A New 76Ge Double Beta Decay Experiment at LNGS

This Letter of Intent has been submitted to the Scientific Committee of the INFN Laboratori Nazionali del Gran Sasso (LNGS) in March 2004. It describes a novel facility at the LNGS to study the double beta decay of 76Ge using an (optionally active) cryogenic fluid shield. The setup will allow to scrutinize with high significance on a short time scale the current evidence for neutrinoless double beta decay of 76Ge using the existing 76Ge diodes from the previous Heidelberg-Moscow and IGEX experiments. An increase in the lifetime limit can be achieved by adding more enriched detectors, remaining thereby background-free up to a few 100 kg-years of exposure.Comment: 67 pages, 19 eps figures, 17 tables, gzipped tar fil

Simulation-optimization framework for synthesis and design of natural gas downstream utilization networks

Many potential diversification and conversion options are available for utilization of natural gas resources, and several design configurations and technology choices exist for conversion of natural gas to value-added products. Therefore, a detailed mathematical model is desirable for selection of optimal configuration and operating mode among the various options available. In this study, we present a simulation-optimization framework for the optimal selection of economic and environmentally sustainable pathways for natural gas downstream utilization networks by optimizing process design and operational decisions. The main processes (e.g., LNG, GTL, and methanol production), along with different design alternatives in terms of flow-sheeting for each main processing unit (namely syngas preparation, liquefaction, N2 rejection, hydrogen, FT synthesis, methanol synthesis, FT upgrade, and methanol upgrade units), are used for superstructure development. These processes are simulated using ASPEN Plus V7.3 to determine the yields of different processing units under various operating modes. The model has been applied to maximize total profit of the natural gas utilization system with penalties for environmental impact, represented by CO2eq emission obtained using ASPEN Plus for each flowsheet configuration and operating mode options. The performance of the proposed modeling framework is demonstrated using a case study. 2018 by the authors.The authors would like to acknowledge the financial support from NSERC and from Qatar University to conduct this research. A.E. and M.A.S. would also like to acknowledge the Gas Research Center (GRC) at the Petroleum Institute during the later stages of this research.Scopu

Control of a train of high purity distillation columns for efficient production of 13C isotopes

It is well-known that high-purity distillation columns are difficult to control due to their ill-conditioned and strongly nonlinear behaviour. The fact that these processes are operated over a wide range of feed compositions and flow rates makes the control design even more challenging. This paper proposes the most suitable control strategies applicable to a series of cascaded distillation column processes. The conditions for control and input-output relations are discusssed in view of the global control strategy. The increase in complexity with increased number of series cascaded distillation column processes is tackled. Uncertainty in the model parameters is discussed with respect to the dynamics of the global train distillation process. The main outcome of this work is insight into the possible control methodologies for this particular class of distillation processes

Techno-economic analysis of expander-based configurations for natural gas liquefaction

The use of liquefied natural gas (LNG) as a marine fuel is rapidly growing because of the possible economic advantages over conventional fuels and stricter environmental regulations. Production of LNG is energy intensive because of the required temperature level of around -160\ub0C. Three main types of refrigeration cycles have been developed. The present work focuses on the comparison of six expander-based configurations, which in spite of the higher power consumption, are more compact, flexible and easier to operate. They are optimised from a thermodynamic perspective: the exergetic efficiency is found to range between 17 % and 33 % for a specific power consumption down to 1340 kJ/kg. Multi-objective optimisations are performed to simultaneously minimise the net power consumption and the heat transfer conductance as an indicator of the required heat transfer area. The latter ranges between 50 kW/K and 300 kW/K. A trade-off between power consumption and heat transfer area is found, which justifies a further economic analysis. A simplified economic analysis is set based on a discounted cash flow model. The unitary profit ranges between 0.5 and 0.9 DKK/kg of produced LNG. The most profitable expander-based configuration is the dual-refrigerant cycle with nitrogen in the bottoming refrigeration cycle. Finally, the influence of the cost correlations on the economic outcome is assessed: the compressors represent the major costs, which leads to the coincidence of the thermodynamic and economic optima

Optimized Design of Shale Gas Processing and NGL Recovery Plant under Uncertain Feed Conditions

Shale gas is an increasingly booming resource and it has been predicted to increase from 1% in 2000 to 40% in 2035 of the total US domestic gas produced. Since shale gas is both industrially economical and environmentally clean compared to oil or coal as a resource, many studies are focused on developing technologies to monetize shale gas. However, one of the key challenges in utilizing shale gas is its fluctuating flow rate and compositional behavior. The flow rate of a shale gas well dwindles over a period of time and the composition of shale gas differs from well to well in the same shale play. This provides a challenge in designing a plant of optimum size for a shale gas processing and NGL recovery plant. In this study, this uncertainty in shale gas feed flow rate and composition is addressed while designing a shale gas processing and NGL recovery plant. First, different shale gas flow rates are chosen over a period of shale gas well life based on the average shale gas rate declination curve of a shale play. Second, two different process flow sheets are developed (i) using conventional technology and (ii) using novel technology. In the novel technology, the NGL recovery section of the conventional technology is modified to accommodate novel changes such as using a divided wall column or pre-fractionated sequence to separate methane, ethane, and propane. Later, these process flow sheets are simulated in Aspen plus for comparing the economics of different plant sizes. Furthermore, heat integration and optimization of individual units of the process flow sheets are carried out using pinch and sensitivity analyses, respectively. Lastly, the economic analysis of a plant of optimum size with constant feed flow rate over its plant life is evaluated. In this case, shale gas from different wells is collected in a header and adjusted such that the shale gas flow rate is constant to the plant. Environmental impact of the process is also observed. From the economic analysis of various cases for conventional and novel technology, it is observed that case-3 provides the optimum plant design with highest ROI percentage compared to other cases and for case-3, novel technology ROI is 4.17% more compared to conventional technology. Finally, constant production rate case, at the flow rate of case-3, the ROI percentage is observed to be more than minimum requirement implying that this processing plant is economically viable to implement

천연가스 공급망 내 초구조 최적화 및 다중모듈방식을 이용한 공정설계 및 운전

학위논문 (박사)-- 서울대학교 대학원 : 공과대학 화학생물공학부, 2019. 2. 이원보.본 논문은 공정시스템 분야의 최신기술 수요에 상응하는 최적 공정설계 및 운전기술 개발을 주목적으로 한다. 최근 셰일가스 등 변화하는 천연가스 자원으로부터 지속적인 부가가치 창출과 플랜트의 내재적 안전성을 제고할 수 있는 설계 및 운전을 도모하였다는 점에서 실제 산업에의 응용가치가 매우 높다. 첫 번째로 천연가스 가솔린회수 및 액화 통합공정에 질소회수공정을 추가하여, 저품질 천연가스로부터 지속적인 액화천연가스 생산이 가능한 공정을 설계하였다. 열교환망 및 분리공정 최적화를 위해 공정요소들의 엑서지를 최소화할 수 있는 초구조를 설계함으로써 기존의 연구가 찾지 못하였던 새로운 최적 구조 및 운전조건을 결정하였다. 나아가 서로 다른 천연가스 조성에 따라 각기 적용이 가능한 대안공정을 추가 설계·최적화함으로써 변화되는 천연가스 자원에 지속적인 가치창출을 위한 해답을 제시하고 있다. 두 번째로 공정의 예비설계단계에서 내재적 안전성의 개념을 도입하여, 경제성과 안전성의 균형을 유지하기 위한 새로운 다목적최적화 알고리즘을 개발하였다. 잠재적 위험도가 높은 천연가스 액화공정을 대상으로 액화사이클에 따른 초구조를 모사하여 두 가지 목적함수의 가중치에 따른 최적해를 결정함으로써 기존 최적화의 한계를 보완하였다. 마지막으로 플랜트 안전운전을 위해 공정이상에서부터 사고의 발생 및 전파과정을 실시간으로 구현할 수 있는 시뮬레이션 모듈을 개발하였다. 동적공정시뮬레이션 및 사고시뮬레이션의 두 가지 독립된 모듈을 객체연결매입 기법을 이용하여 연동함으로써 사고상황에서 운전원의 임의조치가 모듈에 실시간 반영되도록 하였다. 해당 모듈은 임의의 사고상황에서 제어실 및 현장 운전원의 적절한 대응을 효과적으로 유도할 수 있으며 나아가 플랜트 안전시스템설계에 객관화된 지표를 제시할 수 있었다. 본 논문은 위와 같이 실제 산업의 기술적 수요를 충족시키고 이를 발전시킴으로써 공정시스템 학술분야에 기여하였다.Recently in the field of process systems engineering in natural gas processing, various researches trying to make changes in the existing framework of process design and operation have been studied with the emerging need of sustainability and safety in the chemical processes. These two considerations of sustainability and safety either result in a totally new solution for a certain decision making or require far different methods or technologies for it. Especially for a natural gas supply chain broadly from drilling of the gas/oil reservoirs to distributing the product gas to end-users like households or offices, new frameworks of process design and operation critically influence the way of producing desired products and supplying them to the users in the associated industries. Then it determines the structure, operating conditions, and operation procedures of chemical processes which are economically powerful and good in operability. Recently, as the natural gas sources becomes unconventional varying from mid-to-small size reservoirs or shale gases, this change makes the offshore natural gas plants emerge as an alternative and vital site of producing LNG (liquefied natural gas) with strict requirements of safety. It also makes additional processing units like a cryogenic nitrogen recovery be necessary for sustainable production of LNG with leaner feed natural gases. Among various processes in the overall natural gas supply chain, this thesis dealt with largely three parts including gas pre-treatment, liquefaction, and distribution to the end-users, attempting to design new processes or develop new methods of decision making in the context of the new framework considering sustainability and safety in process systems engineering. In this thesis, I will discuss the process synthesis, intensification, and optimization for sequential units, multi-objective optimization for economic feasibility and inherent safety, and multi-modular approach for interactive simulation of dynamic process and 3D-CFD (computational fluid dynamics) accident models. First of all, for designing a sustainable process of producing LNG from feed natural gases with high amounts of nitrogen, two cryogenic nitrogen recovery processes integrated with LNG production and NGL (natural gas liquid) recovery were designed and optimized based on the structural analysis of components separation: one for integrated nitrogen recovery unit and the other for standalone one. The difference of each process is the way the nitrogen is removed from the natural gas. The former recovers nitrogen in the integrated heat and mass transfer structure with natural gas liquefaction while the latter separates the nitrogen recovery unit into an independent structure apart from the liquefaction section. These sophisticated nitrogen recovery solutions follow the recent demand of highly efficient electric motors as alternative compressor drivers which require less or no fuel gas, the major sink of nitrogen in the feed gas. These two processes were compared with each other in terms of specific power (kWH/kg_LNG), which is equivalent to the overall process efficiency, with respect to the nitrogen content in the feed gas from 0mol% to 20mol%. Consequently, as the nitrogen content in the feed gas increases, the specific power of each process also increases while the standalone solution has a priority over the other until around 17mol% of nitrogen and after that point the integrated solution becomes relatively more efficient. It should be noted that all of the optimization results of each configuration were improved with the reduced specific power by up 38.6% compared to those from previous studies which have similar configurations. The way this study aimed could be reasonable guidelines for other chemical process designs as well as nitrogen recovery in natural gas processing. Secondly, for designing a safer process of natural gas processing, two different systematic approaches were newly proposed in this study: one for risk reduction method based on rigorous QRA (quantitative risk assessment) results through process design modification of an existing plant which already finished up to the detailed design stage, and the other for deciding an optimal process design through multi-objective optimization for minimizing both the TAC (total annual cost) and the risk (fatality frequency) at the preliminary design stage. This latter approach could largely lower the cost required for finalizing the design as it doesnt need to follow the general QRA procedure where the recursive loop is recycled until the risk is reduced to an acceptable level. But before this approach starts to be applied, the suitability of its method should be verified as it has to make some assumptions in assessing the safety level of the process with limited information. Also the computation load would be higher as it needs to simultaneously consider the economic feasibility and inherent safety in designing a process. Despite the differences these two approaches have each other, however, they are essentially in the same context in that they share the same purpose of deciding a process design which is safer and/or even cheaper than the existing processes. Consequently, for the former approach of which the target process is the GTU (gas treatment unit) of an existing GOSP (gas oil separation plant) for processing associated natural gas, the modified design with different operation conditions reduced the total risk integrals by 27% at the expense of only the additional $50,000 for capital cost. In addition, sensitivity analysis of total risk with respect to probability of success for safety barriers was carried out in order to show the preferences of process design modification, this study proposed, over the improvement of safety systems. Meanwhile, the latter approach of superstructure formulation and multi-objective optimization for designing an optimal heat transfer structure and operating conditions was applied to the natural gas liquefaction processes, deciding that the SMR (single-stage mixed refrigerant process) structure with the TAC of 626.6MM$/yr and fatality frequency of 1.28E-03/yr has the highest priority over all possible solutions. Finally, with the aim of safely operating a chemical plant, a new operator training module which mainly targets the interactive cooperation of control room operators and field operators was developed through using multi-modular approach with advanced simulations and data processing technologies. This interactive simulation modeling delivers the online simulation results of process operation to the operators and induces them to take proper actions in case of a random accidental situation among pre-identified scenarios in a chemical plant. Developed model integrates the real-time process dynamic simulations with the off-line database of 3D-CFD accident simulation results in a designed interface using OLE (Object Linking and Embedding) technology so that it could convey the online information of the accident to trainees which is not available in existing operator training systems. The model encompasses the whole process of data transfer till the end of the training at which trainees complete an emergency shutdown system in a programmed model. The developed module was applied to a natural gas pressure regulating station where the high pressure gas is depressurized and distributed to the end-users like households or offices. An overall scenario is simulated in the interactive simulation model, which starts from an abnormal increase of the discharge (2nd) pressure of the main valve due to its malfunction, spreads to an accidental gas release through the crack of a pressure recorder, and ends with gas dispersion and explosion. Then the magnitude of the accident outcomes with respect to the lead time of each trainees emergency response is analyzed. Consequently, the module could improve the effectiveness of operator training system through interactively linking the trainee actions with the model interface so that the associated accident situations would vary with respect to each trainees competence facing an accident.Abstract i Table of Contents vii List of Figures x List of Tables xiv CHAPTER 1. Introduction 1 1.1. Research motivation 1 1.2. Research objectives 4 1.3. Outline of the thesis 6 1.4. Associated publications 11 CHAPTER 2. Process Intensification 12 2.1. Introduction 13 2.2. Conceptual Design of the Nitrogen Recovery 17 2.3. Design Improvement and Optimization 26 2.3.1. Integrated Nitrogen Recovery Unit 26 2.3.2. Optimization of the Base Case 32 2.3.3. Design Improvement 40 2.4. Alternative Process Design and Optimization 65 2.4.1. Standalone Nitrogen Recovery Unit 65 2.4.2. Optimization of Standalone Nitrogen Recovery Unit 74 2.4.3. Comparison between End-flash and Stripping Options 78 2.5. Varying Feed Composition and Optimization 95 2.6. Concluding Remarks 105 CHAPTER 3. Safer Process Design 107 3.1. Introduction 109 3.2. Risk Reduction through Process Design Modification 112 3.2.1. Risk Assessment for the Target Process 113 3.2.2. Risk Reduction to ALARP 141 3.3. Multi-objective Optimization Including Inherent Safety 154 3.3.1. New Decision Making Schemes for Inherent Safety 159 3.3.2. Superstructure for Natural Gas Liquefaction Processes 168 3.3.3. Multi-objective Optimization 187 3.3.4. Decision Making for Final Optimal Solution 203 3.3.5. Future Works 208 3.4. Concluding Remarks 210 CHAPTER 4. Safe Operation with Multi-modular Approach 212 4.1. Introduction 213 4.2. Interactive Simulation Modeling 218 4.2.1. Model Structure 218 4.2.2. Dynamic Process and Accident Simulation Engine 221 4.2.3. Real-time 3D-CFD Data Processing Method 225 4.3. Case Study – Pressure Regulating Station 231 4.3.1. Developing a Program Prototype 231 4.3.2. Prototype Test and Training Evaluation 252 4.4. Concluding Remarks 256 CHAPTER 5. Conclusion 257 Nomenclature 261 Reference 263 Abstract in Korean (국문초록) 270Docto

CIS-lunar space infrastructure lunar technologies: Executive summary

Technologies necessary for the creation of a cis-Lunar infrastructure, namely: (1) automation and robotics; (2) life support systems; (3) fluid management; (4) propulsion; and (5) rotating technologies, are explored. The technological focal point is on the development of automated and robotic systems for the implementation of a Lunar Oasis produced by Automation and Robotics (LOAR). Under direction from the NASA Office of Exploration, automation and robotics were extensively utilized as an initiating stage in the return to the Moon. A pair of autonomous rovers, modular in design and built from interchangeable and specialized components, is proposed. Utilizing a buddy system, these rovers will be able to support each other and to enhance their individual capabilities. One rover primarily explores and maps while the second rover tests the feasibility of various materials-processing techniques. The automated missions emphasize availability and potential uses of Lunar resources, and the deployment and operations of the LOAR program. An experimental bio-volume is put into place as the precursor to a Lunar environmentally controlled life support system. The bio-volume will determine the reproduction, growth and production characteristics of various life forms housed on the Lunar surface. Physicochemical regenerative technologies and stored resources will be used to buffer biological disturbances of the bio-volume environment. The in situ Lunar resources will be both tested and used within this bio-volume. Second phase development on the Lunar surface calls for manned operations. Repairs and re-configuration of the initial framework will ensue. An autonomously-initiated manned Lunar oasis can become an essential component of the United States space program

“Blue” Hydrogen & Helium From Flare Gas Of The Bakken Formation Of The Williston Basin, North Dakota: A Novel Process

Is it possible to curtail flaring in the Williston basin while simultaneously sequestering carbon dioxide, harvesting economic quantities of natural gas liquids, helium and other valuable products? Utilizing a novel approach described here, diatomic hydrogen and elemental helium, as well as other products, can be profitably extracted from the gas streams produced from horizontal, hydraulically-fractured Middle Bakken Member wells, in the Devonian-Mississippian Bakken Formation of the Williston Basin, North Dakota, USA.However, there are two vastly different methods employed to extract these gasses. Hydrogen is harvested from the gas stream by physically reforming methane (CH4) through the application of one or another of two-stage processes: “Autothermal Reformation + Water Gas Shift (WGS) reaction”, known as ATR; or “Steam Methane Reforming”, SMR. Both yield H2, plus CO (carbon monoxide) in the first phase, and CO2 (carbon dioxide) after the second. Elemental diatomic hydrogen (H2) can be used in fuel cells to generate electricity or directly in certain internal combustion engines; primarily turbines, as primary fuel. The produced CO2 can be captured (CCUS: Carbon Capture, Utilization and Sequestration) and injected downhole for both reservoir energy enhancement and CO2 sequestration, or sold for industrial use because of its purity. Helium, on the other hand, is inert and therefore it is unnecessary to expend the amount of energy required to reformat methane to liberate hydrogen. There are several methods commercially available to economically extract 99.995% pure helium from gas streams where the helium concentration can be as low as 0.010%. The extraction of crude helium from natural gas requires three processing steps. The first step removes impurities through deamination, glycol absorption, nitrogen rejection, and desiccant adsorption, which remove CO2, H2O, N2, and H2S; a typical gas pre-treatment process. The second step removes high-molecular weight hydrocarbons (Natural Gas Liquids), if desired, while the third step is via cryogenics, which removes the final methane. The result is 75-90% pure helium. Final purification, before liquefaction, is accomplished via activated charcoal absorbers at liquid-nitrogen temperatures and high pressure, or pressure-swing adsorption (PSA) processes. Low-temperature adsorption can yield helium purities of 99.99 percent, while PSA processes recover helium at better than 99.9999 percent purity. However, with the advent of selective zeolite or organometallic membranes, the cryogenic extraction of He from the CH4 stream step can be eliminated. Heating the gas stream and passing it through selective semi-permeable membranes allow for the helium, with its much smaller size, and higher energy, pass while excluding the relatively massive CH4 molecule. The helium can be isolated and purified via pressure swing adsorption (PSA) methods to achieve 99.999% purity. The heated methane can then be directly ported to a Steam Methane Reformer unit for extraction of hydrogen. Both H2 and He extraction procedures eliminate the need for gas flaring, as both yield salable products such as LNG and NGLs, and the opportunity to capture and sequester carbon dioxide (CO2) from the produced gas stream. This extracted so-called “Blue Hydrogen” is slated for use in transportation via fuel cells or use in internal combustion engines and sells for approximately $3.00/MCF, depending on the cost of the feedstock natural gas. “Metallurgical helium” or “Grade-A Helium” (i.e., \u3e 99.9999$498/MCF (02-2023). The cost of hydrogen vs. helium extraction is difficult to compare. Hydrogen production depends on the cost of natural gas as a feedstock, which is particularly variable. The cost of helium extraction depends on the volume of gas being processed, as most helium extraction units could handle 10-12 Bakken wells simultaneously. However, as a straight-up market product, helium revenue exceeds hydrogen by a factor of 100. Doing both coincidental from the same gas stream will enhance the revenue of each