Anaerobic co-digestion of crude glycerin and starch industry effluent

The Brazil's Biodiesel Production and Use Program introduces biodiesel in the Brazilian energy matrix, bringing along the perspective of a growth of the glycerin offer, co-product generated in the proportion of 10 kg for each 100 L of biodiesel. The aim of this study was to evaluate the addition of crude glycerin in the anaerobic digestion of cassava starch industry effluent (cassava wastewater), in a horizontal semi-continuous flow reactor of one phase in laboratory scale. It was used a reactor with a 8.77 L of useful volume, a medium support for corrugated conduit of polyvinyl chloride (PVC), temperature of 261 ºC, fed with cassava wastewater and glycerin, with hydraulic detention times of 4 and 5 days and increasing volumetric organic load of 3.05; 9.32; 14.83 and 13.59 g COD L-1 d-1, obtained with the addition of glycerin at 0; 2; 3 and 2% (v/v), respectively. The average removal efficiencies of TS and TVS were decreasing from the addition of glycerin to the cassava wastewater, averaging 81.19 to 55.58% for TS and 90.21 to 61.45% for TVS. The addition of glycerin at 2% increased the biogas production compared to the control treatment, reaching 1.979 L L-1 d-1. The biogas production as a function of the consumed COD was higher for the control treatment than for the treatments with addition of glycerin, which indicates lower conversion of organic matter into biogas.

Start-up of horizontal anaerobic reactors with sludge blanket and fixed bed for wastewater treatment from coffee processing by wet method

In this study it was evaluated the start-up procedures of anaerobic treatment system with three horizontal anaerobic reactors (R1, R2 and R3), installed in series, with volume of 1.2 L each. R1 had sludge blanket, and R2 and R3 had half supporter of bamboo and coconut fiber, respectively. As an affluent, it was synthesized wastewater from mechanical pulping of the coffee fruit by wet method, with a mean value of total chemical oxygen demand (CODtotal) of 16,003 mg L-1. The hydraulic retention time (HRT) in each reactor was 30 h. The volumetric organic loading (VOL) applied in R1 varied from 8.9 to 25.0 g of CODtotal (L d)-1. The mean removal efficiencies of CODtotal varied from 43 to 97% in the treatment system (R1+R2+R3), stabilizing above 80% after 30 days of operation. The mean content of methane in the biogas were of 70 to 76%, the mean volumetric production was 1.7 L CH4 (L reactor d)-1 in the system, and the higher conversions were around at 0.20 L CH4 (g CODremoved)-1 in R1 and R2. The mean values of pH in the effluents ranged from 6.8 to 8.3 and the mean values of total volatile acids remained below 200 mg L-1 in the effluent of R3. The concentrations of total phenols of the affluent ranged from 45 to 278 mg L-1, and the mean removal efficiency was of 52%. The start-up of the anaerobic treatment system occurred after 30 days of operation as a result of inoculation with anaerobic sludge with active microbiota.

Performance of UASB reactors in two stages under different HRT and OLR treating residual waters of swine farming

In this study it was evaluated the effects of hydraulic retention time (HRT) and Organic Loading Rate (OLR) on the performance of UASB (Upflow Anaerobic Sludge Blanket) reactors in two stages treating residual waters of swine farming. The system consisted of two UASB reactors in pilot scale, installed in series, with volumes of 908 and 188 L, for the first and second stages (R1 and R2), respectively. The HRT applied in the system of anaerobic treatment in two stages (R1 + R2) was of 19.3, 29.0 and 57.9 h. The OLR applied in the R1 ranged from 5.5 to 40.1 kg CODtotal (m³ d)-1. The average removal efficiencies of chemical oxygen demand (COD) and total suspended solids (TSS) ranged, respectively, from 66.3 to 88.2% and 62.5 to 89.3% in the R1, and from 85.5 to 95.5% and 76.4 to 96.1% in the system (R1 + R2). The volumetric production of methane in the system (R1 + R2) ranged from 0.295 to 0.721 m³CH4 (m³ reactor d)-1. It was found that the OLR applied were not limiting to obtain high efficiencies of CODtotal and TSS removal and methane production. The inclusion of the UASB reactor in the second stage contributed to increase the efficiencies of CODtotal and TSS removal, especially, when the treatment system was submitted to the lowest HRT and the highest OLR.

Performance of UASB reactors in two stages followed by post-treatment with activated sludge in wastewater batch of wet-processed coffee

In this study it was evaluated the efficiency of the treatment of wet-processed coffee wastewater in upflow anaerobic sludge blanket (UASB) reactors in two stages, in bench scale, followed by post-treatment with activated sludge in batch. The first UASB reactor was submitted to an hydraulic retention time (HRT) of 6.2 d and organic loading rates (OLR) of 2.3 and 4.5g CODtotal (L d)-1, and the second UASB reactor to HRT of 3.1 d with OLR of 0.4 and 1.4g CODtotal (L d)-1. The average values of the affluent CODtotal increased from 13,891 to 27,926mg L-1 and the average efficiencies of removal of the CODtotal decreased from 95 to 91%, respectively, in the UASB reactors in two stages. The volumetric methane production increased from 0.274 to 0.323L CH4 (L reactor d)-1 with increment in the OLR. The average concentrations of total phenols in the affluent were of 48 and 163mg L-1, and the removal efficiencies in the UASB reactors in two stages of 92 and 90%, respectively, and increased to 97% with post-treatment. The average values of the removal efficiencies of total nitrogen and phosphorus were of 57 to 80% and 44 to 60%, respectively, in the UASB reactors in two stages and increased to 91 and 84% with the post-treatment.

Anaerobic-aerobic treatment of swine wastewater in uasb and batch reactors in series

In this work it was evaluated the performance of two systems of swine wastewater treatment consisting of two-stage upflow anaerobic sludge blanket (UASB) reactors, with and without post-treatment in sequencing batch reactor (SBR), fed continuously, with aerobic phase. The UASB reactors in the first stage had 908 L in the sets I and II, and in the second stage 350 and 188 L, respectively. In the set II the post-treatment was performed in a SBR of 3,000 L. The hydraulic detention times in the anaerobic treatment systems were 100, 75 and 58 h in the set I; 87, 65 and 51 h in the set II; and 240 and 180 h in the SBR. The volumetric organic load applied in the first stage UASB reactors ranged from 6.9 to 12.6 g total COD (L d)-1 in the set I and 7.5 to 9.8 g total COD (L d)-1 in the set II. The average removal efficiencies of total COD, total phosphorus (Ptotal), and Kjeldahl and organic nitrogen (KN and Norg) in the anaerobic treatment systems were similar and reached maximum values of 97%, 64%, 68%, and 98%. In the SBR, the removal efficiencies of total COD and thermotolerant coliforms were up to 62 and 92% resulting, respectively, in effluent concentrations of 135 mg L-1 and 2x10(4)MPN (100 mL)-1. For Ptotal, total nitrogen (TN) and Norg, the average removal efficiencies in the SBR were up to 58, 25 and 73%, respectively.

Start-up of anaerobic reactors for slaughterhouse wastewater treatment

This study aimed to evaluate the start-up of a horizontal anaerobic fixed bed reactor (HAFBR) followed by an upflow anaerobic sludge blanket (UASB) for the slaughterhouse wastewater treatment. HAFBR was filled with bamboo rings and had 1.2 m in length, 0.10 m in diameter and volume of 7.5 L. The UASB had the volume of 15 L. The HAFBR and UASB operated at organic loading rate and hydraulic retention time average of 8.46 and 3.77 kg m-3 d-1 of COD and 0.53 and 0.98 days, respectively. During 150 days of monitoring system it was found pH 6.8, relatively high values of bicarbonate alkalinity (> 1000 mg L-1) and reduced values of volatile acids (70 to 150 mg L-1), which afforded average removal efficiencies of COD total and total suspended solids of the order of 31 and 23% in HAFBR and 79% and 63% in UASB. It can be concluded that the generation and consumption of bicarbonate alkalinity and total volatile acids, thereby maintaining the pH during the study indicated stable operation of the reactors. The COD removal in the reactors was satisfactory especially when it considers that the assessment was conducted in a period of adaptation of organisms to the effluent and also the high organic load applied during this period.

Eksotermiset kemialliset reaktiot ydinreaktoreissa

Neljännen sukupolven reaktoreissa käytetään uusia teknisiä ratkaisuja ja uudenlaisia materiaaleja, joten myös niiden turvallisuuskriteerien laatimiseen tarvitaan uusia näkökulmia. Tällä hetkellä kehitetäänkin teknologianeutraaleja turvallisuuskriteerejä, joista voitaisiin johtaa jokaiselle uudelle reaktorikonseptille reaktorin erityispiirteet huomioivat teknologiaspesifit turvallisuuskriteerit. Näin pystytään takaamaan turvallisuuden korkea taso kaikissa uusissa reaktoreissa. Eksotermiset eli lämpöä vapauttavat kemialliset reaktiot muodostavat merkittävän uhan ydinvoimalaitosten turvallisuudelle. Tutkimalla nykyisin käytössä olevia turvallisuuskriteerejä sekä kehitteillä olevia teknologianeutraaleja turvallisuuskriteerejä voitiin havaita, että eksotermiset kemialliset reaktiot on niissä huomioitu hyvin, mutta ei kovin systemaattisesti. Tämän tutkielman tavoitteena oli pohtia, kuinka eksotermiset kemialliset reaktiot voitaisiin huomioida systemaattisemmin teknologianeutraaleissa turvallisuuskriteereissä. Johtopäätöksenä on, että epätoivottujen eksotermisten kemiallisten reaktioiden tapahtuminen tulisi ensisijaisesti pyrkiä estämään, mutta jos tällainen reaktio kuitenkin tapahtuu, tulisi sen seurauksia lieventää. Eksotermisten kemiallisten reaktioiden tapahtuminen pystytään estämään, jos eksotermisesti reagoivia aineita ei ole tai ne pystytään pitämään erillään toisistaan, tai jos lämpötilat saadaan pidettyä riittävän alhaisina. Tutkielman toisena tavoitteena oli tarkastella onnettomuusskenaarioita, jotka voisivat johtaa eksotermisiin kemiallisiin reaktioihin erityisesti neljännen sukupolven reaktoreissa. Tätä varten tutkitaan kirjallisuuden avulla joidenkin reaktorimateriaalien kemiallisia ominaisuuksia sekä muutamia neljännen sukupolven reaktoreja. Kirjallisuuden avulla tarkastellaan myös muutamaa sellaista ydinvoimalaitosonnettomuutta, joissa eksotermiset kemialliset reaktiot ovat olleet merkittävässä roolissa.

Corrosion behaviour of boiler tube materials during combustion of fuels containing Zn and Pb

Många förbränningsanläggningar som bränner utmanande bränslen såsom restfraktioner och avfall råkar ut för problem med ökad korrosion på överhettare och/eller vattenväggar pga. komponenter i bränslena som är korrosiva. För att minimera problemen i avfallseldade pannor hålls ångparametrarna på en relativt låg nivå, vilket drastiskt minskar energiproduktionen. Beläggningarna i avfallseldade pannor består till största delen av element som är förknippade med högtemperaturkorrosion: Cl, S, alkalimetaller, främst K och Na, och tungmetaller som Pb och Zn, och det finns också indikationer av Br-förekomst. Det låga ångtrycket i avfallseldade pannor påverkar också stålrörens temperatur i pannväggarna i eldstaden. I dagens läge hålls temperaturen normalt vid 300-400 °C. Alkalikloridorsakad (KCl, NaCl) högtemperaturkorrosion har inte rapporterats vara relevant vid såpass låga temperaturer, men närvaro av Zn- och Pb-komponenter i beläggningarna har påvisats förorsaka ökad korrosion redan vid 300-400 °C. Vid förbränning kan Zn och Pb reagera med S och Cl och bilda klorider och sulfater i rökgaserna. Dessa tungmetallföreningar är speciellt problematiska pga. de bildar lågsmältande saltblandningar. Dessa lågsmältande gasformiga eller fasta föreningar följer rökgasen och kan sedan fastna eller kondensera på kallare ytor på pannväggar eller överhettare för att sedan bilda aggressiva beläggningar. Tungmetallrika (Pb, Zn) klorider och sulfater ökar risken för korrosion, och effekten förstärks ytterligare vid närvaro av smälta. Motivet med den här studien var att få en bättre insikt i högtemperaturkorrosion förorsakad av Zn och Pb, samt att undersöka och prediktera beteendet och motståndskraften hos några stålkvaliteter som används i överhettare och pannväggar i tungmetallrika förhållanden och höga materialtemperaturer. Omfattande laboratorie-, småskale- och fullskaletest utfördes. Resultaten kan direkt utnyttjas i praktiska applikationer, t.ex. vid materialval, eller vid utveckling av korrosionsmotverkande verktyg för att hitta initierande faktorer och förstå deras effekt på högtemperaturkorrosion.

Modelling of calciner in post-combustion carbon capture process

Climate change has given an impetus to research and developed new technologies to reduce significantly carbon dioxide emissions in energy production in the developed countries. The major pollution source, fossil fuels, will be used as an energy source for many decades, which provides the demand for carbon capture and storage technologies. Over recent years many new technologies has been developed and one of the most promising is calcium-looping in post-combustion carbon capture process, which use carbonation-calcination cycle to capture carbon dioxide from the flue gas of a combustion process. First pilot plant for calcium-looping process has been built in Oviedo, Spain. In this study, a three-dimensional model has been created for the calciner, which is one of the two fluidized bed reactors needed for the process. The calciner is a regenerator where the captured carbon dioxide is removed from the calcium material and then collected after the reactor. Thesis concentrates in creating the calciner 3D-model frame with CFB3D-program and testing the model with two different example cases. Used input parameters and calciner geometry are Oviedo pilot plant design parameters. The calculation results give information about the process and show that pilot plant calciner should perform as planned. This Master’s Thesis is done in participation to EU FP7 project CaOling.

Catalysis by gold for biomass transformations

The development of new technologies to supplement fossil resources has led to a growing interest in the utilization of alternative routes. Biomass is a rich renewable feedstock for producing fine chemicals, polymers, and a variety of commodities replacing petroleumderived chemicals. Transformation of biomass into diverse valuable chemicals is the key concept of a biorefinery. Catalytic conversion of biomass, which reduces the use of toxic chemicals is one of the important approaches to improve the profitability of biorefineries. Utilization of gold catalysts allows conducting reactions under environmentally-friendly conditions, with a high catalytic activity and selectivity. Gold-catalyzed valorization of several biomass-derived compounds as an alternative approach to the existing technologies was studied in this work. Isomerization of linoleic acid via double bond migration towards biologically active conjugated linoleic acid isomers (CLA) was investigated. The activity and selectivity of various gold catalysts towards cis-9,trans-11-CLA and trans-10,cis-12-CLA were investigated in a semi-batch reactor, showing that the yield of the desired products varied, depending on the catalyst support. The structure sensitivity in the selective oxidation of arabinose was demonstrated using a series of gold catalysts with different Au cluster sizes in a shaker reactor operating in a semibatch mode. The gas-phase selective oxidation of ethanol was studied and the influence of the catalyst support on the catalytic performance was investigated. The selective oxidation of the lignan hydroxymatairesinol (HMR), extracted from the Norway spruce (Picea abies) knots, to the lignan oxomatairesinol (oxoMAT) was extensively investigated. The influence of the reaction conditions and catalyst properties on the yield of oxoMAT was evaluated. In particular, the structure sensitivity of the reaction was demonstrated. The catalyst deactivation and regeneration procedures were studied. The reaction kinetics and mechanism were advanced.

New Type Nuclear Reactors (NETNUC) 2008-2011 Final Report

This report summarizes the work done by a consortium consisting of Lappeenranta University of Technology, Aalto University and VTT Technical Research Centre of Finland in the New Type Nuclear Reactors (NETNUC) project during 2008–2011. The project was part of the Sustainable Energy (SusEn) research programme of the Academy of Finland. A wide range of generation IV nuclear technologies were studied during the project and the research consisted of multiple tasks. This report contains short articles summarizing the results of the individual tasks. In addition, the publications produced and the persons involved in the project are listed in the appendices.

Production of Mg(OH)2 from Mg-silicate rock for CO2 mineral sequestration

Sequestration of carbon dioxide in mineral rocks, also known as CO2 Capture and Mineralization (CCM), is considered to have a huge potential in stabilizing anthropogenic CO2 emissions. One of the CCM routes is the ex situ indirect gas/sold carbonation of reactive materials, such as Mg(OH)2, produced from abundantly available Mg-silicate rocks. The gas/solid carbonation method is intensively researched at Åbo Akademi University (ÅAU ), Finland because it is energetically attractive and utilizes the exothermic chemistry of Mg(OH)2 carbonation. In this thesis, a method for producing Mg(OH)2 from Mg-silicate rocks for CCM was investigated, and the process efficiency, energy and environmental impact assessed. The Mg(OH)2 process studied here was first proposed in 2008 in a Master’s Thesis by the author. At that time the process was applied to only one Mg-silicate rock (Finnish serpentinite from the Hitura nickel mine site of Finn Nickel) and the optimum process conversions, energy and environmental performance were not known. Producing Mg(OH)2 from Mg-silicate rocks involves a two-staged process of Mg extraction and Mg(OH)2 precipitation. The first stage extracts Mg and other cations by reacting pulverized serpentinite or olivine rocks with ammonium sulfate (AS) salt at 400 - 550 oC (preferably < 450 oC). In the second stage, ammonia solution reacts with the cations (extracted from the first stage after they are leached in water) to form mainly FeOOH, high purity Mg(OH)2 and aqueous (dissolved) AS. The Mg(OH)2 process described here is closed loop in nature; gaseous ammonia and water vapour are produced from the extraction stage, recovered and used as reagent for the precipitation stage. The AS reagent is thereafter recovered after the precipitation stage. The Mg extraction stage, being the conversion-determining and the most energy-intensive step of the entire CCM process chain, received a prominent attention in this study. The extraction behavior and reactivity of different rocks types (serpentinite and olivine rocks) from different locations worldwide (Australia, Finland, Lithuania, Norway and Portugal) was tested. Also, parametric evaluation was carried out to determine the optimal reaction temperature, time and chemical reagent (AS). Effects of reactor types and configuration, mixing and scale-up possibilities were also studied. The Mg(OH)2 produced can be used to convert CO2 to thermodynamically stable and environmentally benign magnesium carbonate. Therefore, the process energy and life cycle environmental performance of the ÅAU CCM technique that first produces Mg(OH)2 and the carbonates in a pressurized fluidized bed (FB) were assessed. The life cycle energy and environmental assessment approach applied in this thesis is motivated by the fact that the CCM technology should in itself offer a solution to what is both an energy and environmental problem. Results obtained in this study show that different Mg-silicate rocks react differently; olivine rocks being far less reactive than serpentinite rocks. In summary, the reactivity of Mg-silicate rocks is a function of both the chemical and physical properties of rocks. Reaction temperature and time remain important parameters to consider in process design and operation. Heat transfer properties of the reactor determine the temperature at which maximum Mg extraction is obtained. Also, an increase in reaction temperature leads to an increase in the extent of extraction, reaching a maximum yield at different temperatures depending on the reaction time. Process energy requirement for producing Mg(OH)2 from a hypothetical case of an iron-free serpentine rock is 3.62 GJ/t-CO2. This value can increase by 16 - 68% depending on the type of iron compound (FeO, Fe2O3 or Fe3O4) in the mineral. This suggests that the benefit from the potential use of FeOOH as an iron ore feedstock in iron and steelmaking should be determined by considering the energy, cost and emissions associated with the FeOOH by-product. AS recovery through crystallization is the second most energy intensive unit operation after the extraction reaction. However, the choice of mechanical vapor recompression (MVR) over the “simple evaporation” crystallization method has a potential energy savings of 15.2 GJ/t-CO2 (84 % savings). Integrating the Mg(OH)2 production method and the gas/solid carbonation process could provide up to an 25% energy offset to the CCM process energy requirements. Life cycle inventory assessment (LCIA) results show that for every ton of CO2 mineralized, the ÅAU CCM process avoids 430 - 480 kg CO2. The Mg(OH)2 process studied in this thesis has many promising features. Even at the current high energy and environmental burden, producing Mg(OH)2 from Mg-silicates can play a significant role in advancing CCM processes. However, dedicated future research and development (R&D) have potential to significantly improve the Mg(OH)2 process performance.

Vaikutusalakirjastojen muodostaminen Serpent-ARES-laskentaketjussa

Tässä diplomityössä on esitetty työn yhteydessä toteutetun Serpent-ARES-laskentaketjun muodostamiseksi tarvittavat toimenpiteet. ARES-reaktorisydän-simulaattorissa tarvittavien homogenisoitujen ryhmävakiokirjastojen muodostaminen Serpentiä käyttäen tekee laskentaketjusta muiden käytössä olevien reaktorisydämen laskentaketjujen mahdollisista virhelähteistä riippumattoman. Monte Carlo-laskentamenetelmään perustuvaa reaktorifysiikan laskentaohjelmaa käyttämällä ryhmävakiokirjastot muodostetaan uudella menetelmällä ja näin saadaan viranomaiskäyttöön voimayhtiöiden käyttämistä menetelmistä riippumaton laskentaketju reaktorien turvallisuusmarginaalien laskentaan. Työn yhteydessä muodostetun laskentaketjun ja tehtyjen vaikutusalakirjastojen muodostamisrutiinien sekä parametrisovitteiden toimivuus on todettu laskemalla Olkiluoto 3 - reaktorin alkulatauksen säätösauvojen tehokkuuksia ja sammutusmarginaaleja eri olosuhteissa. Menetelmä on todettu toimivaksi parametrien pätevyysalueella ja saadut laskentatulokset ovat oikeaa suuruusluokkaa. Parametrimallin tarkkuutta ja pätevyysaluetta on syytä vielä kehittää, ennen kuin laskentaketjua voidaan käyttää varmentamaan muilla menetelmillä laskettujen tulosten oikeellisuutta.

HTR-PROTEUS-reaktorin mallintaminen

Maailmassa on tarve entistä turvallisemmille ja taloudellisemmille ydinreaktoreille. Neljännen sukupolven reaktorikonseptit ovat aiempia turvallisempia ja luotettavampia, niissä on tehokkaampi polttoaineresurssien käyttö ja ydinjätettä syntyy vähemmän. Lisäksi ne ovat taloudellisesti kilpailukykyisempiä ja niissä on erinomainen proliferaation vastustuskyky. Kuulakekoreaktorikonsepti on toinen korkealämpötilaisten kaasujäähdytteisten reaktoreiden (HTGR, High Temperature Reactor) päätyypeistä ja jäähdytteen lämpötilan noustessa reaktorissa riittävän korkealle, sitä voidaan pitää myös erittäin korkean lämpötilan reaktorina (VHTR, Very High Temperature Reactor), joka on neljännen sukupolven reaktorikonsepti. Tässä kandidaatintyössä käsitellään 90-luvulla Sveitsissä sijainnutta kuulakekoreaktori-tyyppistä koereaktoria HTR-PROTEUS (tai LEU-HTR-PROTEUS), jolla tutkittiin ennen kaikkea matalaväkevöidyn (LEU, Low Enriched Uranium) uraanipolttoaineen käyttöä kuulakekoreaktorissa. Lisäksi erityisenä mielenkiinnon kohteena oli veden joutuminen reaktoriin onnettomuustilanteessa. Työn tarkoituksena on mallintaa reaktorisysteemi ja laskea kasvutekijät viidelle eri reaktorikonfiguraatiolle. Reaktorin mallinnus ja laskenta suoritetaan Monte Carlo -menetelmää käyttävällä Serpent-laskentakoodilla. Saatuja tuloksia verrataan muissa lähteissä eri laskentakoodeilla esitettyihin tuloksiin.

Öljynjalostamon vetyverkon PINCH-analyysi

Tässä diplomityössä on tarkasteltu Porvoon öljynjalostamon vetyverkkoa ja pohdittu keinoja, joilla vedyn käyttöä jalostamolla voitaisiin tehostaan sekä polttokaasuverkkoon menevän vedyn määrä pienentää. Tarkastelun lähtökohtana toimii vetytaseen pohjalta laadittu vetypinch-analyysi. Kirjallisuusosassa on esitelty jalostamon vetyverkkoon kuuluvat yksiköt sekä käsitelty lyhyesti niiden toimintaa. Lisäksi on käsitelty vetypinch-analyysin periaate, sekä kuinka todelliset prosessirajoitteet voidaan huomioida sitä toteutettaessa. Kirjallisuusosan lopussa on esitetty miten vetyverkon vaiheittainen optimointi etenee. Työn soveltavassa osassa laadittiin vetyverkon virtauskaavio, jolla saatiin luotua kattava käsitys jalostamon vedynjakelusta. Virtauskaaviosta tehtiin yksinkertaistettu versio, jonka perusteella laadittiin vetytase. Vetytaseen pohjalta suoritettiin vetypinch-analyysi, jonka mukaan jalostamolla tuotettiin tasehetkellä ylimäärin vetyä. Vedyn käytön tehostamiseksi jalostamolla tulee rikkivedyn talteenottoyksikkö 2:n polttokaasuvirta pyrkiä minimoimaan tai hyödyntämään. Lisäksi virtausmittareiden mitoituspisteiden molekyylimassat tulisi muuttaa vastaamaan paremmin nykyistä ajotilannetta, sekä seurata niitä jatkossa säännöllisesti. Myös vetypitoisuutta mittaavien online-analysaattoreiden kalibroinnista tulee huolehtia, ja ottaa riittävästi kenttänäytteitä vetyverkosta. On huomattava, että öljynjalostamon vedyn tuotannon minimointi ei ole aina automaattisesti taloudellisin ratkaisu. Joissain tapauksissa vedyn osapaineen nostaminen vetyä kuluttavan yksikön reaktorissa voi lisätä yksikön tuottavuutta niin paljon, että se kompensoi lisääntyneestä vedyn tuotannosta aiheutuvat kustannukset.