Ultra Deep Desulfurization of Diesel: How an understanding of the underlying kinetics can reduce investment costs

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1 Ultra Deep Desulfurization of Diesel: How an understanding of the underlying kinetics can reduce investment costs Abstract Kim G. Knudsen and Barry H. Cooper Haldor Topsøe A/S This paper presents an overview of the critical factors governing the production of ultra low sulfur diesel (ULSD) i.e. diesel fuel with less than 50 ppm sulfur. To produce ULSD it is necessary to remove the most refractive sulfur compounds, which are certain alkyl-substituted dibenzothiophenes. Alkylsubstituted dibenzothiophenes are desulfurized via one of two routes: by direct extraction of the sulfur atom, or by hydrogenation of one of the aromatic rings followed by sulfur extraction. Factors affecting the relative rates of reaction for the two routes are discussed, in particular the inhibiting effect of certain nitrogen containing components of diesel oils on the hydrogenation route. CoMo catalysts are generally more active for the direct desulfurization route, whereas NiMoP catalysts show relatively higher activity for the hydrogenation route. The consequences for ULSD are demonstrated through a number of cases studies, which serve to illustrate the effect of catalyst choice on required catalyst volume, hydrogen consumption and product properties. The case studies are used to discuss the merits of revamps versus grassroots units. Introduction Diesel fuel specifications are being tightened throughout the world as part of efforts to improve air quality. At the same time, the demand for diesel is increasing necessitating use of lower quality feedstocks. The combination of these factors places a heavy burden on the refiner s hydroprocessing capabilities. New hydrotreating capacity and revamp of existing facilities are needed to meet the future diesel specifications. The present emphasis is on the reduction of sulfur, but future requirements may include improvement of cetane number, reduction in polyaromatic content and reduction in density. For the production of ultra low sulfur diesel (ULSD), the refiner has to decide whether to revamp an existing hydrotreater or to build a new, grassroots unit. A revamp is less costly but will often be less flexible with respect to changes in feedstock and in required product properties. Many factors need to be considered in choosing the most cost-effective solution, but in all cases it is essential to have a thorough understanding of the kinetics for removal of the most refractive sulfur compounds. The kinetics of deep desulfurization is governed by the extent to which desulfurization (HDS) occurs by direct sulfur extraction, or by hydrogenation of the sulfur-containing molecule. The direct route is primarily inhibited by hydrogen sulfide, and the hydrogenation route by specific nitrogen-containing compounds. CoMo and NiMoP catalysts exhibit different preferences for the two routes. Detailed understanding of the kinetics of deep desulfurization is used to select the most suitable catalyst for a given service and to evaluate the relative advantages of a revamp versus a grassroots unit with respect to investments, hydrogen costs and product properties. Whether or not the refiner decides on a revamp or a grassroots unit, careful attention needs to be paid to the design of the reactor internals. Poor distribution of the reactants over the catalyst can contribute to channeling through the catalyst bed resulting in inefficient utilization of the catalyst, development of hot spots, and catalyst deactivation due to coke formation. The problem of poor distribution becomes more acute as the requirement for desulfurization increases. Changes in Diesel Specifications and Demand In recent years, the development and use of environmentally friendly fuels has had high priority throughout the world. The driving force is improvement in air quality especially in metropolitan areas. Reductions in vehicle emissions require improvements in both engine and exhaust technologies, and

2 - 2 - in fuel quality. The vehicle manufacturers have issued a World-Wide Fuel Charter 1, which stipulates minimum requirements for fuel quality to meet future emission standards. In the EU, current diesel specifications limit sulfur to a maximum of 3. By the year 2005, the sulfur content must be reduced to, and diesel containing a maximum of S must also be available. By Jan 1, 2009 all on-road diesel in EU will (subject to review) have a specification of max. sulfur. In Germany sulfur diesel will be mandatory from In the United States, the EPA has announced proposals to reduce diesel fuel sulfur levels by mid 2006 to 15 wppm. In California, transit bus fleets must use a 15 wppm sulfur diesel by October, 2002 and it is expected that this limit will be extended to more fleets shortly afterward. In Japan the government is considering plans to reduce sulfur content to below by The demand for diesel is growing in both Asia and Europe. Although the growth rate for middle distillate in Asia Pacific was relatively stagnant from , it rose to 4.6% in and future demand is forecast to be equivalent to the pre-1997 rate of approximately 5-8% per year 3. In the EU, the increase in demand for mid-distillates has been at about 1.2%/annum over the past 5 years. It is predicted that diesel demand in the EU will increase by 30% over the next 15 years 4. There is a reduced demand for home heating oil and fuel oil cutter stocks which can help meet the increase need for diesel but these lower quality stocks will require severe hydrotreatment to meet the future specifications. The Selection of Catalyst for Ultra Deep Desulfurization To appreciate the basis for the selection of catalyst for ultra deep desulfurization it is important to understand the nature of the most refractive sulfur compounds in diesel pool streams, and understand how these sulfur compounds react. Many studies have shown that the most refractive sulfur compounds in diesel streams are alkyl-substituted dibenzothiophenes in which the substituents are in the 4 and 6 positions (see Fig.1). In the feed to the hydrotreater, the proportion of these refractive sulfur compounds in relation to the total sulfur content varies depending on feed origin and boiling-range but in products from the hydrotreater containing 100 ppm sulfur or less essentially all the sulfur compounds will be compounds of this type R S Figure 1 - Most Refractive Sulfur Compounds in Diesel Fuels The normal reaction route for desulfurization is via extraction of the sulfur atom (see Fig. 2). CoMo catalysts remove sulfur primarily via this route. When the dibenzothiophene (DBT) contains alkyl groups in the 4 and 6 positions, access to the catalyst site becomes sterically-hindered and the rate of reaction drops considerably. There is an alternative reaction route for desulfurization called the hydrogenation route in which one ring of the DBT is hydrogenated before the sulfur is extracted. This route is much slower for most alkyl-substituted DBTs, but is faster for the sterically-hindered DBTs. NiMoP catalysts exhibit a relatively high activity for removal of sulfur via the hydrogenation route. NiMoP catalysts are generally less active for removal of the bulk of the sulfur (via direct extraction) but are better than CoMo catalysts for removing the sterically-hindered DBTs via the hydrogenation route. Unfortunately, inhibitors present in the oil poison the hydrogenation route. Recent work has identified these inhibitors as certain basic nitrogen compounds 4-7. Due to different reactivities towards removal of the inhibitors and the refractive sulfur molecules, a NiMoP catalyst behaves differently than a CoMo catalyst. The NiMoP catalyst does not become very active until almost all of the inhibitors have been removed, at which point it becomes more active than a CoMo catalyst. NiMoP catalysts are preferable to CoMo catalysts at high pressure and when the content of the inhibiting basic nitrogen compounds is low. Furthermore, the hydrogenation route is equilibrium limited, which results in a lower reactivity (and R' 7

3 - 3 - low apparent activation energy), so that at low pressures and high temperatures, a CoMo catalyst can therefore be a better choice than a NiMoP catalyst. Hydrogenation reactions such as aromatic saturation also proceed via the hydrogenation route and are inhibited by the same nitrogen compounds. If NiMoP catalysts can be applied, more aromatic saturation occurs (compared to using CoMo catalysts) resulting in a greater improvement in cetane number and density, and a lower product PAH content. There will also be higher hydrogen consumption, which may have consequences for hydrogen availability and recycle rate, and for compression costs. Case Studies for the Production of Ultra Low Sulfur Diesel As mentioned earlier, the refiner needs to decide whether the desired reduction in diesel sulfur content can be achieved by revamping an existing unit (e.g. adding more hydrotreating reactor capacity, revamping reactor internals, revamping the treat gas system etc.) or whether it is necessary to build a grassroots unit. The decision will depend on many factors including the quality of feedstocks, the design criteria for the existing unit, and whether or not improvements in other diesel properties are required. The optimum solution with respect to overall investment and operating costs will depend on the correct choice of catalyst based on the considerations outlined above. In order to illustrate how the r e- quired extra reactor volume depends on operating conditions and feedstock properties, we present below three case studies. The case studies also serve to illustrate the effects on other key parameters for diesel fuel quality and the extent to which there is a need for more hydrogen. The three cases are: Figure 2 - Reaction Pathways for HDS of DBT Case 1:Hydrotreater producing 500 wppm sulfur operating at 32 bar hydrogen pressure on a straight-run feedstock Case 2:Hydrotreater producing 500 wppm sulfur operating at 32 bar hydrogen pressure on a blended feedstock containing 25% LCO and 75% straight-run. Case 3:Hydrotreater producing 500 wppm sulfur operating at 54 bar hydrogen pressure on a blended feedstock containing 25% LCO and 75% straight-run. For each case, calculations have been made to estimate the incremental reactor volume needed to reach a and a sulfur specification, and key product properties have been estimated. The basis for the calculations and estimates is extensive testing performed in our laboratories at ultra deep desulfurization conditions. Comparisons are made between two high activity catalysts for ULSD: TK-574 (CoMo) and (NiMoP). Case 1: Straight-run Feed at 32 bar

4 - 4 - This case is based on straight-run gas oil containing 1.2 wt% sulfur operating at a hydrogen partial pressure at inlet of 32 bar. Feedstock properties are given in Table 1. A comparison is made between TK-574 and. Catalyst cycle length is fixed at 2½ years. Table 2 shows the reactor volumes required to reach and sulfur relative to the reactor volume required to reach on the CoMo catalyst, and the relative chemical hydrogen consumption. The table also shows changes in other key product properties. Density, kg/m Sulfur, wt% 1.2 ASTM D86, C 10v% / 50v% 90v% / 95v% 243/ /360 Total Aromatics Content, wt% 25.5 PAH content, wt% 9.0 Calculated Cetane Index, ASTM D Table 1: Feed Properties for Straight-run High Sulfur Gas Oil For Case 1, reducing the product sulfur content from to whilst maintaining cycle length requires almost a doubling of reactor volume for the CoMo catalyst, and 75% increase in reactor volume for the NiMoP catalyst. The NiMoP catalyst can remove the inhibitors to the hydrogenation route at the conditions needed to reach the two product sulfur levels, and as a result performs better than the CoMo catalyst. Similarly, the NiMoP catalyst exhibits more hydrogenation and this result in improve product properties with respect to PAH content, density and Cetane Index, and a corresponding higher hydrogen consumption. TK-574 TK-574 Relative Reactor Volume Relative Hydrogen Consumption (SOR) Product Properties at Start-of-Run PAH Content, wt% Density, kg/m CCI, ASTM D Table 2: Relative Reactor Volume and Hydrogen Consumption, and Product Properties (Case 1) Case 2: Blended Feed at 32 bar This case is based on a blend of 25% light cycle oil and 75% straight-run gas oil containing 1.5 wt% sulfur operating at a hydrogen partial pressure at inlet of 32 bar. Feedstock properties are given in Table 3. The catalyst is TK-574, a high activity CoMo type catalyst. Catalyst cycle length is fixed at 2½ years. Density, kg/m Sulfur, wt% 1.5 ASTM D86, C 10v% / 50v% 90v% / 95v% 243 / / 360 Total Aromatics Content, wt% 30.0 PAH content, wt% 14.0 Calculated Cetane Index, ASTM D Table 3: Feed Properties for High Sulfur Blended Gas Oil

5 - 5 - Table 4 shows the reactor volumes required to reach and sulfur relative to the reactor volume required to reach 500 wppm, and the relative chemical hydrogen consumption. The table also shows changes in other key product properties. 500 wppm Relative Reactor Volume Relative Hydrogen Consumption (SOR) Product Properties PAH Content, wt% 4.2 (SOR) 9.1(EOR) 5.6 (SOR) 8.5 (EOR) 6.3 (SOR) 8.3(EOR) Density, kg/m (SOR) 856 (SOR) 856 (SOR) CCI, ASTM D (SOR) 48.9 (SOR) 48.7 (SOR) Table 4: Relative Reactor Volume and Hydrogen Consumption, and Product Properties (Case 2) For Case 2, reducing the product sulfur content from 500 wppm to whilst maintaining cycle length requires almost a doubling of reactor volume, and further reduction from to requires the addition of approximately 80% more reactor volume. The hydrogen consumption is similar for all product sulfur levels. The large extra volume required to meet the low product sulfur levels will result in an increase in pressure drop and may necessitate a revamp of the recycle gas system. It is also possible that the low LHSV required at the lowest product sulfur levels will result in significant hydrocracking (to naphtha and gas) thereby reducing diesel yield and necessitating extra investment in product fractionator overhead equipment. If there is significant hydrocracking, there will be an increase in hydrogen consumption compared to Table 4. There is a deterioration in the other key product properties as product sulfur level is lowered. Furthermore, the quality of the product with respect to the three properties shown in Table 4 deteriorates throughout the run as temperature is raised to counteract catalyst deactivation. This is illustrated in Table 4 by comparing the PAH content at start-of-run (SOR) and end-of-run (EOR). The PAH content in all cases is very high at EOR, because the equilibrium between mono-ring aromatics and poly-ring aromatics becomes less favorable at the temperatures used at EOR. The PAH concentration affects product density and cetane index (and cetane number), and at EOR the density will be higher in all three cases and the cetane index (and cetane number) will be lower. Case 3: Blended Feed at 54 bar This case is based on the same blend of 25% light cycle oil and 75% straight-run gas oil used in Case 2, but the unit operates at a hydrogen partial pressure at inlet of 54 bar. The feedstock properties are the same as those given in Table 3. The CoMo catalyst, TK-574, is chosen for the 500 wppm product sulfur case, and the NiMoP catalyst,, for all the low sulfur cases. Catalyst cycle length is fixed at 2½ years. Table 5 shows the reactor volumes and chemical hydrogen consumption for the three product sulfur levels. The reactor volumes are relative to the reactor volume required for Case 2, 500 wppm sulfur. The table also shows changes in other key product properties. For Case 3, reducing the product sulfur content from 500 wppm to whilst maintaining cycle length requires a 70% increase in reactor volume, and further reduction from to requires the addition of approximately 45% more reactor volume. The percentage increase is less than for Case 2, and the absolute increase in reactor volume is only 40% that for Case 2. The effect of pressure on the performance of TK-574 is seen by comparing the results for 500 wppm product sulfur in Tables 4 and 5. Increasing pressure by almost 70% results in a reduction in required reactor volume by 35%. At the higher pressure, even the CoMo catalyst exhibits a higher hydrogenation activity as reflected in higher hydrogen consumption, and improved product properties.

6 - 6 - For the remaining product sulfur levels, the difference in required reactor volumes for Case 2 and Case 3 may be explained by the higher reactivity of the NiMoP catalyst in Case 3. At the higher pressure in Case 3, the NiMoP catalyst can remove the inhibiting species enabling desulfurization of the sterically-hindered DBTs via the (quicker) hydrogenation route. 500 wppm TK-574 Relative Reactor Volume Relative Hydrogen Consumption (SOR) Product Properties PAH Content, wt% 1.4 (SOR) 6.3 (EOR) 1.8 (SOR) 5.9 (EOR) 2.1 (SOR) 5.3 (EOR) Density, kg/m (SOR) 848 (SOR) 843 (SOR) CCI, ASTM D (SOR) 51.6 (SOR) 52.5 (SOR) Table 5: Relative Reactor Volume and Product Properties (Case 3) The higher hydrogenation activity of the NiMoP catalyst compared to the CoMo catalyst is reflected in the key product properties for the three product sulfur levels. Although the diesel quality with respect to these properties will deteriorate at EOR (for the same reason as given above), the extent of deterioration will be less because the aromatics equilibria are more favorable at the higher pressure in Case 3. This has been illustrated in Table 6 for the PAH content at both SOR and EOR. The higher level of aromatic saturation obtained in Case 3 may be desirable, depending on future diesel specification requirements. It does, however, give higher operating costs due to higher chemical hydrogen consumption, especially for the low sulfur product levels. Higher hydrogen consumption results in a lower partial pressure of hydrogen at the reactor outlet, adversely affecting the rate of catalyst deactivation and the key product properties. It is therefore necessary to increase the recycle gas to oil ratio in order to maintain outlet hydrogen partial pressure, and this will very often require revamp of the recycle gas system. Yield loss due to cracking is less at the higher space velocities used in Case 3 than in Case 2, and is furthermore countered by volume swell due to a higher hydrogen addition. Revamp vs. Grassroots Unit Case 2 and 3 can be used to illustrate the considerations involved when deciding between revamping a unit or building a grassroots unit. Take the case of an European refiner who has a unit producing a diesel with 500 wppm sulfur at 32 bar hydrogen partial pressure using the feed shown in Table 3. The refiner is faced with having to meet sulfur in 2005, and 10 ppm in Should the refiner choose to revamp the existing unit by adding extra reactor volume i.e. Case 2, or build a new g rassroots unit operating at higher pressure, i.e. Case 3? If the only consideration is to reduce sulfur, the preferred solution would probably be to add reactor volume as in Case 2, but this assumes that the existing gas recycle system can manage the increased pressure drop and that the diesel yield loss due to cracking is acceptable. It may be necessary to revamp of the recycle gas system and the overhead fractionator. This solution if possible will be much cheaper than building a grassroots unit, but the incremental cost of going from 50 ppm to 10 ppm may be higher. If PAH content, density or cetane number are also important, then the refiner may choose to build a new high pressure unit to meet the product sulfur level i.e. the Case 3 solution. This involves more costly investments and the intelligent use of existing equipment can help reduce overall costs 8. If the product sulfur requirement is lowered at a subsequent date, the incremental investment will be lower. In our experience refiners may opt for either solution, depending on their specific needs and possibilities 9. Topsøe has over the past three years designed nineteen ULSD units with specifications of less than sulfur. Twelve of these units are designed to produce less than sulfur diesel,

7 - 7 - of which six are revamps. Conclusion Refiners will need to invest heavily in hydrotreating units as legislation for ultra low sulfur diesel fuel is adopted. For optimum design in which the cost of new units is kept to a minimum and the best use is made of existing equipment, it is necessary to have a deep understanding of the factors governing the removal of the most refractive compounds in diesel fuels. Topsøe has identified the compounds present in diesel feedstocks that inhibit the removal of the most refractive sulfur compounds, and this knowledge can be used to define the correct choice of catalyst for a given service. The choice of catalyst also affects other key diesel properties such as the density, PAH content and Cetane Index, as well as hydrogen consumption and the required treat gas-to-oil ratio. References Yamaguchi, N.D., Update on: Asian Product Demand and Quality, Hart s World Fuel Conference, Washington, DC, September Purvin and Gertz, Hart s 4 th Annual World Fuel Conference, Brussels, May 19-21, Whitehurst, D.D., Knudsen, K.G., Nielsen I.V., Wiwel, P., Zeuthen, P. Preprints, ACS Div. Petr. Chem. 45, No.4, p Knudsen, K.G., Whitehurst, D.D., Zeuthen, P. A detailed understanding of the inhibition effect of organic nitrogen compounds for ultra deep HDS and the consequences for the choice of catalyst, Presented at the AIChE Spring National Meeting, Atalanta, GA, March 5-9, Whitehurst, D.D., Knudsen, K.G., Wiwel, P., Zeuthen, P., Preprints, ACS Div. Petr. Chem., 45, No.2, p Cooper, B.H., Knudsen, K.G., "The importance of Good Liquid Distribution and Proper Selection of Catalyst for Ultra deep Diesel HDS", JPI Petroleum refining Conference, October 19-20, 2000, Tokyo, Japan 8. Bingham, F.E., Christensen, P. Revamping HDS Units to Meet High Quality Diesel Specifications, Asian refinery Technology Conference, March 8-10,2000, Kuala Lumpur, Malaysia 9. De la Fuente, E., Low, G., "Cost-effectively improve hydrotreater designs", Hydrocabon Processing, November, 2001, p 43-46

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