215 results on '"Brandin, Jan"'
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2. Fischer-Tropsch synthesis—Investigation of the deactivation of a Co catalyst by exposure to aerosol particles of potassium salt
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Gavrilović, Ljubiša, Brandin, Jan, Holmen, Anders, Venvik, Hilde J., Myrstad, Rune, and Blekkan, Edd A.
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- 2018
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3. The effect of aerosol-deposited ash components on a cobalt-based Fischer–Tropsch catalyst
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Gavrilović, Ljubiša, Brandin, Jan, Holmen, Anders, Venvik, Hilde J., Myrstad, Rune, and Blekkan, Edd A.
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- 2019
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4. Deactivation and Characterization of SCR Catalysts Used in Municipal Waste Incineration Applications
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Brandin, Jan G. M. and Odenbrand, C. U. Ingemar
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- 2017
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5. Poisoning of SCR Catalysts used in Municipal Waste Incineration Applications
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Brandin, Jan G. M. and Odenbrand, C. U. Ingemar
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- 2017
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6. Pore Condensation in Glycerol Dehydration: Modification of a Mixed Oxide Catalyst
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Hulteberg, Christian, Leveau, Andreas, and Brandin, Jan Gunnar Meo
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- 2017
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7. Modeling of soot formation during partial oxidation of producer gas
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Svensson, Helena, Tunå, Per, Hulteberg, Christian, and Brandin, Jan
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- 2013
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8. Selective catalytic oxidation of ammonia by nitrogen oxides in a model synthesis gas
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Tunå, Per and Brandin, Jan
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- 2013
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9. High-temperature and high-concentration SCR of NO with NH3: Application in a CCS process for removal of carbon dioxide
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Brandin, Jan G.M., Hulteberg, Christian P., and Odenbrand, C.U. Ingemar
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- 2012
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10. Unit operations for production of clean hydrogen-rich synthesis gas from gasified biomass
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Brandin, Jan and Liliedahl, Truls
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- 2011
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11. High temperature water-gas shift step in the production of clean hydrogen rich synthesis gas from gasified biomass
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Einvall, Jessica, Parsland, Charlotte, Benito, Patricia, Basile, Francesco, and Brandin, Jan
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- 2011
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12. Pore Condensation in Glycerol Dehydration
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Hulteberg, Christian, Leveau, Andreas, and Brandin, Jan Gunnar Meo
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- 2013
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13. Deactivation of a Ni-Based Reforming Catalyst During the Upgrading of the Producer Gas, from Simulated to Real Conditions
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Albertazzi, Simone, Basile, Francesco, Barbera, Davide, Benito, Patricia, Brandin, Jan, Einvall, Jessica, Fornasari, Giuseppe, Trifirò, Ferruccio, and Vaccari, Angelo
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- 2011
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14. Shift catalysts in biomass generated synthesis gas
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Kirm, Ilham, Brandin, Jan, and Sanati, Mehri
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- 2007
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15. Preface
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Hulteberg, Christian, Odenbrand, Ingemar, Gustafson, Johan, Brandin, Jan, and Lundgren, Edvin
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- 2017
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16. Ba-Ni-Hexaaluminate as a New Catalyst in the Steam Reforming of 1-Methyl Naphthalene and Methane
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Parsland, Charlotte, primary, Ho, Phuoc Hoang, additional, Benito, Patricia, additional, Larsson, Ann-Charlotte, additional, Fornasari, Giuseppe, additional, and Brandin, Jan, additional
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- 2019
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17. Deactivation of the cobalt fischer-tropsch catalyst : a kinetic study
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Gavrilović, Ljubiša, Brandin, Jan, Holmen, Anders, Venvik, Hilde J., Myrstad, Rune, Rout, Kumar Ranjan, Rytter, Erling, Hillestad, Magne, Blekkan, Edd Anders, Gavrilović, Ljubiša, Brandin, Jan, Holmen, Anders, Venvik, Hilde J., Myrstad, Rune, Rout, Kumar Ranjan, Rytter, Erling, Hillestad, Magne, and Blekkan, Edd Anders
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- 2019
18. The effect of aerosol-deposited ash components on a cobalt-based Fischer–Tropsch catalyst
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Gavrilovic, Lubisa, Brandin, Jan, Holmen, Anders, Venvik, Hild J., Myrstad, Rune, Blekkan, Edd A., Gavrilovic, Lubisa, Brandin, Jan, Holmen, Anders, Venvik, Hild J., Myrstad, Rune, and Blekkan, Edd A.
- Abstract
The effect of ash salts on Co-based Fisher–Tropsch catalysts was studied using an aerosol deposition technique. The major elements in the ash were found to be K, S and Cl. The ash was deposited on a calcined catalyst as dry particles with an average diameter of approx. 350 nm. The loading of ash particles was varied by varying the time of exposure to the particles in a gas stream. Catalyst characterization did not reveal significant differences in cobalt dispersion, reducibility, surface area, pore size, or pore volume between the reference and the catalysts with ash particles deposited. Activity measurements showed that following a short exposure to the mixed ash salts (30 min), there were no significant loss of activity, but a minor change in selectivity of the catalyst . Extended exposure (60 min) led to some activity loss and changes in selectivity. However, extending the exposure time and thus the amount deposited as evidenced by elemental analysis did not lead to a further drop in activity. This behavior is different from that observed with pure potassium salts, and is suggested to be related to the larger size of the aerosol particles deposited. The large aerosol particles used here were probably not penetrating the catalyst bed, and to some extent formed an external layer on the catalyst bed. The ash salts are therefore not able to penetrate to the pore structure and reach the Co active centers, but are mixed with the catalyst and detected in the elemental analysis.
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- 2019
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19. Deactivation of oxidation and SCR catalysts used in flue gas cleaning by exposure to aerosols of high- and low melting point salts, potassium salts and zinc chloride
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Moradi, Farokhbag, Brandin, Jan, Sohrabi, Morteza, Faghihi, Mostafa, and Sanati, Mehri
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- 2003
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20. Deactivation of Co-based Fischer-Tropsch catalyst by aerosol deposition of potassium salts
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Gavrilovic, Ljubisa, Brandin, Jan, Holmen, Anders, Venvik, Hilde, Myrstad, R., Blekkan, Edd, Gavrilovic, Ljubisa, Brandin, Jan, Holmen, Anders, Venvik, Hilde, Myrstad, R., and Blekkan, Edd
- Abstract
A 20%Co/0.5%Re/γAl2O3 Fischer-Tropsch catalyst was poisoned by four potassium salts (KNO3, K2SO4, KCl, K2CO3) using the aerosol deposition technique, depositing up to 3500 ppm K as solid particles. Standard characterization techniques (H2 Chemisorption, BET, TPR) showed no difference between treated samples and their unpoisoned counterpart. The Fischer-Tropsch activity was investigated at industrially relevant conditions (210 °C, H2:CO = 2:1, 20 bar). The catalytic activity was significantly reduced for samples exposed to potassium, and the loss of activity was more severe with higher potassium loadings, regardless of the potassium salt used. A possible dual deactivation effect by potassium and the counter-ion (chloride, sulfate) is observed with the samples poisoned by KCl and K2SO4. The selectivity towards heavier hydrocarbons (C5+) was slightly increased with increasing potassium loading, while the CH4 selectivity was reduced for all the treated samples. The results support the idea that potassium is mobile under FT conditions. The loss of activity was described by simple deactivation models which imply a strong non-selective poisoning by the potassium species.
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- 2018
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21. Deactivation and Characterization of SCR Catalysts Used in Municipal Waste Incineration Applications
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Brandin, Jan, Odenbrand, Ingemar, Brandin, Jan, and Odenbrand, Ingemar
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Catalysts used for selective catalytic reduction were deactivated for various times in a slipstream from a municipal solid waste incineration plant and then characterized. The activity for NO reduction with NH3 was measured. The Brunauer–Emmett–Teller surface areas were determined by N2 adsorption from which the pore size distributions in the mesopore region were obtained. Micropore areas and volumes were also obtained. The composition of fresh and deactivated catalysts as well as fly ash was determined by atomic absorption spectroscopy and scanning electron microscopy with energy dispersive X-ray analysis. The changes in surface area (8% decrease in BET surface area over 2311 h) and pore structure were small, while the change in activity was considerable. The apparent pre-exponential factor was 1.63 × 105 (1/min) in the most deactivated catalyst, compared to 2.65 × 106 (1/min) in the fresh catalyst, i.e. a reduction of 94%. The apparent activation energy for the fresh catalyst was 40 kJ/mol, decreasing to 27 kJ/mol with increasing deactivation. Characterization showed that catalytic poisoning is mainly due to decreased acidity of the catalyst caused due to increasing amounts of Na and K.
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- 2018
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22. A review of the thermo-chemical conversion of biomass into biofuels – Focusing on gas cleaning and up-grading process steps
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Brandin, Jan, Hulteberg, Christian, and Kušar, Henrik
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- 2017
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23. A review of thermo-chemical conversion of biomass into biofuels : focusing on gas cleaning and up-grading process steps
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Brandin, Jan, Hulteberg, Christain, and Kusar, Henrik
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gas cleaning ,biomass ,gasification ,biofuel ,thermo-chemical ,up-grading ,Energy Systems ,Energisystem - Abstract
It is not easy to replace fossil-based fuels in the transport sector, however, an appealing solution is to use biomass and waste for the production of renewable alternatives. Thermochemical conversion of biomass for production of synthetic transport fuels by the use of gasification is a promising way to meet these goals. One of the key challenges in using gasification systems with biomass and waste as feedstock is the upgrading of the raw gas produced in the gasifier. These materials replacing oil and coal contain large amounts of demanding impurities, such as alkali, inorganic compounds, sulphur and chlorine compounds. Therefore, as for all multi-step processes, the heat management and hence the total efficiency depend on the different clean-up units. Unfortunately, the available conventional gas filtering units for removing particulates and impurities, and also subsequent catalytic conversion steps have lower optimum working temperatures than the operating temperature in the gasification units. This report focuses on on-going research and development to find new technology solutions and on the key critical technology challenges concerning the purification and upgrading of the raw gas to synthesis gas and the subsequent different fuel synthesis processes, such as hot gas filtration, clever heating solutions and a higher degree of process integration as well as catalysts more resistant towards deactivation. This means that the temperature should be as high as possible for any particular upgrading unit in the refining system. Nevertheless, the temperature and pressure of the cleaned synthesis gas must meet the requirements of the downstream application, i.e. Fischer-Tropsch diesel or methanol. Before using the gas produced in the gasifier a number of impurities needs to be removed. These include particles, tars, sulphur and ammonia. Particles are formed in gasification, irrespective of the type of gasifier design used. A first, coarse separation is performed in one or several cyclone filters at high temperature. Thereafter bag-house filters (e.g. ceramic or textile) maybe used to separate the finer particles. A problem is, however, tar condensation in the filters and there is much work performed on trying to achieve filtration at as high a temperature as possible. The far most stressed technical barriers regarding cleaning of the gases are tars. To remove the tar from the product gas there is a number of alternatives, but most important is that the gasifier is operated at optimal conditions for minimising initial tar formation. In fluid bed and entrained flow gasification a first step may be catalytic tar cracking after particle removal. In fluid bed gasification a catalyst, active in tar cracking, may be added to the fluidising bed to further remove any tar formed in the bed. In this kind of tar removal, natural minerals such as dolomite and olivine, are normally used, or catalysts normally used in hydrocarbon reforming or cracking. The tar can be reformed to CO and hydrogen by thermal reforming as well, when the temperature is increased to 1300ºC and the tar decomposes. Another method for removing tar from the gas is to scrub it by using hot oil (200-300ºC). The tar dissolves in the hot oil, which can be partly regenerated and the remaining tar-containing part is either burned or sent back to the gasifier for regasification. Other important aspects are that the sulphur content of the gas depends on the type of biomass used, the gasification agent used etc., but a level at or above 100 ppm is not unusual. Sulphur levels this high are not acceptable if there are catalytic processes down-stream, or if the emissions of e.g. SO2 are to be kept down. The sulphur may be separated by adsorbing it in ZnO, an irreversible process, or a commercially available reversible adsorbent can be used. There is also the possibility of scrubbing the gas with an amine solution. If a reversible alternative is chosen, elementary sulphur may be produced using the Claus process. Furthermore, the levels of ammonia formed in gasification (3,000 ppm is not uncommon) are normally not considered a problem. When combusting the gas, nitrogen or in the worst case NOx (so-called fuel NOx) is formed; there are, however, indications that there could be problems. Especially when the gasification is followed by down-stream catalytic processes, steam reforming in particular, where the catalyst might suffer from deactivation by long-term exposure to ammonia. The composition of the product gas depends very much on the gasification technology, the gasifying agent and the biomass feedstock. Of particular significance is the choice of gasifying agent, i.e. air, oxygen, water, since it has a huge impact on the composition and quality of the gas, The gasifying agent also affects the choice of cleaning and upgrading processes to syngas and its suitability for different end-use applications as fuels or green chemicals. The ideal upgraded syngas consists of H2 and CO at a correct ratio with very low water and CO2 content allowed. This means that the tars, particulates, alkali salts and inorganic compounds mentioned earlier have to be removed for most of the applications. By using oxygen as the gasifying agent, instead of air, the content of nitrogen may be minimised without expensive nitrogen separation. In summary, there are a number of uses with respect to produced synthesis gas. The major applications will be discussed, starting with the production of hydrogen and then followed by the synthesis of synthetic natural gas, methanol, dimethyl ether, Fischer-Tropsch diesel and higher alcohol synthesis, and describing alternatives combining these methods. The SNG and methanol synthesis are equilibrium constrained, while the synthesis of DME (one-step route), FT diesel and alcohols are not. All of the reactions are exothermal (with the exception of steam reforming of methane and tars) and therefore handling the temperature increase in the reactors is essential. In addition, the synthesis of methanol has to be performed at high pressure (50-100 bar) to be industrially viable. There will be a compromise between the capital cost of the whole cleaning unit and the system efficiency, since solid waste, e.g. ash, sorbents, bed material and waste water all involve handling costs. Consequently, installing very effective catalysts, results in unnecessary costs because of expensive gas cleaning; however the synthesis units further down-stream, especially for Fischer-Tropsch diesel, and DME/methanol will profit from an effective gas cleaning which extends the catalysts life-time. The catalyst materials in the upgrading processes essentially need to be more stable and resistant to different kinds of deactivation. Finally, process intensification is an important development throughout chemical industries, which includes simultaneous integration of both synthesis steps and separation, other examples are advanced heat exchangers with heat integration in order to increase the heat transfer rates. Another example is to combine exothermic and endothermic reactions to support reforming reactions by using the intrinsic energy content. For cost-effective solutions and efficient application, new solutions for cleaning and up-grading of the gases are necessary. Det är en stor utmaning att ersätta fossila bränslen inom transportsektorn, en tilltalande lösning är att använda biomassa och avfall för produktion av förnyelsebara drivmedel. Termokemisk omvandling av biomassa är ett lovande sätt för att producera olika sorters syntetiska drivmedel, då främst genom förgasningsteknik. En av de främsta utmaningarna i att använda termokemisk omvandling av biomassa och avfall är en rening och uppgradering av rågasen som produceras i förgasaren. Dessa material som är tänkta att ersätta olja och kol innehåller betydande mängder av alkaliska-, oorganiska-, svavel- och klor-föreningar. De olika renings- och uppgraderingsstegen påverkar den totala verkningsgraden på hela processen, därför blir hanteringen av värme i de olika process strömmarna viktiga, som för alla processer i flera steg. Dessvärre, har de tillgängliga konventionella gas filtreringsenheterna för att ta bort partiklar och orenheter, och även efterföljande katalytiska omvandlingssteg, lägre optimala arbetstemperaturer än driftstemperaturen hos förgasningsenheterna. Denna rapport fokuserar på pågående forskning och utveckling för att hitta ny teknik och lösningar när det gäller rening och uppgradering av rågas till syntesgas, samt efterföljande bränslesyntesprocesser, såsom hetgas-filtrering, smarta uppvärmnings lösningar och högre grad av integrationsprocess, samt katalysatorer som är mer tåliga mot deaktivering. Detta innebär att temperaturen bör vara så hög som möjligt för varje enskild renings- och en uppgraderingsenhet, likväl måste temperaturen och trycket hos den renade syntesgasen uppfylla kraven för nedströms bränslesyntes, d.v.s. Fischer-Tropsch-diesel eller metanol. Ett antal orenheter behöver tas bort innan gasen som producerats i förgasaren kan användas, dessa inkluderar partiklar, tjäror, svavelföreningar och ammoniak. Partiklar bildas alltid vid förgasning, oberoende av vilken typ av förgasningsteknik som används, en första grovseparation utförs i en eller flera cyklonfilter vid höga temperaturer. För att separera de finare partiklarna används därefter olika keramiska- eller textilfilter, ett problem är dock kondensation av tjära i filtren, mycket arbete utförs på att försöka uppnå filtrering vid så hög temperatur som möjligt, så att man slipper tjärproblemen. Det största hindret när det gäller rening och uppgradering av gaserna är tjära. För att bli av med tjäran från produktgasen finns ett antal olika alternativ, men det väsentligaste är att själva förgasaren drivs vid optimala förhållanden för att minimera att tjära bildas överhuvudtaget. För förgasning med fluidiserad bädd och entrained flowförgasning skulle det första steget kunna vara katalytisk tjärkrackning efter att ha avlägsnat alla partiklar. Vid förgasning i fluidiserad bädd kan aktiva katalysatorer tillsättas till den fluidiserande bädden som kan kracka tjäran redan i bädden och hindra att ytterligare eventuell tjära bildas. Katalysatorer som används är främst naturliga mineraler, såsom dolomit och olivin, dessa användes normalt vid reformering eller krackning av kolväten. Tjäran kan reformeras till vätgas och kolmonoxid genom termisk reformering såsom när temperaturen höjs till 1300ºC och tjäran sönderfaller. En annan metod för att avlägsna tjära från gasen är att tvätta gasen med hjälp av het olja (200-300ºC). Tjäran löser sig i den heta oljan, som delvis kan vara regenererad och den återstående tjärhaltiga delen kan antingen brännas eller återföras till förgasaren för förgasning. Svavelföreningar är en annan viktig kontaminering som behöver tas bort ur gasen, svavelhalten i gasen beror främst på vilken typ av biomassa som används. Nivåer över 100 ppm inte är ovanligt och är inte acceptabelt för efterföljande nedströms katalytiska processer, eller om utsläppen av t.ex. SO2 ska hållas nere. Svavel kan separeras genom adsorption med ZnO som är en irreversibel process, eller genom kommersiellt tillgängliga reversibla adsorbenter som kan användas. Ytterligare alternativ är att tvätta/skrubba gasen med en aminlösning. Om ett reversibelt alternativ används kan elementärt svavel framställas med hjälp av Claus-processen. Ammoniak bildas vid förgasning och nivåer runt 3000 ppm är inte ovanligt, men anses vanligtvis inte ett problem efterföljande nedströms processer. Om gasen förbränns, kan dock kväve eller i värsta fall NOx (så kallad bränsle NOx) bildas. Det finns dock indikationer på att problem kan uppstå, speciellt när förgasning följs av nedströms katalytiska processer, exempelvis vid ångreformering där katalysatorn kan deaktiveras vid långvarig exponering för ammoniak Sammansättningen på produktgasen beror framförallt på valet av förgasningsteknik, vilket förgasningsmedel som används, samt viken sorts biomassa sam används. Valet av förgasningsmedel, dvs. luft, syre, vatten, är extra viktigt eftersom det har en direkt inverkan på sammansättningen och kvaliteten hos gasen. Valet av förgasningsmedel påverkar också vilka renings- och uppgraderingsprocesser som kan användas och lämpar sig bäst för olika slutanvändningstillämpningar som t.ex. drivmedel eller för gröna kemikalier. Idealt består en syntesgas som är uppgraderad av vätgas och kolmonoxid i korrekt förhållande, med mycket låga halter vatten och koldioxid. Detta innebär att tjäror, partiklar, alkalisalter och oorganiska föreningar, som nämnts tidigare, måste avlägsnas för de flesta tillämpningarna. Genom att använda syre som förgasningsmedel, i stället för luft, kan innehållet av kväve i gasen minimeras, så man undviker efterföljande dyrbar separation av kväve. Sammanfattningsvis finns det ett antal olika användningsområden för olika producerade syntesgaser. De olika tillämpningarna kommer att diskuteras i rapporten med början med produktion av vätgas, följt av framställning av syntetisk naturgas (SNG), metanol, dimetyleter, Fischer-Tropsch-diesel och syntes av högre alkoholer, samt beskrivningar av metoder som kombinerar dessa. Processystemen är olika där syntes av SNG och metanol begränsas jämvikt, medan syntes av dimetyleter, (DME), FT-diesel och alkoholer inte är jämviktsberoende. Samtliga reaktioner är exoterma, med undantag för ångreformering av metan och tjäror, vilket medför att det är viktigt att kontrollera temperaturökningen i reaktorerna. Dessutom måste syntes av metanol utföras vid högt tryck (50-100 bar) för att vara industriellt gångbar. För att hålla nere kapitalkostnaderna för hela reningssystemet och systemets effektivitet behöver man kompromissa, eftersom hanteringen av fast avfall, t.ex. aska, absorberande medel, bäddmaterial och avloppsvatten alla innebär kostnader. Att installera väldigt effektiva katalysatorer resulterar i dyrare gasrening på grund av onödiga kostnader, men nedströms syntesprocesser kommer att dra nytta av effektiv gasrening som förlänger katalysatorernas livstid, särskilt för Fischer-Tropsch-diesel, och DME/metanol syntes. Generellt måste katalysatorerna i de olika uppgraderingsprocesserna vara mer stabila och motståndskraftiga mot olika typer av deaktivering. Slutligen är process-intensifiering ett viktigt område för utveckling inom hela kemiindustrin som bland annat omfattar integration av både syntes och separationssteg, med olika former av avancerad värmeväxling med värmeintegration för att öka värmeöverföringshastigheten, och att kombinera exoterma och endoterma reaktioner. Därför är det nödvändigt med nya innovativa lösningar för rening och uppgradering av gaserna för att få fram kostnadseffektiva och effektiva tillämpningar.
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- 2017
24. Deactivation of Co-Based Fischer–Tropsch Catalyst by Aerosol Deposition of Potassium Salts
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Gavrilović, Ljubiša, primary, Brandin, Jan, additional, Holmen, Anders, additional, Venvik, Hilde J., additional, Myrstad, R., additional, and Blekkan, Edd A., additional
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- 2018
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25. Preface : Special issue of Topics in Catalysis constitutes the Proceedings of the 17th Nordic Symposium of Catalysis
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Hulteberg, Christian, Odenbrand, Ingemar, Gustafson, Johan, Brandin, Jan, Lundgren, Edvin, Hulteberg, Christian, Odenbrand, Ingemar, Gustafson, Johan, Brandin, Jan, and Lundgren, Edvin
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- 2017
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26. Poisoning of SCR Catalysts used in Municipal Waste Incineration Applications
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Brandin, Jan, Odenbrand, Ingemar, Brandin, Jan, and Odenbrand, Ingemar
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A commercial vanadia, tungsta on titania SCRcatalyst was poisoned in a side stream in a waste incinerationplant. The effect of especially alkali metal poisoning was observed resulting in a decreased activity at long times of exposure. The deactivation after 2311 h was 36% whilet he decrease in surface area was only 7.6%. Thus the major cause for deactivation was a chemical blocking of acidic sites by alkali metals. The activation–deactivation model showed excellent agreement with experimental data. The model suggests that the original adsorption sites, from the preparation of the catalyst, are rapidly deactivated but are replaced by a new population of adsorption sites due to activation of the catalyst surface by sulphur compounds (SO2, SO3) in the flue gas.
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- 2017
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27. Ni-substituted Ba-hexaaluminate as a new catalytic material in steam reforming of tars
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Parsland, Charlotte, Brandin, Jan, Benito, Patricia, Hoang Ho, Phuoc, Fornasari, Guiseppe, Parsland, Charlotte, Brandin, Jan, Benito, Patricia, Hoang Ho, Phuoc, and Fornasari, Guiseppe
- Published
- 2017
28. Deactivation of SCR catalysts used in municipal waste incineration applications
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Odenbrand, Ingemar and Brandin, Jan
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Other Chemical Engineering ,sulfur activation ,Catalyst deactivation ,Selective Catalytic Reduction ,SCR ,waste combustion ,Annan kemiteknik - Published
- 2016
29. Influence of potassium species on Co based Fischer-Tropsch-catalyst.
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Gavrilovic, Ljubisa, Blekkan, Ed Anders, Venvik, H.J., Holmen, Anders, Brandin, Jan, Gavrilovic, Ljubisa, Blekkan, Ed Anders, Venvik, H.J., Holmen, Anders, and Brandin, Jan
- Abstract
1. Introduction The purpose of this work is better understanding of the alkali influence on Co-based F-T catalyst. Since potassium is one of the elements that can be present in syngas from biomass[1], one of the questions is how potassium species affect the Co catalyst. From previous work it has been shown that alkali species act as poisons, thus deactivating catalysts[2]. Most previous work in this group[3][4] and by others[5] has concerned Co catalysts that were exposed to potassium species by incipient wetness impregnation, which is essentially different from the real behaviour during the gasification process where the species will mainly be in the vapor phase. In the present work we study potassium influence on a Co-based catalyst, using aerosol technology as a new method for potassium deposition on the Co surface. 2. Experimental 4 different potassium salts were deposited using aerosol deposition on 20%Co/0.5%Re/γAl2O3. The amount of potassium salts deposited were determined using ICP analysis. Potassium salts were chosen from studies of the gases from biomass gasification[6]. These are K2SO4, KCl, KNO3 and K2CO3. KNO3 will be reduced to KOH during biomass gasification, but since in these experiments temperature was not so high and there was no H2/CO, most likely KNO3 will be deposited as such on the Co surface. BET N2 adsorption, H2 chemisorption, temperature programmed reduction (TPR) were used to characterize all the poisoned catalysts. Fischer Tropsch activity and selectivity measurements were performed at the in house build set-up, at 210°C, 20 bar and at H2:CO ratio of 2.1. The GHSV was consistently varied to maintain comparable CO conversion levels between 20-50%. A detailed description of the setup and procedures can be found elsewhere[3]. 3. Results The potassium species were deposited using aerosol technology in the apparatus shown in Fig. 1. Potassium salts are dissolved in deionized water and the solution is placed inside the atomizer, which pro
- Published
- 2016
30. Aerosolkatalysatorer för industriell gasrening
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Brandin, Jan, Strand, Michael, Ali, Sharafat, Brandin, Jan, Strand, Michael, and Ali, Sharafat
- Abstract
Aerosol catalysts – small particles (with aerodynamic diameter up to 100 m) of catalytically active material suspended in gas – were examined for the intended use of NOx reduction with ammonia (SCR) in smaller industrial plants and boilers as an alternative to SNCR. The aerosol particles are intended to be injected into the flue gas at high temperature, together with ammonia/urea, and then separated on a particulate filter (bag‐type filter) at low temperature. The NOx reduction can occur during the pneumatic transport in the boiler or/and on the catalytically active filter cake. The catalysts must have sufficiently high activity in order to keep down their consumption, they must be cheap enough to be used as a consumable item, and must be harmless to humans and the environment. Two materials were developed during the work as possible candidates: natural zeolites and a FeSO4/activated carbon‐based catalyst. Cost estimates, for a hypothetical 1 MWth plant, shows that a NOx reduction close to 50% economically justify the introduction of SNCR for small plants (<25 GWh, NOx reductions levels between 30‐50% and 2 in stoichiometric ratio), both for the use of urea and liquid anhydrous ammonia with the percent NOx fee of 50 SEK/kg. The result is modest, at best 15‐20% cost reduction compared to no action. Raised tariffs to 60 SEK/kg NOx will improved the situation, but the results are still modest. When the aerosol catalysts was used in the cost estimate, and an assumed NOx reduction degree of 85% was supposed to be reached, good results were obtained at low catalyst costs (0.5‐2 SEK/kg). However the plant can handle at most a cost of 4 SEK/kg. Estimated cost for the aerosol catalyst is in the range of 10 SEK/kg. In order to be economically attractive, the catalyst should be recycled, thereby lowering the cost of catalyst consumption., I detta arbete har aerosolkatalysatorer, det vill säga små partiklar (med aerodynamisk diameter upp till 100 µm) av katalytiskt aktiva material, suspenderade i gas, undersökts med tänkt användning för NOx-reduktion med ammoniak (SCR) i mindre industriella anläggningar och pannor som ett alternativ till SNCR. Aerosolpartiklarna är avsedda att injiceras i rökgasen vid hög temperatur, tillsammans med ammoniak/urea, och avskiljs på ett partikelfilter, av slangfiltertyp, vid låg temperatur. Reduktion av NOx kan då ske dels vid den pneumatiska transporten av katalysatorn genom pannan och dels i den katalytiskt aktiva filterkaka som byggs upp på slangfiltret. Katalysatorerna måste ha tillräckligt hög aktivitet, vid den pneumatiska transporten, för att begränsa förbrukningen, vara tillräckligt billiga för att kunna användas som förbrukningsvara och vara ofarliga för människor och miljö. Två material togs fram under arbetet som tänkbara kandidater; naturliga zeoliter och en FeSO4/träkolkatalysator. Kostnadsuppskattningar för en tänkt 1 MWth-anläggning, visar att det behövs närmre 50 % reduktionsgrad för att ekonomiskt motivera införande av SNCR för små anläggningar (<25 GWh, NOx-reduktion mellan 30-50 % och 2 i stökiometri), detta både för användning av urea och flytande vattenfri ammoniak med dagens NOx-avgift. Resultatet är måttligt, som bäst nås 15-20 % kostnadsreduktion jämfört med utan åtgärd. Höjs avgiften till 60 SEK/kg NOx, förbättras situationen, men resultaten är fortfarande måttliga (20-25 % kostnadsreduktion). Vid användande av aerosolkatalysatorer, och en reduktionsgrad av 85 %, fås bra utfall vid låga katalysatorkostnader (0.5-2 SEK/kg), men anläggningen klarar på sin höjd en kostnad på 4 SEK/kg. Uppskattade priser för aerosolkatalysatorn är i storleksordningen 10 SEK/kg. För att processen ska bli ekonomiskt intressant, måste katalysatorn kunna recirkuleras för att ge en sänkt kostnad för katalysatorförbrukning.
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- 2016
31. Reneweble Propane : Tayloring WO3/ZrO2 catalyst for the dehydration of glycerol to acrolein.
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Hulteberg, Christian, Leveau, Andreas, Brandin, Jan, Hulteberg, Christian, Leveau, Andreas, and Brandin, Jan
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- 2016
32. Catalyst choise and considerations in the conversion of Glucose to glycerol.
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Nørregård, Øyvind, Hulteberg, Christian, Brandin, Jan, Leveau, Andreas, Nørregård, Øyvind, Hulteberg, Christian, Brandin, Jan, and Leveau, Andreas
- Abstract
Through the 20th century the use of glycerine has mainly been focused to the food industry, the cosmetic industry and the pharmaceutical industry. The required volumes for these industries can’t be compared with the larger bulk chemicals produced today. These low requirements together with the increased glycerine production, associated with the biodiesel production from which glycerine is a large by-product, has forced the prices down to approximately 100-150 $/tonne. This low cost crude glycerine has been an initiator for developing methods on how to convert the glycerine to more usable products. A proposed method by the company Biofuel Solutions has been to convert the glycerine into bio-LPG. With the EU directives stating that at least 10 % of the fuels in the transport sector should come from renewable sources this route may turn out favourable. This will though cause a large increase in demand as one of the few new ways to provide bio-LPG and thus increase in price, which will require new ways to produce glycerine. With a possible increased demand on glycerine a proposed route to produce glycerine is via catalytic hydrogenation of glucose to sorbitol and further catalytic hydrogenolysis of sorbitol to glycerine. The production of sorbitol from glucose is today already industrialised with large producers such as Roquette Frères, Cargill and SPI Polyols. The industrial process is historically made batch wise with low cost Raney-nickel catalyst but with the development of good selectivity catalysts with no leaching problems it is assumed that todays’ production is mainly operating with catalyst with noble metals as the active metal, such as ruthenium, in a continuous process. For the hydrogenolysis of sorbitol to glycerine a good method is rather unexplored as the hydrogenolysis is previously mostly performed with either ethylene glycol (EG) or propylene glycol (PG) as the wanted product [1]. In context with the text above it is of great interest to investigate th
- Published
- 2016
33. Ni-substituted Ba-hexaaluminates catalyst for tar reforming from gasified iomass
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Parsland, Charlotte, Larsson, Ann-Charlotte, Brandin, Jan, Parsland, Charlotte, Larsson, Ann-Charlotte, and Brandin, Jan
- Published
- 2016
34. Modelling of a reverse-flow partial oxidation reactor for synthesis gas production from gasifier product gas.
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Tunå, Per, Svensson, Helena, Brandin, Jan, Tunå, Per, Svensson, Helena, and Brandin, Jan
- Abstract
Biomass gasification followed by fuel synthesis is one of the alternatives for producing liquid fuels and chemicalsfrom biomass feedstocks. The gas produced by gasification contains CO, H2, H2O, CO2, light hydrocarbons and tars. Thelight hydrocarbons can account for as much as 50% of the total energy content of the gas, depending on the type of gasifier,operating conditions and feedstock. The gas also contains catalyst poisons such as sulphur, in the form of H2S and COS. Thispaper presents simulations of a reverse-flow partial-oxidation reformer that converts the light hydrocarbons into more synthesisgas, while achieving efficiencies approaching that of conventional catalytic processes. Variations in parameters such as pressure,amount of oxidant and steam-to-carbon ratio were also investigated. Simulations of the reforming of natural gas were includedfor comparison. The results show the benefits of using reverse-flow operation with lean gases such as gasifier product gas.
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- 2015
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35. Fischer-Tropsch Synthesis : Investigation of CO catalyst by exposure to aerosol particles of potassium salts
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Gavrilovic, Ljubisa, Blekkan, Edd, Holmen, Anders, Venvik, Hilde, Brandin, Jan, Gavrilovic, Ljubisa, Blekkan, Edd, Holmen, Anders, Venvik, Hilde, and Brandin, Jan
- Abstract
Ej belagd 160411
- Published
- 2015
36. Nickel-substituted bariumhexaaluminates as novel catalysts in steam reforming of tars
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Parsland, Charlotte, Larsson, Ann-Charlotte, Benito, Patricia, Fornasari, Guiseppe, Brandin, Jan, Parsland, Charlotte, Larsson, Ann-Charlotte, Benito, Patricia, Fornasari, Guiseppe, and Brandin, Jan
- Abstract
This work investigates the performance of Ba–Ni-hexaaluminate, BaNixAl12 − xO19, as a new catalyst in thesteam-reforming of tars. Substituted hexaaluminates are synthesized and characterized. Steam reforming testsare carried out with both a model-substance (1-methylnaphthalene) and a slip-stream from a circulatingfluidized bed gasifier. The water–gas-shift activity is studied in a lab-scale set-up. Barium–nickel substitutedhexaaluminates show a high catalytic activity for tar cracking, and also shows activity for water–gas-shift.
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- 2015
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37. Nickel-substituted bariumhexaaluminates as novel catalysts in steam reforming of tars
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Parsland, Charlotte, primary, Larsson, Ann-Charlotte, additional, Benito, Patricia, additional, Fornasari, Guiseppe, additional, and Brandin, Jan, additional
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- 2015
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38. Selective Catalysts for Glycerol Dehydration
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Brandin, Jan, Hulteberg, Christian, and Leveau, Andreas
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Glycerol ,Renewable Bioenergy Research ,Förnyelsebar bioenergi ,Dehydration ,Kemiteknik ,pore condensation ,Bioenergy ,Bioenergi ,Catalyst ,Chemical Engineering - Abstract
There has been an increased interest over the last decade for replacing fossil based feedstock’s with renewable ones. There are several such feedstock’s that are currently being investigated such as cellulose, lignin, hemicellulose, triglycerides etc. However, when trying to perform selective reactions an as homogeneous feedstock as possible is preferable. One such feedstock example is glycerol, a side-product from biofuels production, which is a tri-alcohol and thus has much flexibility for reactions, e.g. dehydration, hydrogenation, addition reactions etc. Glycerol in itself is a good starting point for fine chemicals production being non-toxic and available in rather large quantities [1-2]. A key reaction for glycerol valorisation is the dehydration of glycerol to form acrolein, an unsaturated C3 aldehyde, which may be used for producing acrylic acid, acrylonitrile and other important chemcial products. It has recently been shown that pore-condensation of glycerol is an issue under industrial like conditions, leading to liquid-phase reactions and speeding up the catalyst activity and selectivity loss [3]. To address this issue, modified catalyst materials have been prepared where the relevant micro and meso pores have been removed by thermal sintering; calculations have shown that pores below 45 Å may be subject to pore condensation. The catalyst starting material was a 10% WO3 by weight supported on ZrO2 in the form of beads 1–2 mm and it was thermally treated at 400°C, 500°C, 600°C, 700°C, 700°C, 800°C, 850°C, 900°C and 1000°C for 2 hours. The catalysts were characterised using nitrogen adsorption, mercury intrusion porosimetry (MIP), Raman spectroscopy and ammonia temperature programmed desorption. The thermal sintered catalysts show first of all a decreasing BET surface area with sintering commencing between 700°C and 800°C when it decreases from the initial 71 m2/g to 62 m2/g and at 1000°C there is a mere 5 m2/g of surface area left. During sintering, the micro and meso-porosity is reduced as evidenced by MIP and depicted in figure 1. As may be seen in the figure, sintering decrease the amount of pores below and around 100 Å is reduced at a sintering temperature of 800°C and above. The most suitable catalyst based on the MIP appears to be the one sintered at 850°C which is further strengthened by the Raman analysis. There is a clear shift in the tungsten structure from monoclinic to triclinic between 850°C and 900°C and it is believed that the monoclinic phase is important for activity and selectivity. Further, the heat treatment shows that there is an increase in catalyst acidity measured as mmol NH3/(m2/g) but a decrease in the acid strength as evidenced by a decrease in the desorption peak maximum temperature.
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- 2013
39. Nickel-substituted Ba-hexaaluminates as catalysts stem-reforming of tars
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Parsland, Charlotte and Brandin, Jan
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Renewable Bioenergy Research ,Förnyelsebar bioenergi ,Kemiteknik ,Reforming ,Substituted Ba-hexaaluminate ,Bioenergy ,Bioenergi ,Catalyst ,Chemical Engineering ,Tars - Abstract
Gasification of woody biomass converts the solid organic material into a gaseous product with a higher energy value and by this mean provide a more carbon neutral gaseous fuel than the common fossil ones. The produced raw gas mainly contains H2, CO, CO2, CH4, H2O and N2 together with organic (tars) and inorganic (alkali) components and fine particulates. The amount of impurities in the raw gas is dependent of the fuel properties and the gasification process technology and the quality of the resulting product gas determines its suitability for more advanced purposes. One of the major general concerns within the gasification processes is the formation of tars. Tars are a vast group of polyaromatic hydrocarbons and there are a number of definitions. On an EU/IEA/US-DOE discussion meeting in Brussels 1998, a number of experts agreed on a simplified classification of tars as “all organic contaminants with a molecular weight larger than benzene” [1]. The aim of this work is to investigate the steam reforming ability of a catalytic material not previously tested in this type of application in order to achieve an energy-efficient and high-quality gasification gas. The physical demands for an optimal tar-cracking and steam reforming catalyst is a high surface area, thermal stability, mechanical strength and a capacity to withstand high gas velocities, poisons such as H2S or NH3 and other impurities. Additionally it has to resist the process steam, as steam is well known to enhance sintering of porous materials. Nickel is a familiar catalyst for steam reforming. Hexaaluminate is a well-known catalyst support with properties that may answer to the requests of a non-abrasive, high-temperaturestable and steam-resistant catalytic material. It is a structural oxide where the general formula for the doped unit cell is MIMII(x)Al12-xO19-d where MI represents the mirror plane cation and MII is the aluminum site in the lattice where substitution may occur. MII is often a transition metal ion of the same size and charge as aluminum. MI is an ion located in the mirror plane of the structure and it is a large metal ion, often from the alkaline, alkaline earth or rare earth metal group. The stability and activity of these materials are often being related to the properties of MI and MII. The activity is highly dependent on the nature of the Al-substituted metal and partially by the nature of MII [2]. In our experiments we have tested the catalytic capacity of Ni-substituted Ba-hexaaluminates synthesised by the sol-gel method [3], both in a model set-up and in a gasification plant. In the lab-scale set-up different catalyst-formulae was tested under various temperatures for reforming of methyl-naphthalene. The results show a good catalytic activity for tar-breakdown. As expected the substitution level of Ni is clearly coupled to the reaction temperature. With the most highly substituted Ni-Bahexaaluminate at 900 °C all of the methyl-naphthalene has been broken downtogether with all of the resulting hydrocarbons. The Ni-Bahexaaluminate catalyst has recently also been tested in real process-gas. These results are still to be evaluated, but indicate a positive result. Nationellt Förgasningscentrum
- Published
- 2013
40. Deactivation and Characterization of SCR Catalysts Used in Municipal Waste Incineration Applications.
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Brandin, Jan G. M. and Odenbrand, C. U. Ingemar
- Subjects
- *
CATALYTIC activity , *ACTIVATION (Chemistry) , *CATALYTIC reduction , *NITRIC oxide , *INCINERATION , *SOLID waste - Abstract
Catalysts used for selective catalytic reduction were deactivated for various times in a slipstream from a municipal solid waste incineration plant and then characterized. The activity for NO reduction with NH was measured. The Brunauer-Emmett-Teller surface areas were determined by N adsorption from which the pore size distributions in the mesopore region were obtained. Micropore areas and volumes were also obtained. The composition of fresh and deactivated catalysts as well as fly ash was determined by atomic absorption spectroscopy and scanning electron microscopy with energy dispersive X-ray analysis. The changes in surface area (8% decrease in BET surface area over 2311 h) and pore structure were small, while the change in activity was considerable. The apparent pre-exponential factor was 1.63 × 10 (1/min) in the most deactivated catalyst, compared to 2.65 × 10 (1/min) in the fresh catalyst, i.e. a reduction of 94%. The apparent activation energy for the fresh catalyst was 40 kJ/mol, decreasing to 27 kJ/mol with increasing deactivation. Characterization showed that catalytic poisoning is mainly due to decreased acidity of the catalyst caused due to increasing amounts of Na and K. Graphical Abstract: [ABSTRACT FROM AUTHOR]
- Published
- 2018
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41. Förgasning-Gasmotor för småskalig kraft-värme
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Brandin, Jan, Tunér, Martin, and Odenbrand, Ingemar
- Subjects
Gas Engine ,kraft-värme ,CHP ,Energy Engineering ,Bioenergi ,Combined Heat and Power ,Energiteknik ,Biofuel ,Kemiska processer ,Chemical Process Engineering ,Gasmotor ,Biobränsle ,Bioenergy ,Förgasning ,Gasification - Abstract
In a joint project, Linnaeus University in Växjö (LNU) and the Faculty of Engineering at Lund University (LTH) were commissioned by the Swedish Energy Agency to make an inventory of the techniques and systems for small scale gasifier-gas engine combined heat and power (CHP) production and to evaluate the technology. Small scale is defined here as plants up to 10 MWth, and the fuel used in the gasifier is some kind of biofuel, usually woody biofuel in the form of chips, pellets, or sawdust. The study is presented in this report. The report has been compiled by searching the literature, participating in seminars, visiting plants, interviewing contact people, and following up contacts by e-mail and phone. The first, descriptive part of the report, examines the state-of-the-art technology for gasification, gas cleaning, and gas engines. The second part presents case studies of the selected plants: Meva Innovation’s VIPP-VORTEX CHP plant DTU’s VIKING CHP plant Güssing bio-power station Harboøre CHP plant Skive CHP plant The case studies examine the features of the plants and the included unit operations, the kinds of fuels used and the net electricity and overall efficiencies obtained. The investment and operating costs are presented when available as are figures on plant availability. In addition we survey the international situation, mainly covering developing countries. Generally, the technology is sufficiently mature for commercialization, though some unit operations, for example catalytic tar reforming, still needs further development. Further development and optimization will probably streamline the performance of the various plants so that their biofuel-to-electricity efficiency reaches 30-40 % and overall performance efficiency in the range of 90 %. The Harboøre, Skive, and Güssing plant types are considered appropriate for municipal CHP systems, while the Viking and VIPP-VORTEX plants are smaller and considered appropriate for replacing hot water plants in district heating network. The Danish Technical University (DTU) Biomass Gasification Group and Meva International have identified a potentially large market in the developing countries of Asia. Areas for suggested further research and development include: Gas cleaning/upgrading Utilization of produced heat System integration/optimization Small scale oxygen production Gas engine developments I ett gemensamt projekt har Linnéuniversitetet i Växjö och Lunds Tekniska Högskola, på uppdrag av Energimyndigheten, genomfört en inventering av teknik och system för småskalig kombinerad värme och kraft produktion via förgasare-gasmotor teknik. Definitionen för småskalighet i denna studie, är anläggningar med en termisk effekt upp till 10 MW(3 MWel) och där bränslet är någon form av biomassa, vanligtvis träbaserad (trä eller skogsavfall) i form av flis, pellets eller spån. Projektrapporten innehåller först en deskriptiv del över teknikens ståndpunkt inom småskalig förgasning, gasrening och gasmotorer. Den andra delen utgörs av en fallbeskrivning för de olika anläggningarna som ingår i studien. MEVA Innovations VIPP-VORTEX CHP anläggning DTU:s VIKING CHP anläggning Bio-kraftverket i Güssing Harboøre CHP anläggning Skive CHP anläggning I fallbeskrivningarna gås anläggningarnas särdrag, funktioner samt enhetsoperationer igenom, samt vilken typ av bränsle som används och vilka verkningsgrader som uppnås. Investerings- och driftskostnaderna, där sådana är tillgängliga, presenteras tillsammans med uppgifter på anläggningarnas tillgänglighet. Även en internationell utblick, huvudsakligen fokuserad på utvecklingsländer, har genomförts. Generellt sett är tekniken tillräckligt mogen för kommersialisering. Det finns dock en del enhetsoperationer, t.ex. tjärkrackning och tjärreformering, som behöver fortsatt forskning och utveckling. Fortsatt utveckling av systemen kommer förmodligen att göra prestandan för anläggningarna än mera lika och öka elverkningsgraden till 30-40 % med en total verkningsgrad runt 90 %. Harboøre-, Güssing- och Skiveanläggningarna är avsedda som kommunala kraft-värmeanläggningar medan Viking och VIPP-VORTEX är avsedda att ersätta mindre varmvattencentraler i fjärrvärmenätet. Bimass Gasification Group DTU och MEVA Innovation har också identifierat en potentiellt stor marknad i utvecklingsländer i Asien. Förslag till områden för fortsatt forsknings och utvecklingsarbete: Gasrening/Gasuppgradering Användning av producerat värme System integration/optimering Småskalig syre-produktion Vidareutveckling av gasmotorer
- Published
- 2011
42. Modelling of a reverse-flow partial oxidation reactor for synthesis gas production from gasifier product gas
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Tunå, Per, primary, Svensson, Helena, additional, and Brandin, Jan, additional
- Published
- 2015
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43. Modeling of Reverse Flow Partial Oxidation Process for Gasifier Product Gas Upgrading
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Tunå, Per, Svensson, Helena, and Brandin, Jan
- Subjects
Energiteknik ,Partial Oxidation ,Energy Engineering ,Reverse Flow Operation ,Gasification - Abstract
Biomass gasification is one of the alternatives to producing liquid fuels and chemicals from biomass residues. The gas produced in gasification contains CO, H2, H2O, CO2, light hydrocarbons and tars. Depending on the gasifier type, operating conditions and fuel, the light hydrocarbons can contain as much as 50 % of the total energy contents in the gas. The gas also contains catalyst poisons such as sulfur, as H2S and COS. This paper presents simulation work of a reverse flow partial oxidation reformer that reaches efficiencies approaching conventional catalytical processes. Furthermore, different reactor designs and parameter variations such as pressure are investigated. For comparison, natural gas simulations are included which clearly show the benefits of using reverse flow operation with lean gases such as gasifier product gas. GREENSYNGAS
- Published
- 2010
44. Reforming of tars and hydrocarbons from gasified biomass
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Brandin, Jan and Brandin, Jan
- Abstract
Tars are produced during gasification of biomass due to thermal decomposition of main constituent of the biomass, cellulose, hemicellulose and lignin. Since the tars will condense on colder surfaces, they cause problems by clogging of pipes and valves and depositions on heat transfer surfaces, for instance. One strategy is to remove the tars by condensing them in water or oil scrubbers, however since the tars might contain a significant part of the heating value in the producer gas the yield of the produced synthesis gas will decrease. To utilize the heat content in the tars they can be converted in situ to synthesis gas either by a catalytic process like steam reforming or autothermal reforming (ATR). The problem with catalytic reforming is that the catalysts used are sensitive towards the sulphur content, mainly H2S, in the producer gas. The deactivation of the reforming catalysts can be counteracted by increasing the reforming temperature, for instance by the use of ATR. However, at elevated temperature, 1000-1100 oC, the thermal sintering of the catalyst will be accelerated instead. There is a need for development of new high temperature stable reforming catalysts. Another problem is the production of soot due to the high temperatures in the flame in the autothermal reformer unit. The formed sooth will cause problems by clogging packed bed of reforming catalyst and to cope with this it is probably necessary to use a monolithic catalyst. However, by developing a way to homogenous combust the added oxygen, avoiding the peak temperatures in the flame, would suppress or eventually eliminate the soot formation., Swedish gasification centre
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- 2013
45. Usage of Biofuels in Sweden
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Brandin, Jan and Brandin, Jan
- Abstract
In Sweden, biofuels have come into substantial use, in an extent that are claimed to be bigger than use of fossil oil. One driving force for this have been the CO2-tax that was introduced in 1991 (1). According to SVEBIO:s calculations (2) based on the Swedish Energy Agency´s prognosis, the total energy consumption in Sweden 2012 was 404 TWh. If the figure is broken down on the different energy sources (figure 1) one can see that the consumption roughly distribute in three different, equally sized, blocks, Biofuels, fossil fuels and water & nuclear power. The major use of the fossil fuels is for transport and the water & nuclear power is used as electric power. The main use of the biofuels is for heating in the industrial sector and as district heating. In 2009 the consumption from those two segments was 85 TWh, and 10 TWh of bio power was co-produced giving an average biomass to electricity efficiency of 12%. This indicates a substantial conversion potential from hot water production to combined heat and power (CHP) production. in Sweden 2013 broken down on the different energy sources. In 2006 the pulp, paper and sawmill industry accounted for 95% of the bio energy consumption in the industrial sector, and the major biofuel consumed was black liquor (5). However, the pulp and paper industries also produced the black liquor in their own processes. The major energy source (58%) for district heating during 2006 was woody biomass (chips, pellets etc.) followed by waste (24%), peat (6%) and others (12%) (5). The use of peat has probably decreased since 2006 since peat is no longer regarded as a renewable energy source. While the use of biofuel for heating purpose is well developed and the bio-power is expected to grow, the use in the transport sector is small, 9 TWh or 7% in 2011. The main consumption there is due to the mandatory addition (5%) of ethanol to gasoline and FAME to diesel (6). The Swedish authorities have announced plans to increase the renewable, Nationellt förgasningscenter
- Published
- 2013
46. High-temperature and high concentration SCR of NO with NH3 : application in a CCS process for removal of carbon dioxide
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Brandin, Jan, Hulteberg, Christian, Odenbrand, Ingemar, Brandin, Jan, Hulteberg, Christian, and Odenbrand, Ingemar
- Abstract
This study investigates several commercial selective catalytic reduction (SCR) catalysts (A–E) for application in a high-temperature (approximately 525 °C) and high-concentration (5000 ppm NO) system in combination with CO2 capture. The suggested process for removing high concentrations of NOx seems plausible and autothermal operation is possible for very high NO concentrations. A key property of the catalyst in this system is its thermal stability. This was tested and modelled with the general power law model using second-order decay of the BET surface area with time. Most of the materials did not have very high thermal stability. The zeolite-based materials could likely be used, but they too need improved stability. The SCR activity and the possible formation of the by-product N2O were determined by measurement in a fixed-bed reactor at 300–525 °C. All materials displayed sufficiently high activity for a designed 96% conversion in the twin-bed SCR reactor system proposed. The amount of catalyst needed varied considerably and was much higher for the zeolithic materials. The formation of N2O increased with temperature for almost all materials except the zeolithic ones. The selectivity to N2 production at 525 °C was 98.6% for the best material and 95.7% for the worst with 1000 ppm NOx in the inlet; at 5000 ppm NOx, the values were much better, i.e., 98.3 and 99.9%, respectively.
- Published
- 2012
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47. A Process for Producing Acrolein
- Author
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Hulteberg, Christian, Brandin, Jan, Hulteberg, Christian, and Brandin, Jan
- Abstract
Disclosed is a process for dehydrating glycerol into acrolein over an acidic catalyst in gas phase in the presence of hydrogen, minimizing side reactions forming carbon deposits on the catalyst.
- Published
- 2012
48. Nickel-substituted Barium-hexaaluminates as Catalysts in the Steam-reforming of Tars
- Author
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Parsland, Charlotte, Brandin, Jan, Parsland, Charlotte, and Brandin, Jan
- Abstract
The aim of this work is to investigate the catalytic properties, i.e. activity, selectivity and stability of nickel‐substituted Ba‐hexaaluminates for the cracking and steam‐reforming of a tar in product gas from biomass gasification. A lab‐scale set‐up has been constructed, consisting of a quartz reactor placed in a vertical oven, filled with the catalyst bed material. Methyl‐naphthalene was chosen as a tar model substance since naphthalene is considered to be especially difficult to reform, and since it is in liquid form at room temperature it is easier to handle than the solid naphthalene. A gas stream containing nitrogen gas, steam and methyl‐naphthalene was passed through the reactor and the resulting gas was analyzed by GC‐FID and GC‐TCD. Different catalyst compositions have been tested at different temperatures. The activity, stability and the product distribution was investigated as function of the temperature for the Ni‐substituted catalysts. In this study, three catalysts with different Ni‐substitution levels were used; BaNiAl11O19, BaNi1.5Al10.5O19and BaNi2Al10O19. The physical demands for an optimal cracking and steam reforming catalyst is a high surface area, thermal stability, abrasion resistance, and a capacity to withstand high gas velocities. Additionally it has to resist the process steam, as steam is well known to enhance sintering of porous materials. Hexaaluminate is a well ‐known high‐temperature material with properties that may well answer to these requests. If it can be substituted to a high catalytic activity this material may well be a good candidate for steam reforming. Our results show that we have synthesized a material with the desired composition and structure. The activity tests show that we have a good reforming ability from all the catalytic materials, but with an increased activity for BaNi2Al10O19. At 1000°C all methyl‐naphthalene was decomposed in all three cases and also at 900°C for the BaNi2Al10O19. There was no char depositio
- Published
- 2012
49. Small Scale Gasifiction : Gas Engine CHP for Biofuels
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Brandin, Jan, Tunér, Martin, Odenbrand, Ingemar, Brandin, Jan, Tunér, Martin, and Odenbrand, Ingemar
- Abstract
In a joint project, Linnaeus University in Växjö (LNU) and the Faculty of Engineering at Lund University (LTH) were commissioned by the Swedish Energy Agency to make an inventory of the techniques and systems for small scale gasifier-gas engine combined heat and power (CHP) production and to evaluate the technology. Small scale is defined here as plants up to 10 MWth, and the fuel used in the gasifier is some kind of biofuel, usually woody biofuel in the form of chips, pellets, or sawdust. The study is presented in this report. The report has been compiled by searching the literature, participating in seminars, visiting plants, interviewing contact people, and following up contacts by e-mail and phone. The first, descriptive part of the report, examines the state-of-the-art technology for gasification, gas cleaning, and gas engines. The second part presents case studies of the selected plants: Meva Innovation’s VIPP-VORTEX CHP plant DTU’s VIKING CHP plant Güssing bio-power station Harboøre CHP plant Skive CHP plant The case studies examine the features of the plants and the included unit operations, the kinds of fuels used and the net electricity and overall efficiencies obtained. The investment and operating costs are presented when available as are figures on plant availability. In addition we survey the international situation, mainly covering developing countries. Generally, the technology is sufficiently mature for commercialization, though some unit operations, for example catalytic tar reforming, still needs further development. Further development and optimization will probably streamline the performance of the various plants so that their biofuel-to-electricity efficiency reaches 30-40 % and overall performance efficiency in the range of 90 %. The Harboøre, Skive, and Güssing plant types are considered appropriate for municipal CHP systems, while the Viking and VIPP-VORTEX plants are smaller and considered appropriate for replacing hot water plants in distr, I ett gemensamt projekt har Linnéuniversitetet i Växjö och Lunds Tekniska Högskola, på uppdrag av Energimyndigheten, genomfört en inventering av teknik och system för småskalig kombinerad värme och kraft produktion via förgasare-gasmotor teknik. Definitionen för småskalighet i denna studie, är anläggningar med en termisk effekt upp till 10 MW(3 MWel) och där bränslet är någon form av biomassa, vanligtvis träbaserad (trä eller skogsavfall) i form av flis, pellets eller spån. Projektrapporten innehåller först en deskriptiv del över teknikens ståndpunkt inom småskalig förgasning, gasrening och gasmotorer. Den andra delen utgörs av en fallbeskrivning för de olika anläggningarna som ingår i studien. MEVA Innovations VIPP-VORTEX CHP anläggning DTU:s VIKING CHP anläggning Bio-kraftverket i Güssing Harboøre CHP anläggning Skive CHP anläggning I fallbeskrivningarna gås anläggningarnas särdrag, funktioner samt enhetsoperationer igenom, samt vilken typ av bränsle som används och vilka verkningsgrader som uppnås. Investerings- och driftskostnaderna, där sådana är tillgängliga, presenteras tillsammans med uppgifter på anläggningarnas tillgänglighet. Även en internationell utblick, huvudsakligen fokuserad på utvecklingsländer, har genomförts. Generellt sett är tekniken tillräckligt mogen för kommersialisering. Det finns dock en del enhetsoperationer, t.ex. tjärkrackning och tjärreformering, som behöver fortsatt forskning och utveckling. Fortsatt utveckling av systemen kommer förmodligen att göra prestandan för anläggningarna än mera lika och öka elverkningsgraden till 30-40 % med en total verkningsgrad runt 90 %. Harboøre-, Güssing- och Skiveanläggningarna är avsedda som kommunala kraft-värmeanläggningar medan Viking och VIPP-VORTEX är avsedda att ersätta mindre varmvattencentraler i fjärrvärmenätet. Bimass Gasification Group DTU och MEVA Innovation har också identifierat en potentiellt stor marknad i utvecklingsländer i Asien. Förslag till områden för fortsatt forsknings
- Published
- 2011
50. Method for Hydrogenating 1,2-Unsaturated Carbonylic Compounds
- Author
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Hulteberg, Christian, Brandin, Jan, Hulteberg, Christian, and Brandin, Jan
- Abstract
Disclosed is a method of hydrogenating an1,2-unsaturated carbonylic compound to obtain the corresponding saturated carbonylic compound in the presence of a palladium catalyst with heterogeneous distribution of palladium
- Published
- 2011
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