Husums plant has a selection of different pulp pumps at bleaching plant 4 and 5. The displacement- (HC-pump, Sund Defibrator PTD-60) and centrifugalpumps (MC-pump, MCA 42-200, MCP 30/20) are of interest in this report. The centrifugal pumps are controlled by throttle valves, which result in an energy loss. Chemical mixers are used to mix ClO2 into the pulp before proceeding into a holding tower where the bleaching process occurs. The energy demand of the different positions has been measured or calculated to be used in comparisons against new equipment. Quotations were requested and delivered from Valmet and Sulzer. The quotations were made with a production increase of 10 ADMt/h and plant compared to current equipment. Therefore energy need of the equipment in the quotation had to be recalculated to the same production output as when measurements were conducted to be comparable. Quotation of the pumps assumes the use of frequency inverters. A deeper investigation was made for 441PU255 which is located at bleaching plant 4. The drop leg level of the pump is controlled via a throttle valve. A frequency inverter is installed but not utilized to maintain constant pulp level in the drop leg. This was due to physical changes in the process not being compensated for in the control system. This caused the drop leg level to oscillate when automatic control was used. As a workaround the drive had been set at a constant speed. To investigate the potential savings, an attempt was made in which the speed was lowered from 1520 rpm to 1100 rpm, resulting in a power reduction of 82 kW or 342,081 Sek per year at a production of 36 ADMT/h. The experiment was done with slightly lower production output than desirable; because of this, savings will decrease slightly at higher outputs. Comparisons showed that considerable amounts of energy could be saved at all positions. However the investment cost is high and therefore favorable payback times can only be seen for some of the positions. The MC-pumps are oversized and in need of constant throttling therefore the majority of the energy savings is made through the installation of frequency inverters and not the pump upgrade. / Metsä Board Husum har idag ett flertal olika modeller av massapumpar vid blekeri 4 och 5. Dessa är av deplacerande typ (HC-pump, Sunds Defibrator PTD-60) samt centrifugalmodell (MC-pump, MCA 42-200, MCP 30/20), centrifugalmodellen regleras med strypventiler vilket innebär en extra förlust, speciellt märkbar är denna då produktionen tas ned. Vid blekeriet finns även kemikaliemixrar för att mixa in ClO2 innan pappersmassan pumpas till ett uppehållstorn där blekprocessen sker. Anläggningens nuläge genomgick en mindre kartläggning där specifikationer och mätdata samlades in för att ge en bakgrund till det energibehov som finns idag. Tillgänglighet för reservdelar har varit av intresse för de äldre HC-pumparna. Tillsammans med Sulzer har uppfordringshöjd beräknats för positioner utrustade med PTD -60 då uppgifter för denna saknades. Sulzer och Valmet har offererat ny utrustning för dessa positioner som jämförs mot uppmätta värden för att beräkna återbetalningstid. Inkomna offerter förutsätter frekvensomriktare och baseras på en önskad produktionsökning till 50 ADMt/h för blekeri 4 och 60 ADMt/h för blekeri 5. Detta är en ökning på 10 ADMt/h och blekeri. Erforderlig effekt för drifter i inkomna offerter och uppmätt effekt är ej angiven vid samma driftpunkt. De offererade pumparnas driftpunkt har därför räknats om för att motsvara driftpunkt vid tillfället för insamling av data. Detta för att enkelt kunna jämföra offerter mot nuläge. På blekeri 4 återfinns en MC-pump av modell MCA 42-200 med posnummer 441PU255. Vid denna position gjordes en djupare undersökning då nivåregleringen ej fungerar som tänkt. Nivåhållning sker via reglerventil och varvtalsreglering med frekvensomriktare. För att kunna köra driften har frekvensomriktaren manuellt ställts i ett fast varvtal och reglerventilen lagts i automatik. Ventilen styr därmed nivå i fallröret och har vid normal drift en öppningsgrad på 40-50 %. Vid genomgången upptäcktes att parametrar i styrsystem gällande de varvtal motorn skall arbeta vid inte korrigerats efter en ombyggnation. Detta har medfört att nivån inte gått att reglera i automatik utan att systemet börjat självsvänga. För att undersöka skillnad mellan varvtalsstyrning och strypreglering gjordes ett försök där varvtalet sänktes från 1520 rpm till 1100 rpm vilket resulterade i en effektminskning på 82 kW eller 342 081 kr per år jämfört med strypreglering; detta var vid en produktion av 36 ADMt/h. Försöket gjordes med något lägre produktion än önskvärt; på grund av detta kommer besparingen minska något vid högre produktion. Samtliga positioner uppvisar minskat energibehov med ny utrustning. Dock gör hög investeringskostnad och krav på kort återbetalningstid att endast några få positioner är lämpliga kandidater för ombyggnad i dagsläget. För MC-pumparna kan däremot majoriteten av besparingen uppnås genom att bygga om dagens strypreglering till varvtalsreglering. Detta sker till en betydligt lägre kostnad än vid uppgradering av pump. Arbetet visar att det finns stor potential att minska energikonsumtion vid blekning av pappersmassa, detta gäller speciellt för de befintliga MC-pumparna som är kraftigt överdimensionerade och regleras med strypventil. De gamla kemikaliemixrarna använder stora mängder energi för att mixa in ClO2, nya mixrar använder mindre än hälften av energin och ger överskådliga återbetalningstider.

A magnetic bead-based DNA extraction and purification device has been designed to be used for extraction of the target DNA molecules from whole blood sample. Mixing and separation steps are performed using functionalised superparamagnetic beads suspended in the cell lysis buffer in a circular chamber that is sandwiched between two electromagnets. Non-uniform nature of the magnetic field causes temporal and spatial distribution of the beads within the chamber. This process efficiently mixes the lysis buffer and whole blood in order to extract DNA from target cells. Functionalized surface of the magnetic beads then attract the exposed DNA molecules. Finally, DNA-attached magnetic beads are attracted to the bottom of the chamber by activating the bottom electrode. DNA molecules are extracted from the magnetic beads by washing and re-suspension processes. The numerical simulation approach has been adopted in order to design the magnetic field source. The performance of the magnetic field source has been investigated against different physical and geometrical parameters and optimised dimensions are obtained with two different magnetic field sources; integrated internal source and external source. A new magnetic field pattern has been introduced in order to efficiently control the bulk of magnetic beads inside the mixing chamber by dynamic shifting of magnetic field regions from the centre of the coils to the outer edge of the coils and vice versa. A Matlab code has been developed to simulate beads trajectories inside the designed extraction chip in order to investigate the efficiency of the magnetic mixing. A preliminary target molecule capturing simulation has also been performed using the simulated bead trajectories to evaluate the DNA-capturing efficiency of the designed extraction chip. The performance of the designed extraction chip has been tested by conducting a series of biological experiments. Different magnetic bead-based extraction kits have been used in a series of preliminary experiments in order to extract a more automation friendly extraction protocol. The efficiency of the designed device has been evaluated using the spiked bacterial DNA and non-pathogenic bacterial cell cultures (B. subtilis, Gram positive bacteria and E. coli, Gram negative bacteria) into the blood sample. Excellent DNA yields and recovery rates are obtained with the designed extraction chip through a simple and fast extraction protocol.

Atualmente, dois dos grandes desafios com os quais o agronegócio brasileiro, responsável por aproximadamente 37% do PIB nacional em 2007, se depara em seu constante crescimento são a alta dependência de produtos químicos (fertilizantes) para que sua fronteira agrícola se expanda e, conseqüentemente, as enormes distâncias (e custos de transportes) que essas fronteiras impõem para que sejam vencidas, tanto para o recebimento de insumos de produção, quanto para o fornecimento de seus produtos finais. Particularmente, a região Centro-Oeste brasileira, formada pelos estados de Goiás, Mato Grosso, Mato Grosso do Sul e Distrito Federal, se enquadra em ambos os pontos possui grandes fronteiras agrícolas a serem exploradas e, ao mesmo, tempo se localiza a grandes distâncias dos principais portos de escoamento de sua produção e aquisição de insumos (especialmente, adubos e fertilizantes). Dentro deste contexto, o presente trabalho teve como objetivo, através da elaboração de um modelo matemático de programação linear, indicar localizações para instalação de fábricas misturadoras de adubos que minimizem os custos de transporte envolvidos. Portanto, de forma geral, os dados levantados para a realização desse estudo dizem respeito, basicamente, aos custos de transportes envolvidos com a distribuição de matéria-prima e produto final entre os municípios envolvidos, bem como suas respectivas necessidades de consumo e capacidade de fornecimento. Observou-se, a partir dos resultados gerados, uma tendência bastante clara de instalações de fábricas misturadoras em locais que o acesso às matérias-primas envolvidas no processo produtivo se caracterizasse pela facilidade e pelo baixo custo. Um outro ponto bastante evidente nos resultados observado é a participação do modal ferroviário no processo de distribuição das principais matérias-primas. / Currently, the brazilian agribusiness is responsible for about 37% of the national PIB and face up to two of the great challenges in its constant growth which are the high dependence of chemical products (fertilizers) to expand its agricultural frontier and consequently, the distance (and transports costs) that this frontiers impose to be overcome, as much for the receiving of production input as the supply of its final products. Particularly, the brazilian Center-West region, formed by the States of Goiás, Mato Grosso, Mato Grosso do Sul and Distrito Federal, is inserted in both points, has greats agricultural frontiers to be explored and in the same time, is located so far of the main draining ports of its production and acquisition of inputs (specially fertilizers). Inside of this context and thought the elaboration of a mathematic model of linear programming, the present work had as objective to indicate localizations for mixers fertilizers plants installation which minimize the involved transport costs. Therefore, in general form, the data raised for the accomplishment of this study means of the involved transports costs with the distribution of raw material and final product between the involved cities, as its respective needs of consumption and supply capacity. A sufficiently clear tendency of mixers plants installation in locals where the access of raw materials involved in productive process was characterized by facility and low cost. Another evident point in the results is the participation of railway modal in the distribution process of the main raw materials.

Superconductor-Insulator-Superconductor (SIS) mixers offer the best noise properties of any heterodyne mixing technique at millimetre wavelengths. In astronomy, they are used for sensitive spectroscopy, which is vital for understanding the properties of the cold interstellar medium, including regions of star formation activity. Modern SIS receivers have noise properties that are ∼3 times the quantum limit, and it is now becoming increasingly difficult to lower the noise properties any further. In this thesis, I investigate two techniques that extend the capability of SIS receivers. The first technique is extending the instantaneous bandwidth of the receivers, i.e., the intermediate frequency bandwidth (IFBW). For spectral line sources, wide IFBW expands the survey depth to allow multiple emission lines to be observed simultaneously. Here, I present a new SIS mixer device at 230 GHz. The planar circuit was minimised to reduce any parasitic capacitances that may limit the IFBW. Experimentally, the device provides excellent noise temperatures down to 36 K and an IFBW extending from approximately 0-11 GHz. Simulation software was developed to better understand the performance of this device, and it suggests that the IFBW can be extended to higher frequencies if the IF measurement chain is upgraded. The second technique that I investigate is increasing the number of receivers in the focal plane of the receiver, i.e., adding more pixels. There are many challenges involved in this task including how to fit multiple receivers into a small space, how to properly cool the receiver, and how to deliver the local-oscillator signal. Here, I present a new 1 × 4 focal plane array. This array is acting as a demonstrator for a new array architecture that can be expanded into many more pixels in the future. It uses cascaded waveguide power splitters to divide the local-oscillator signal, and then waveguide directional couplers to combine the LO with the astronomical signals. Finally, I present CO(J=1→0) measurements from 34 galaxies in the 5MUSES survey. These measurements trace the amount of cold molecular gas present in these galaxies. By comparing these measurements to other metrics that trace star formation activity (e.g., infrared luminosity), I was able to form empirical relationships between the observed quantities. I also combined these results with other star formation studies from nearby and high redshift galaxies to form scaling relationships spanning a large fraction of cosmic time.

<p>Cilj ovog rada je ispitivanje uticaja procesnih<br />parametara (transmembranski pritisak, protok i<br />koncentracija suspenzije) na vrednost fluksa<br />permeata, sa i bez prisustva statičkog me&scaron;ača,<br />tokom procesa mikrofiltracije suspenzija<br />p&scaron;eničnog skroba na keramičkim membranama<br />različitih veličina pora (200 nm i 500 nm).<br />Mikrofiltracija je izvođena u uslovima<br />recirkulacije i koncentrisanja napojne suspenzije.<br />Za modelovanje zavisnosti procesa mikrofiltracije<br />suspenzija skroba od procesnih parametara<br />primenjen je postupak odzivne povr&scaron;ine.<br />Ispitivanjem mikrofiltracije suspenzija p&scaron;eničnog<br />skroba na membranama sa različitim srednjim<br />prečnikom pora (200 i 500 nm) uočeno je da sa<br />povećanjem veličine pora vrednost fluksa<br />permeata opada.<br />U posmatranom eksperimentalnom opsegu<br />procesnih parametara postignuto je relativno<br />povećanje stacionarnog fluksa od 25% do 50% u<br />uslovima recirkulacije napojne suspenzije, dok je<br />u uslovima koncentrisanja napojne suspenzije<br />relativno povećanje srednjeg fluksa iznosilo od<br />20% do 80%. Porast fluksa do kojeg dolazi<br />postavljanjem statičkog me&scaron;ača u kanal membrane</p><p>uslovljen je uspostavljanjem turbulentnih uslova<br />proticanja i karakterističnog kretanja fluida duž<br />kanala membrane, koja je posledica<br />karakterističnog povezivanja helikoidnih<br />elemenata Kenics statičkog me&scaron;ača.<br />Kako u uslovima recirkulacije napojne sme&scaron;e,<br />tako i u uslovima koncentrisanja, vrednost<br />relativne specifične potro&scaron;nje energije zavisi skoro<br />isključivo od vrednosti protoka napojne sme&scaron;e. Sa<br />povećanjem protoka specifična potro&scaron;nja energije<br />u prisustvu statičkog me&scaron;ača naglo raste i<br />relativno povećanje protoka nije dovoljno da bi<br />kompenzovalo gubitak hidrauličke snage. U<br />opsegu protoka od 80 do 100 L/h su obezbeđene<br />pozitivne vrednosti relativne promene specifične<br />potro&scaron;nje energije, te je upotreba statičkog me&scaron;ača<br />opravdana sa ekonomskog aspekta.<br />Optimizacija eksperimentalnih uslova urađena je<br />postupkom istovremene maksimizacije fluksa<br />permeata u sistemima sa statičkim me&scaron;ačem i<br />relativne promene specifične potro&scaron;nje energije.<br />Optimalni uslovi izvođenja procesa mikrofiltracije<br />suspenzija p&scaron;eničnog skroba u uslovima<br />recirkulacije napojne suspenzije ukazuju da je<br />proces potrebno izvoditi pri maksimalnoj<br />vrednosti transmembranskog pritiska od 0,9 bara,<br />protocima od 85 do 100 L/h i koncentraciji od 5<br />do 6 g/L.<br />Optimalni uslovi izvođenja procesa mikrofiltracije<br />suspenzija p&scaron;eničnog skroba u uslovima<br />koncentrisanja napojne suspenzije ukazuju da je<br />proces potrebno izvoditi pri vrednosti<br />transmembranskog pritiska od 0,85 do 0,9 bara,<br />protocima od 85 do 100 L/h i koncentraciji od 5<br />do 7 g/L.<br />Pored ispitivanja na laboratorijskoj<br />aparaturi, cilj ovog rada je bio i ispitivanje uticaja<br />procesnih parametara na proces mikrofiltracije<br />suspenzija skroba u poluindustrijskim uslovima<br />(na jednokanalnoj i vi&scaron;ekanalnoj membrani<br />srednjeg prečnika pora 200 nm), odnosno &scaron;ireg<br />opseg vrednosti transmembranskog pritiska i<br />protoka suspenzije na pomenute odzive u<br />uslovima koncentrisanja napojne suspenzije.</p> / <p> The aim of this study was to investigate the effect of<br /> process parameters (transmembrane pressure, flow<br /> rate and suspension concentration) on the permeate<br /> flux in the system with and without the presence of<br /> static mixer. Microfiltration of wheat starch<br /> suspensions was performed in recirculation and<br /> concentration mode using ceramic membranes with<br /> different pore size (200 nm and 500 nm). Response<br /> surface methodology was applied for modeling<br /> cross-flow microfiltration of starch suspensions.<br /> During investigation of starch suspension<br /> microfiltration process on membranes with different<br /> pore size diameter (200 and 500 nm) it was<br /> observed that with increasing pore size the permeate<br /> flux declined.<br /> In the experimental range of process parameters,<br /> flux increase had values between 25% and 50% in<br /> recirculation mode, while in concentration mode<br /> this improvement was in range between 20% and 80%. The increase in flux that occurs by placing a</p> <p> static mixer in the membrane channel was caused<br /> by the establishment of turbulent flow conditions<br /> and the characteristic flow of fluid along the<br /> membrane channel, which is a consequence of the<br /> characteristic geometry of Kenics static mixer.<br /> Both in recirculation and concentration mode, the<br /> reduction of specific energy consumption depends<br /> almost exclusively on the value of the suspension<br /> flow rate. Specific energy consumption increased<br /> rapidly with increasing flow rate in the presence of<br /> static mixers and flux improvement is not high<br /> enough to compensate the loss of hydraulic<br /> dissipated power. The flow rate in the range from<br /> 80 to 100 L/h provided positive values of the<br /> reduction of specific energy consumption and the<br /> use of static mixers was justified from the<br /> economical point of view.<br /> Optimization of experimental conditions was done<br /> by a procedure of simultaneous maximization of<br /> permeate flux in systems with static mixers and<br /> reduction of specific energy consumption. Optimal<br /> conditions of the wheat starch suspension<br /> microfiltration in recirculation mode indicate that<br /> the process should be conducted at the maximum<br /> value of transmembrane pressure of 0.9 bar, flow<br /> rates from 85 to 100 L/h and concentration of 5 to 6<br /> g/L.<br /> Optimal conditions of the wheat starch suspension<br /> microfiltration in concentration mode indicate that<br /> the process should be conducted when the value of<br /> transmembrane pressure from 0.85 to 0.9 bar, flow<br /> rates from 85 to 100 L/h and concentration of 5 to 7<br /> g/L.<br /> Apart from investigations in laboratory conditions,<br /> the aim of this study was to examine the influence<br /> of process parameters on the starch suspensions<br /> microfiltration in the pilot plant (one channel and<br /> multichannel membrane with pore diameter 200<br /> nm) and wider range of transmembrane pressure<br /> and suspension flow rate on the mentioned<br /> responses in concentration mode.</p>

In this thesis, design aspects of fully integrated multibandmultistandard front-end receivers are investigated based onthree fundamental aspects: noise, linearity and operatingfrequency. System level studies were carried out to investigatethe effects of different modulation techniques, duplexing andmultiple access methods on the noise, linearity and selectivityperformance of the circuit. Based on these studies and thelow-cost consideration, zero-IF, low-IF and wideband-IFreceiver architectures are promising architectures. These havea common circuit topology in a direct connection between theLNA and the mixer, which has been explored in this work toimprove the overall RF-to-IF linearity. One front-end circuitapproach is used to achieve a low-cost solution, leading to anew multiband multistandard front-end receiver architecture.This architecture needs a circuit whose performance isadaptable due to different requirements specified in differentstandards, works across several RF-bands and uses a minimumamount ofexternal components. Five new circuit topologies suitable for a front-endreceiver consisting of an LNA and mixer (low-noise converter orLNC) were developed. A dual-loop wide-band feedback techniquewas applied in all circuits investigated in this thesis. Threeof the circuits were implemented in 0.18 mm RF-CMOS and 25 GHzbipolar technologies. Measurement results of the circuitsconfirmed the correctness of the design approach. The circuits were measured in several RF-bands, i.e. in the900 MHz, 1.8 GHz and 2.4 GHz bands, with S11 ranging from–9.2 dB to–17 dB. The circuits have a typicalperformance of 18-20 dB RF-to-IF gain, 3.5-4 dB DSB NF and upto +4.5 dBm IIP3. In addition, the circuit performance can beadjusted by varying the circuit’s first-stage biascurrent. The circuits may work at frequencies higher than 3GHz, as only 1.5 dB of attenuation is found at 3 GHz and nopeaking is noticed. In the CMOS circuit, the extrapolated gainat 5 GHz is about 15 dB which is consistent with the simulationresult. The die-area of each of the circuits is less than 1mm2.

This final year project describes the linearisation method Cartesian feedback and the design of such a feedback with a 2.4GHz power amplifier. To investigate the functionality of the Cartesian feedback ideal blocks with no current consumption were made and then gradually analog circuits were introduced into the feedback. The Cartesian feedback design consists of a subtracter, a modulator and a preamplifier in the top path and a demodulator and a filter in the feedback path. The blocks that are discussed in this report are the subtracter and the modulator unit. The circuits are designed in a 0.35µm SiGe BiCMOS technology. The result of the Cartesian feedback showed an increase in 1dB compression point by 6.2dBm and the IMD was improved by 17dB.

Low power wireless communications is the most demanding request among all wireless users. A battery life that can survive for years without being replaced, makes it realistic to implement many applications where the battery is unreachable (e.g. concrete walls) or expensive to change (e.g underground applications). IEEE 802.15.4/ZIGBEE standard is published to cover low power low cost applications, where the battery life can last for years, because of the 1% duty cycle of operation. A fully integrated 2.4GHz IEEE802.15.4 Compliant transceiver suitable for low power, low cost ZIGBEE applications is implemented. Direct conversion architecture is used in both Receiver and Transmitter, to achieve the minimum possible power and area. The chip is fabricated in a standard 0.18um CMOS technology. In the transmit mode, the transmitter chain (Modulator to PA) consumes 25mW, while in the receive mode, the iv receiver chain (LNA to Demodulator) consumes 5mW. The Integer-N Frequency Synthesizer consumes 8.5mW. Other Low power circuits are reported; A 13.56 Passive RFID tag and a low power ADC suitable for Built-In-Testing applications.

In this work, a 3.5 GHz RF Transmitter and Successive Approximation ADC design has been presented. The transmitter serves as an intermediate block which translates 350 MHz signal into 3.5 GHz signal. This signal is applied to 6-40 GHz wideband transmitter. The emphasis is on the design of Up conversion Mixer with high linearity, low noise and moderate image rejection performance. The successive approximation analog to digital converter was designed as a part of feedback loop control, which consists of a sensor circuit to detect the temperature changes in a power amplifier and the ADC to convert the sensor output to digital data. The data is used to determine the necessary control signals to restore the performance of the power amplifier. The circuits have been designed and implemented in ST Microelectronics CMOS 90nm process.

In the flow distribution section of a paper machine, known as the head box, water is injected into the fiber suspension (stock) flow through a tee-mixer for more uniform production. This dilution process has two important requirements that must be fulfilled: (1) sufficient mixing so that the dilution flow spreads across the suspension flow and (2) that the injection flow rate not be so large to significantly alter the local head box flow rate. The objective of this research was to find a combination of velocity ratio and tee mixer geometry that lead to the injection flow being well mixed into the stock flow, but at the same time, the injection should not cause the total flow rate to change by more than 1%. Velocity ratios of 0.25, 0.75, 1.33, 1.5 and 2.25 were examined for four different cases of tee mixer geometries using the CFD software Fluent. Two of the cases had added contractions located near the injection point, while the other two cases had a more standard geometry with no added complexities. The pressure drop across the injection point was also measured. Mixing was qualitatively measured by simulating the injection of a passive tracer into the dilution flow. All of the results indicated that the case where the contraction was located after the injection showed the most promising results with quality mixing and lower flow rates. The cases without added contractions showed poor mixing for lower velocity ratios, and for higher velocity ratios, the flow rates were too large. The cases with contractions showed similar mixing, but the outlet flow rates produced were lower when the contraction was located after the injection instead of before it. A velocity ratio of 0.25-0.75 for the mixers with contractions produced acceptable flow rates and sufficient mixing. The simulations also showed that the static pressure for the contraction cases were nearly identical throughout the majority of the pipe. For both contraction cases the pressure drop across the injection increased with increasing injection flow rate. When the contraction was located before the injection, a pressure drop of 16% was calculated. A pressure drop of 18% to 20% across the injection resulted when the contraction was located after the injection.