Meeting the product objectives under such conditions can be challenging. Very often

    the cycle length is determined not by decline in conversion, but by failure to meet a

    product property such as sulphur content in the diesel fraction. Our catalysts exhibit an

    excellent nitrogen tolerance, resulting in very stable HDS and HDN activities

    throughout the cycle. The optimal catalyst or combination of catalysts depends on feed

    quality and available hydrogen.

    Hydrocracker pretreatment

    The pretreatment stage in a hydrocracker has the primary objective of removingorganic nitrogen, particularly basic nitrogen compounds and aromatics in the feed.

    Nitrogen compounds have a significantly negative impact on the activity of the

    hydrocracking catalyst and consequently on the performance of the hydrocracker.

    The growing interest in processing heavy oils with high nitrogen content has created a

    need for pretreatment catalysts with an even higher HDN activity. Depending on the

    specific needs, Topse has developed two catalysts for this service. The

    catalysts are prepared with the proprietary BRIM technology, resulting in high activity

    for both HDS and in particular HDN. In addition, due to the better utilisation of the

    active metals and modified carriers the high activity BRIM catalysts have attractive

    filling densities.

    TK-607 BRIMexhibits a very high HDN activity and an excellent stability for high-

    pressure hydrocracker services. Sulphur and nitrogen removal are significantly

    improved with TK-607 BRIM compared to previous generation catalysts TK-605

    BRIM and TK-565.

    TK-561 BRIMis a catalyst where the activity for nitrogen removal has been

    maximised while maintaining a high HDS activity. TK-561 BRIM is the perfect choice

    for mild hydrocracking applications, where stability and conversion activity are main

    objectives, and product sulphur is the limiting factor.

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    Information contained herein is confidential; it may not be used for anypurpose other than for which it has been issued, and may not be used byor disclosed to third parties without written approval of Haldor Topse A/S.

    7 Catalyst references

    Slovnaft a.s., Slovakiahas purchased 190 tonnes of catalysts for their high pressure

    hydrocracker. The catalysts were purchased for their 3,400 MT/day unit, operating at

    150 bar with a conversion at about 95%. This decision was taken based on

    experiences with excellent performance of Topses catalysts since 2005. The feed to

    the unit is Russian export blend.

    Preem Lysekil, Sweden has decided to follow a successful three-year TK-558 BRIM

    run of their 53.000 bpsd, 71 bar mild hydrocracker unit with a new load of Topse

    catalysts. This is due to needs for higher conversion when they are in VGO mode of

    this unit and improved cold flow properties of the diesel produced in the diesel mode.

    ENAP Refinerias Bio Bio, Chile has selected catalyst material from Topse for the

    first time to their high pressure hydrocracker. This 2,400 MT/day unit operates at 143

    bar, aiming at a maximum mid-distillate yield at a net conversion of 70% based on

    volume. The processed feed is blends of HVGO and HCGO, and the feed nitrogen

    varies from 1,000 to 3,100 ppm N.

    ENAP Refinerias Aconcagua, Chilehas purchased 224 tonnes of catalysts for their

    single-stage hydrocracker. The catalysts were purchased for their 3,000 MT/day unit

    operating with a conversion at about 60%. The main objectives are high quality FCC

    feed and high quality product diesel. The processed feed is blends of HVGO and VGO.

    YPF, Argentinaselected Topse hydrocracking catalyst system after a series of

    detailed pilot plant studies on actual feed and conditions. The main objectives for this

    full conversion 140 bar hydrocracker are increased diesel and kerosene yields with

    improved properties such as cloud point and cetane index.

    Murphy Meraux, LA, USA has awarded Topse for their hydrocracker train. This full

    load of Topse hydrocracker and pretreatment catalysts for the high pressure, 2,450

    psi, 32,000 bpsd hydrocracker aims at 41% conversion with the highest possible

    selectivity into low sulphur mid distillates. The processed feed is a blend of HVGO,

    LVGO and AG with a rather high Si content.

    Preem Lysekil, Sweden has awarded Topse to their major European hydrocracker.

    This is a full load of Topse hydrocracker and pretreatment catalysts for this single-

    stage two-reactor 142 bar 47,000 bpsd hydrocracker, aiming at a 55% conversion with

    good properties of the produced diesel. Most of the feed being processed is Russian

    VGO.

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    Saras, Sarroch, Italydecided again to use Topse catalysts for their 60,000 bpsd mild

    hydrocracker. This unit, aiming at 40-50% conversion and 10 ppm sulphur in the diesel,

    requires the most stable catalyst system in order to be able to operate for more than

    one year. The feed to this 100 bar unit has an end-point as high as 630C.

    MOL Szazhalombatta, Hungary decided again to purchase Topse hydrocracking

    and pretreatment catalysts for their 2010 turnaround in their 6,000 MTPSD MHC unit.

    The processed feed is blends of HVGO and HCGO, aiming at a conversion of more

    than 27% to high quality diesel. The unit operates at a pressure of 75 bar.

    Petro Piar, Venezuela has again, due to very difficult operating conditions of the U16and an unpredicted short cycle, selected Topse hydrocracking catalysts for this majorhydrocracking 55,000 bpsd U16, treating very heavy coker gas oil feed.