Microsoft Word - B_44_Rippelne_R.doc HUNGARIAN JOURNAL OF INDUSTRIAL CHEMISTRY VESZPRÉM Vol. 39(2) pp. 283-287 (2011) REMOVAL OF HYDROGEN SULFIDE FROM NATURAL GAS, A MOTOR VEHICLE FUEL Á. VÁGÓ1, D. RIPPEL-PETHŐ2 , G. HORVÁTH2, I. TÓTH2, K. OLÁH1 1MOL Hungarian Oil and Gas Company Plc., 1117 Budapest Október 23. utca, HUNGARY E-mail: pethod@almos.uni-pannon.hu 2University of Pannonia, Institute of Chemical and Process Engineering, 8200 Veszprém Egyetem u. 10., HUNGARY Compressed natural gas (CNG) is one of the fossil fuels, and is nothing other than the compressed version of the natural gas extracted by mining. CNG is mostly used for heating and the production of electricity. If used as a fuel for motor vehicles, it entails less emission of CO2 than does the use of gasoline or diesel. Irrespective of usage, the contents of commercial natural gas are strictly regulated by laws. Besides energy density, hydrogen sulfide content for example is a critical quality parameter of natural gas, hence it is strictly regulated. Hydrogen sulfide is extremely corrosive for the pipes. When burning such gases, hydrogen sulfide is converted to sulfur dioxide (SO2) which is harmful for the environment. We have devised a procedure for the replacement of solid adsorbents and amine-containing chemicals in hydrogen sulfide removal that can also be used with gases containing carbon dioxide. The essence of the method is that the natural gas is brought into contact with a dilute solution of NaOH in contact time of less than 1 second. At the beginning of chemisorption, hydrogen sulfide is absorbed 1-2 orders of magnitude faster than carbon dioxide. For the experiments, a laboratory Jet reactor was planned. The efficiency of purification was examined with different hydrogen sulfide containing model gas mixtures with respect to the following parameters: gas volume flow, alkali volume flow and alkali concentration. Keywords: compressed gas, motor vehicle fuel, hydrogen sulfide, chemisortpion, selective extraction Introduction Natural gas is a primary raw material. The typical contents of natural gas are given in Table 1, but they can be different for every gas field. The natural gas consumption of Hungary exceeds 14 billion m3 per annum, which is 70% of the total energy consumption [1]. Table 1: Typical contents of natural gas Component Percentage methane (CH4) 97% ethane (C2H6) 0.919% propane (C3H8) 0.363% butane (C4H10) 0.162% carbon dioxide (CO2) 0.527% oxygen (O2) 0–0.08% nitrogen (N2) 0.936% noble gases (Ar, He, Ne) trace other (e.g..:H2S) 0–0.001% There are 210 well- and/or research sites of natural gas. Most of the wellsites are in the Western Transdanubia and in Eastern Hungary. Domestic resources do not satisfy the consumption, making the country dependent on a significant import, the extent of which is nowadays 80%. Most of the import is arriving from Russia. Fig. 1 illustrates the distribution of natural gas use. The major part of it (45%) is the residential consumption with district heating (more than 6 billion cubic meters per annum). Electricity production (21%) requires 3 billion cubic meters of natural gas per annum. Industrial consumers constitute 33%, while other uses are less than 1%. Industrial consumers 33 % 21 % Electricity production Other 1 % Residential consumption 45 % Figure 1: The distribution of natural gas use Other uses include use as motor vehicle fuel. However, it is important do differentiate between LPG and CNG fuelled vehicles [2]. LPG (Liquefied Petroleum Gas) is a by-product of petroleum oil drilling [3]. Formerly it was usually burned off; nowadays it is sold on the market. As for its contents, it consists of a mixture of 40% propane (C3H8) and 60% butane (C4H10). It is used in fuel tanks at a 284 pressure of 6 bar in a liquefied form. There are approximately 260 LPG tank stations in Hungary. CNG (Compressed Natural Gas) is not a by-product, but the extracted fossil gas. CNG contains 90–92% methane and is in the gaseous state even when densified. The main problem with its use can be caused by imperfect burning, causing the release of greenhouse gases into the atmosphere. This however, is not a threat with a well-set CNG motor vehicle in a good condition. When burning pure methane, one part carbon dioxide (CO2) and two parts water (H2O) in the form of vapor are formed. Compared to traditional fuels, the amount of carbon monoxide (CO) is lower by 60–90%, while the amount of hydrocarbons (CHx) by 40–60%. CNG burns at a lower temperature than gasoline, reducing the amount of nitrous oxides (NOx) by 20–40% in the exhaust gas. In contrast to diesel motor vehicles, there is no release of carcinogenic solid particles. Its advantage compared to LPG is that it is a volatile gas that does not set close to the ground [4]. Several car manufacturers have their own CNG models in Hungary, e.g. Opel (Zafira and Combo), Ford (Focus) and Volvo (S60, S80 and V70). The only setback for CNG fueled vehicles to become widespread is the scarcity of the tank stations. Irrespective of usage, the contents of commercial natural gas are strictly regulated by laws. Besides energy density, hydrogen sulfide content for example is a critical quality parameter of natural gas, hence it is strictly regulated. The amount of hydrogen sulfide can be different for different wellsites, in Hungarian wells, it ranges from 50 to 3000 ppm. The amount of hydrogen sulfide in commercial natural gas, however, cannot exceed 5 ppm. Removal of hydrogen sulfide from natural gases There are several indications for the removal of hydrogen sulfide. The most important is environmental protection, because by burning hydrogen sulfide, sulfur dioxide (SO2) is formed, which is harmful for the environment. The operational indication is that hydrogen sulfide is extremely corrosive for pipes. Since pure natural gas has a higher price, there is also an economical reason. There are several methods for the removal of hydrogen sulfide, such as adsorption, absorption, membrane technology and biological removal. These methods are compared in the followings. For the adsorption methods, the following adsorbents can be used: activated carbon [5, 6], zeolite [7, 8], metal-based (Fe, Ti, Cr, Zn, Al) adsorbents [9, 10] and composites [11, 12]. These adsorbents are efficient at absorbing sulfur, but they have to be regenerated. Most adsorbents can only be regenerated 2 or 3 times consecutively, after this the packing needs to be replaced and disposed of. Membrane separation methods are characterized by ease of installation and use. Membranes are used for hydrogen sulfide removal [13] but their efficiency is not good enough on their own. Because of this, they are used in combined methods [14]. Hydrogen sulfide can be selectively removed by biological ways. However, these systems are hard to control [15]. The absorption techniques use for example alkanol- amines [16, 17]. Their advantage is that they have a high yield and they are regenerable; their disadvantage is that they foam and they are not environmentally friendly. Sodium hydroxide is also used as an absorbent. These techniques can be utilized for the removal of hydrogen sulfide with good efficiency in traditional chemisorption devices [18]. However, with the use of NaOH solution, the selective removal of hydrogen sulfide can be realized for gases containing carbon dioxide as well. The technique based on competitive chemisorption has been known for 55 years now [19]. There are different techniques for the realization of chemisorption. The essence of all of them is that the contact time has to be very short (below 1 sec) and the contact has to be very intensive. This is because (depending on pressure) hydrogen sulfide is absorbed orders of magnitudes faster than carbon dioxide at the beginning of chemisorption [20]. The reaction is exothermic and strongly pH dependent [21]. The above cannot be realized with chemisorbers of classical construction. For alkali consumption, the range of HS- formation is the optimal. For efficiency, a higher, 12-13 pH range is better. Optimization is required of course to determine whether an excess of alkali or several steps are required for the best separation [22, 23]. The intensive contact can be realized by parallel static mixing reactors [24] or by counterflow vaporization [22]. Experimental The natural gas that had to be purified contained 20–100 ppm hydrogen sulfide and 10 (V/V)% carbon dioxide. The aim of the research is the selective removal of hydrogen sulfide. The chosen method is chemisorption with an aqueous solution of sodium hydroxide. Quick and intensive contact is provided by vaporization in the already known process; while the construction enables efficient and fast phase separation to take place. Experimental device Fig. 2 illustrates the experimental device built at the Department of Chemical Engineering at the University of Pannonia. For the experiments, a model gas mixture (1) was produced in a acid-proof gas mixing bridge. The alkali was fed from the alkali vessel (3) with a feeder pump (4), whose volume flow can be regulated. The alkali is vaporized into the reaction space by the gas to be purified (6) through a nozzle (7). The intensively contacted gas and liquid get from the reactor space to the separation space (8). The wastewater (9) can be removed from the 285 separation space, and, after a drop catcher (10), the purified gas (11).There is sampling at both the gas inlet and outlet (12). The hydrogen sulfide and carbon dioxide percentage of the gas is measured by a Dräger X-am 7000 gas analyzer (13). A computer can be attached to the device. With the help of a program, the alkali and gas volume flows can be precisely set. The measured data (temperature, pressure, pressure drop, gas velocity, alkali velocity, gas concentration) can be recorded. Figure 2: Experimental device. 1. gas cylinder, 2. gas inlet, 3. alkali vessel, 4. chemical feeder pump, 5. alkali inlet, 6. reactor space, 7. nozzle, 8. separation space, 9. wastewater removal, 10. drop catcher, 11. outlet of purified gas, 12. gas sampling, 13. gas analyzer The effect of parameters on the efficiency of purification The carbon dioxide concentration of the natural gas was a constant 10 (V/V)% for all experiments, as was the operational pressure of 30 bar. The aim of the experiments is to determine if the incidental fluctuation of the amount of gas or its concentration has any effect on the efficiency of the purification. This is important, because the gas parameters can change when opening or closing a well at a wellsite. The aim is to prove that the procedure can be operated stably, safely and with a near constant efficiency in a given range. The efficiency of the gas purification was examined by changing the following parameters: gas velocity, alkali velocity and alkali concentration. Figs 3 and 4 show the effect of the change of the amount of the gas to be purified. The experiments were carried out with two nozzles: one marked with “a” (Fig. 3) and one marked with “b” (Fig. 4). The velocity of the gas changes in accord with the amount of gas, thus affecting the efficiency of vaporization. Because of this, the nozzles can only be loaded in a given interval without significant changes in efficiency. Nozzle “a” is most efficient at 1100 Nm3/h. 0 10 20 30 40 50 60 70 80 90 100 0 50 100 150 200 250 300 350 400 450 alkali volume flow (cm3/h) ef fic ie nc y (% ) 1.1 Nm3/h 1.5 Nm3/h 1.8 Nm3/h 2.2 Nm3/h 2.8 Nm3/h Figure 3: Change in efficiency as a function of the amount of alkali and gas with nozzle “a”. Fig. 4 illustrates the experiments with nozzle “b”. Nozzle “b” is most efficient at 2200 Nm3/h. As for the experiments of Figures 3 and 4, it can be stated that the decrease of efficiency can be compensated by properly adjusting the velocity of the alkali. With a proper alkali velocity in the range of 1000–3000 Nm3/h, the efficiency of purification changes by ±10%. The adjustment of the amount of alkali to the actual amount of gas can be solved easily. 0 10 20 30 40 50 60 70 80 90 100 0 50 100 150 200 250 300 350 400 450 alkali volume flow (cm3/h) ef fic ie nc y (% ) 1.1 Nm3/h 1.5 Nm3/h 1.8 Nm3/h 2.2 Nm3/h 2.8 Nm3/h Figure 4: Change in efficiency as a function of the amount of alkali and gas with nozzle “b”. Figs 3 and 4 also show the effect of the volume flow of the alkali on the purification efficiencies. As it can be seen, increasing the amount of alkali only increases the efficiency to a certain level. By increasing the amount of the inlet alkali even further, the efficiency is affected negatively. This is due to factors in vaporization. For a given gas velocity, an increasing amount of liquid decreases the efficiency of vaporization. Because of this no intensive contact takes place, also causing the efficiency of purification to decrease. In order to get good efficiency, it is important to choose the appropriate size of nozzles for the given volume flow of the gas, and to set the appropriate alkali velocity as well. Fig. 5 shows the effect of alkali concentration on the efficiency of purification. Only little improvement of efficiency can be achieved by increasing the concentration of the alkali. As long as pH favors the formation of HS, the rate of reaction is minimally dependent on concentration. 286 0 10 20 30 40 50 60 70 80 90 100 0 50 100 150 200 250 300 350 400 450 alkali volume flow (cm3/h) ef fic ie nc y (% ) 1.5 % NaOH 2.5 % NaOH 5 % NaOH Figure 5: Change of efficiency as a function of alkali concentration Fig. 6 illustrates the effect of the concentration of hydrogen sulfide on efficiency. As it can be clearly seen, the concentration of hydrogen sulfide between 20 and 100 ppm does not have an effect on the efficiency of purification (gas volume flow: 1800 Nm3/h). This is of practical importance. If the hydrogen sulfide content of the gas at a given wellsite is fluctuating between the given limits, there is no need to change the technological parameters. The procedure operates with practically the same efficiency throughout. 0 10 20 30 40 50 60 70 80 90 100 0 50 100 150 200 250 300 350 alkali volume flow (cm3/h) ef fic ie nc y (% ) 20 ppm 50 ppm 100 ppm Figure 6: Change of efficiency as a function of the hydrogen sulfide content of the gas The value of specific alkali concentration In addition to the efficiency of purification, the value of the specific alkali concentration (alkali/H2S) is also important. The specific alkali concentration is the proportion of the used alkali and the removed hydrogen sulfide. It gives information about how much more alkali has been used compared to the amount that is required by the chemical reaction. The specific alkali concentration can be decisive when determining the volume flow and concentration of the alkali. Fig. 7 illustrates the values of the specific alkali concentration (with the same gas velocity and 20 ppm hydrogen sulfide content) at different alkali concentrations. As it can be seen, increasing the concentration of the alkali only minimally increases the efficiency. This, however, is enough for the specific alkali concentration to be lower at higher concentrations. The difference is insignificant at lower alkali velocities. At higher alkali velocities, the efficiency decreases, significantly increasing the specific alkali concentration. 0 20 40 60 80 100 120 140 160 0 50 100 150 200 250 300 350 alkali volume flow (cm3/h) al ka li/ H 2S (m ol /m ol ) 1.5 % NaOH 2.5 % NaOH 5 % NaOH Figure 7: Change of specific alkali concentration as a function of alkali concentration Fig. 8 illustrates the effect of hydrogen sulfide concentration on the specific alkali concentration (using the same amount of gas and 2.5 (m/m)% alkali). As we have already seen, the concentration of hydrogen sulfide between 20 and 100 ppm does not have an effect on the efficiency of the purification. However, the specific alkali concentration contains the amount of removed hydrogen sulfide. Hence, the higher the hydrogen sulfide concentration of the gas (in the given range), the lower the specific alkali concentration will be. 0 20 40 60 80 100 120 140 160 180 200 0 50 100 150 200 250 300 350 alkali volume flow (cm3/h) al ka li/ H 2S (m ol /m ol ) 20 ppm H2S 50 ppm H2S 100 ppm H2S Figure 8: Change of specific alkaly concentration as a function of the hydrogen sulfide content of the gas Summary We have devised a procedure for the replacement of solid adsorbents and amine-containing chemicals in hydrogen sulfide removal that can also be used with gases containing carbon dioxide. The essence of the method is that the natural gas is brought into contact with a dilute solution of NaOH in a contact time of less than 1 second. For the experiments, a laboratory Jet reactor was planned. The efficiency of purification was examined by changing the following parameters: gas volume flow, alkali volume flow and alkali concentration. It has been concluded, that for a good efficiency, a nozzle of proper size has to be selected for the given gas volume flow. Also, a proper alkali flow has to be set. The efficiency of purification changes between ±10% at the proper 287 alkali velocity (in the range of 1000–3000 Nm3/h). The concentration of the hydrogen sulfide gas has no effect on the efficiency of the purification between 20 and 100 ppm. Only minimal improvement in efficiency can be achieved by increasing the concentration of the alkali. These observations are of great practical value. The procedure can be operated stably and safely with almost the same efficiency if the parameters fluctuate in the above ranges. ACKNOWLEDGEMENT The authors express their gratitude to the Institute of Chemical Engineering of the University of Pannonia for the financial support of this research. REFERENCES 1. http://www.mol.hu 2. http://www.alternativenergia.hu 3. B. LIANG, S. BALASUBRAMANIAN, B. WANG, A. YANG, D. KENNEDY, V. LE, J. LEGASPI, J. SOUTHERN, LPG characterization and production quantification for oil and gas reservoirs, Journal of Natural Gas Science and Engineering, 2, (2010), 244–252 4. M. U. ASLAM, H. H. MASJUKI, M. A. KALAM, H. ABDESSELAM, T. M. I. MAHLIA, M. A. AMALINA, An experimental investigation of CNG as an alternative fuel for a retrofitted gasoline vehicle, Fuel, 85(5-6), (2006), 717–724 5. M. P. CAL, B. W. STRICKLER, A. A. LIZZIO, S. K. GANGWAL, High temperature hydrogen sulfide adsorption on activated carbon: II. Effects of gas temperature, gas pressure and sorbent regeneration, Carbon, 38(13), (2000), 1767–1774 6. W. H. LEE, P. J. REUCROFT, Vapor adsorption on coal- and wood-based chemically activated carbons: (III) NH3 and H2S adsorption in the low relative pressure range, Carbon, 37(1), (1999), 21–26 7. P. COSOLI, M. FERRONE, S. PRICL, M. FERMEGLIA, Hydrogen sulphide removal from biogas by zeolite adsorption: Part I. GCMC molecular simulations, Chemical Engineering Journal, 145(1), (2008), 86–92 8. J. HOWARD, Z. A. KADIR, The adsorption of H2S on some transition metal exchanged zeolites: An infrared study, Spectrochimica Acta Part A: Molecular Spectroscopy, 41(6), (1985), 825–831 9. H. WANG, D. M. WANG, K. T. CHUANG, A sulfur removal and disposal process through H2S adsorption and regeneration: Breakthrough behaviour investigation, Process Safety and Environmental Protection, 89(1), (2011), 53–60 10. D. NGUYEN-THANH, K. BLOCK, T. J. BANDOSZ, Adsorption of hydrogen sulfide on montmorillonites modified with iron, Chemosphere, 59(3), (2005), 343–353 11. M. SEREDYCH, T. J. BANDOSZ, Reactive adsorption of hydrogen sulfide on graphite oxide/Zr(OH)4 composites, Chemical Engineering Journal, Volume 166(3), (2011), 1032–1038 12. C.-C. HUANG, C.-H. CHEN, S.-M. CHU, Effect of moisture on H2S adsorption by copper impregnated activated carbon, Journal of Hazardous Materials, 136(3), (2006), 866–873 13. S. A. M. MARZOUKA, M. H. AL-MARZOUQIB, N. ABDULLATIFB, Z. M. ISMAIL, Removal of percentile level of H2S from pressurized H2S–CH4 gas mixture using hollow fiber membrane contactors and absorption solvents, Journal of Membrane Science, 360(1-2), (2010), 436–441 14. S. MOHEBI, S. M. MOUSAVI, S. KIANI, Modeling and simulation of sour gas membrane-absorption system: Influence of operational parameters on species removal, Journal of Natural Gas Science and Engineering, 1(6), (2009), 195–204 15. E. M. ELKANZI, Simulation of the Process of Biological Removal of Hydrogen Sulfide from Gas, Proceedings of the 1st Annual Gas Processing Symposium (2009) pp. 266–275 16. M. BOLHÀR-NORDENKAMPF, A. FRIEDL, U. KOSS, T. TORK, Modelling selective H2S absorption and desorption in an aqueous MDEA-solution using a rate-based non-equilibrium approach, Chemical Engineering and Processing, 43(6), (2004), 701–715 17. J.-G. LU, Y.-F. ZHENG, D.-L. HE, Selective absorption of H2S from gas mixtures into aqueous solutions of blended amines of methyldiethanol- amine and 2-tertiarybutylamino-2-ethoxyethanol in a packed column, Separation and Purification Technology, 52(2), (2006), 209–217 18. G. ASTARITA, F. GIOIA, Hydrogen sulphide chemical absorption, Chemical Engineering Science, 19(12), (1964), 963–971 19. R. G. HELTZ, A. L. ROCKLIN, Removal of other acid gases from mixtures containing carbon dioxide, U.S. Patent No. 2,747,962 (1956) 20. J. SIEMAK, M. GELBS, Operating experience with a two-stage H2S scrubber using caustic soda, SPE California Regional Meeting, (1985) 13640-MS 21. R. W. HOHLFELD, Selective Absorption of H2S From Sour Gas, Journal of Petroleum Technology, 32, (1980), 1083–1089 22. V. A. Kent, R. A. Abib, L. H. Kirby, Process for selectively removing hydrogen sulfide , U.S. Patent No. 4,585,630 (1986) 23. R. B. CASSINIS, W. A. FARONE, Improveed H2S Caustic Scubber, SPE Western Regional Meeting, (1997) 38273-MS 24. C. J. WELS, Process for removing sulphide from sour gas stream, U.S. Patent No. 4,395,385 (1983) << /ASCII85EncodePages false /AllowTransparency false /AutoPositionEPSFiles true /AutoRotatePages /None /Binding /Left /CalGrayProfile (Dot Gain 20%) /CalRGBProfile (sRGB IEC61966-2.1) /CalCMYKProfile (U.S. Web Coated \050SWOP\051 v2) /sRGBProfile (sRGB IEC61966-2.1) /CannotEmbedFontPolicy /Error /CompatibilityLevel 1.4 /CompressObjects /Tags /CompressPages true /ConvertImagesToIndexed true /PassThroughJPEGImages true /CreateJDFFile false /CreateJobTicket false /DefaultRenderingIntent /Default /DetectBlends true /DetectCurves 0.0000 /ColorConversionStrategy /CMYK /DoThumbnails false /EmbedAllFonts true /EmbedOpenType false /ParseICCProfilesInComments true /EmbedJobOptions true /DSCReportingLevel 0 /EmitDSCWarnings false /EndPage -1 /ImageMemory 1048576 /LockDistillerParams false /MaxSubsetPct 100 /Optimize true /OPM 1 /ParseDSCComments true /ParseDSCCommentsForDocInfo true /PreserveCopyPage true /PreserveDICMYKValues true /PreserveEPSInfo true /PreserveFlatness true /PreserveHalftoneInfo false /PreserveOPIComments true /PreserveOverprintSettings true /StartPage 1 /SubsetFonts true /TransferFunctionInfo /Apply /UCRandBGInfo /Preserve /UsePrologue false /ColorSettingsFile () /AlwaysEmbed [ true ] /NeverEmbed [ true ] /AntiAliasColorImages false /CropColorImages true /ColorImageMinResolution 300 /ColorImageMinResolutionPolicy /OK /DownsampleColorImages true /ColorImageDownsampleType /Bicubic /ColorImageResolution 300 /ColorImageDepth -1 /ColorImageMinDownsampleDepth 1 /ColorImageDownsampleThreshold 1.50000 /EncodeColorImages true /ColorImageFilter /DCTEncode /AutoFilterColorImages true /ColorImageAutoFilterStrategy /JPEG /ColorACSImageDict << /QFactor 0.15 /HSamples [1 1 1 1] /VSamples [1 1 1 1] >> /ColorImageDict << /QFactor 0.15 /HSamples [1 1 1 1] /VSamples [1 1 1 1] >> /JPEG2000ColorACSImageDict << /TileWidth 256 /TileHeight 256 /Quality 30 >> /JPEG2000ColorImageDict << /TileWidth 256 /TileHeight 256 /Quality 30 >> /AntiAliasGrayImages false /CropGrayImages true /GrayImageMinResolution 300 /GrayImageMinResolutionPolicy /OK /DownsampleGrayImages true /GrayImageDownsampleType /Bicubic /GrayImageResolution 300 /GrayImageDepth -1 /GrayImageMinDownsampleDepth 2 /GrayImageDownsampleThreshold 1.50000 /EncodeGrayImages true /GrayImageFilter /DCTEncode /AutoFilterGrayImages true /GrayImageAutoFilterStrategy /JPEG /GrayACSImageDict << /QFactor 0.15 /HSamples [1 1 1 1] /VSamples [1 1 1 1] >> /GrayImageDict << /QFactor 0.15 /HSamples [1 1 1 1] /VSamples [1 1 1 1] >> /JPEG2000GrayACSImageDict << /TileWidth 256 /TileHeight 256 /Quality 30 >> /JPEG2000GrayImageDict << /TileWidth 256 /TileHeight 256 /Quality 30 >> /AntiAliasMonoImages false /CropMonoImages true /MonoImageMinResolution 1200 /MonoImageMinResolutionPolicy /OK /DownsampleMonoImages true /MonoImageDownsampleType /Bicubic /MonoImageResolution 1200 /MonoImageDepth -1 /MonoImageDownsampleThreshold 1.50000 /EncodeMonoImages true /MonoImageFilter /CCITTFaxEncode /MonoImageDict << /K -1 >> /AllowPSXObjects false /CheckCompliance [ /None ] /PDFX1aCheck false /PDFX3Check false /PDFXCompliantPDFOnly false /PDFXNoTrimBoxError true /PDFXTrimBoxToMediaBoxOffset [ 0.00000 0.00000 0.00000 0.00000 ] /PDFXSetBleedBoxToMediaBox true /PDFXBleedBoxToTrimBoxOffset [ 0.00000 0.00000 0.00000 0.00000 ] /PDFXOutputIntentProfile () /PDFXOutputConditionIdentifier () /PDFXOutputCondition () /PDFXRegistryName () /PDFXTrapped /False /Description << /CHS /CHT /DAN /DEU /ESP /FRA /ITA /JPN /KOR /NLD (Gebruik deze instellingen om Adobe PDF-documenten te maken die zijn geoptimaliseerd voor prepress-afdrukken van hoge kwaliteit. De gemaakte PDF-documenten kunnen worden geopend met Acrobat en Adobe Reader 5.0 en hoger.) /NOR /PTB /SUO /SVE /ENU (Use these settings to create Adobe PDF documents best suited for high-quality prepress printing. Created PDF documents can be opened with Acrobat and Adobe Reader 5.0 and later.) >> /Namespace [ (Adobe) (Common) (1.0) ] /OtherNamespaces [ << /AsReaderSpreads false /CropImagesToFrames true /ErrorControl /WarnAndContinue /FlattenerIgnoreSpreadOverrides false /IncludeGuidesGrids false /IncludeNonPrinting false /IncludeSlug false /Namespace [ (Adobe) (InDesign) (4.0) ] /OmitPlacedBitmaps false /OmitPlacedEPS false /OmitPlacedPDF false /SimulateOverprint /Legacy >> << /AddBleedMarks false /AddColorBars false /AddCropMarks false /AddPageInfo false /AddRegMarks false /ConvertColors /ConvertToCMYK /DestinationProfileName () /DestinationProfileSelector /DocumentCMYK /Downsample16BitImages true /FlattenerPreset << /PresetSelector /MediumResolution >> /FormElements false /GenerateStructure false /IncludeBookmarks false /IncludeHyperlinks false /IncludeInteractive false /IncludeLayers false /IncludeProfiles false /MultimediaHandling /UseObjectSettings /Namespace [ (Adobe) (CreativeSuite) (2.0) ] /PDFXOutputIntentProfileSelector /DocumentCMYK /PreserveEditing true /UntaggedCMYKHandling /LeaveUntagged /UntaggedRGBHandling /UseDocumentProfile /UseDocumentBleed false >> ] >> setdistillerparams << /HWResolution [2400 2400] /PageSize [612.000 792.000] >> setpagedevice