小型LNG装置的模块化撬装工艺技术

以中原油田文23气田1号集气站外输气为例,对小型LNG装置的模块化撬装进行了工艺技术研究,采用特有的模块化复合吸附工艺和SP-MRC混合制冷工艺,得到天然气净化与液化相耦合的全流程节点的温度、压力、摩尔焓、摩尔熵、摩尔流量、气相分率和气液两相组分的摩尔分数。结果表明：LNG回收率＞90%,该装置的能耗成本仅为0.379 kW·h·m^-3,相当于0.19元·m^-3天然气。     

Low-cost small scale processing technologies for production applications in various environments—Mass produced factories

The requirements for chemical and food production technologies will change in the future as a result of shorter time to market and increasing market volatility. Especially the rising use of renewable resources will require the implementation of flexible and fast to install small-scale production technologies. The increasing number of necessary apparatuses and their distributed operation, however, will constitute major challenges, both economically and procedurally.The proposed solution to face the economic challenge is modularization and standardization. For food production, dewatering represents a key issue. Thus, biomass processing should first be divided into small-scale water separation steps and then into further large-scale processing steps. As dewatering usually happens thermally and heat exchangers often benefit from the economies of scale, heat supply and energy consumption or heat transfer with little capital investment are further issues. Therefore, temperature levels should be decreased and the use of solar heat increased. For the production of biofuels and chemicals from biomass, process integration and process simplification are proposed to improve the efficacy of production equipment and processes. Choosing raw materials with molecular structures, similar to the desired chemical building block, will lower the need for heat exchange and make small-scale manufacturing of fuels and chemicals possible.     

GSP粉煤气化生产天然气变换工艺改进的探讨

主要分析了GSP粉煤气化工艺粗煤气成分的特点,并结合已有变换工艺的运行状况,分析了如何在GSP粉煤气化技术制取天然气的工艺路线中对变换工艺的设计上提出改进,目的在于优化变换设计、充分回收变换反应余热、降低消耗及变换装置的投资成本。     

Novel Natural Gas to Liquids Processes: Process Synthesis and Global Optimization Strategies

An optimization‐based process synthesis framework is proposed for the conversion of natural gas to liquid transportation fuels. Natural gas conversion technologies including steam reforming, autothermal reforming, partial oxidation to methanol, and oxidative coupling to olefins are compared to determine the most economic processing pathway. Hydrocarbons are produced from Fischer–Tropsch (FT) conversion of syngas, ZSM‐5 catalytic conversion of methanol, or direct natural gas conversion. Multiple FT units with different temperatures, catalyst types, and hydrocarbon effluent compositions are investigated. Gasoline, diesel, and kerosene are generated through upgrading units involving carbon‐number fractionation or ZSM‐5 catalytic conversion. A powerful deterministic global optimization method is introduced to solve the mixed‐integer nonlinear optimization model that includes simultaneous heat, power, and water integration. Twenty‐four case studies are analyzed to determine the effect of refinery capacity, liquid fuel composition, and natural gas conversion technology on the overall system cost, the process material/energy balances, and the life cycle greenhouse gas emissions. © 2013 American Institute of Chemical Engineers AIChE J, 59: 505–531, 2013     

Production of benzene,toluene, and xylenes from natural gas via methanol: Process synthesis and global optimization

A systematic global optimization‐based process synthesis framework is presented to determine the most profitable processes to produce aromatics from natural gas. Several novel, commercial, and/or competing technologies are modeled within the framework, including methanol‐to‐aromatics, toluene alkylation with methanol, selective toluene disproportionation, and toluene disproportionation and transalkylation with heavy aromatics, among others. We propose a stand‐alone chemicals facility: the main products are aromatics with allowable by‐products of gasoline, liquefied petroleum gas, and electricity. Several case studies are discussed that produce varying ratios of para‐, ortho‐, and meta‐xylene across multiple refinery capacities. The results indicate that utilizing natural gas for the production of aromatics is profitable with net present values as high as $3800 MM dollars and payback periods as low as 6 years. The required investment for these refineries represents as much as a 65% decrease compared to published estimates of similar coal‐based capacity plants. © 2016 American Institute of Chemical Engineers AIChE J, 62: 1531–1556, 2016     

Covariance‐based hardware selection‐part III: Distributed parameter systems

In this article, we propose a new method for the selection of control system hardware (sensors and actuators) for distributed parameter systems. The proposed design scheme seeks to minimize the capital cost of hardware while satisfying predefined performance constraints. Within this minimum capital cost framework, three design scenarios will be discussed; the closed‐loop full state information actuator selection problem, the open‐loop partial state information sensor selection problem, and the closed‐loop partial state information simultaneous sensor and actuator selection problem. The proposed method will be illustrated through application to a nonisothermal tubular reactor example. © 2011 American Institute of Chemical Engineers AIChE J, 2012     

Integrated solvent and process design using a SAFT-VR thermodynamic description: High-pressure separation of carbon dioxide and methane

The increasing importance of natural gas as an energy source poses separation challenges, due to the high pressures and high carbon dioxide concentrations of many natural gas streams. A methodology for computer-aided molecular and process design (CAMPD) applicable to such extreme conditions is presented, based on the integration of process and cost models with an advanced molecular-based equation of state, the statistical associating fluid theory for potentials of variable range (SAFT-VR). The approach is applied to carbon dioxide capture from methane using physical absorption. The search for an optimal solvent is focused on n-alkane blends. A simple flowsheet is optimised using two objectives: maximum purity and maximum net present value. The best equipment sizes, operating conditions, and average chain length of the solvent (the n-alkane) are identified, indicating n-alkane solvents offer a promising alternative. The proposed methodology can readily be extended to wider classes of solvents and to other challenging processes.     

Discovery of novel zeolites for natural gas purification through combined material screening and process optimization

An efficient computational screening approach is proposed to select the most cost‐effective materials and adsorption process conditions for CH₄/CO₂ separation. The method identifies eight novel zeolites for removing CO₂ from natural gas, coalbed methane, shale gas, enhanced oil recovery gas, biogas, and landfill gas sources. The separation cost is minimized through hierarchical material screening combined with rigorous process modeling and optimization. Minimum purity and recovery constraints of 97 and 95%, respectively, are introduced to meet natural gas pipeline specifications and minimize losses. The top zeolite, WEI, can recover methane as economically as $0.15/MMBTU from natural gas with 5% CO₂ to $1.44/MMBTU from natural gas with 50% CO₂, showing the potential for developing natural gas reservoirs with higher CO₂ content. The necessity of a combined material selection and process optimization approach is demonstrated by the lack of clear correlation between cost and material‐centric metrics such as adsorption selectivity. © 2014 American Institute of Chemical Engineers AIChE J, 60: 1767–1785, 2014     

Equation‐oriented simulation and optimization of process flowsheets incorporating detailed spiral‐wound multistream heat exchanger models

Multiple chemical processes rely on multistream heat exchangers (MHEXs) for heat integration, particularly at cryogenic temperatures. Owing to their geometric complexity, the detailed design of MHEXs is typically iterative: the exchanger geometric parameters are selected to match process specifications resulting from a flowsheet optimization step; then, the flowsheet is reoptimized with the predictions of the MHEX model, and these steps are repeated until a convergence criterion is met. This paper presents a novel framework that allows—for the first time, to our knowledge—for the simultaneous optimization of the process flowsheet and the detailed MHEX design. Focusing on spiral‐wound MHEXs, we develop an equation‐oriented exchanger model using industry‐accepted heat transfer and pressure drop correlations for single‐phase and multiphase streams. We embed this model in our previously developed pseudo‐transient equation‐oriented process simulation and optimization framework. We demonstrate our approach on an industrial case study, the PRICO^® natural gas liquefaction process. © 2017 American Institute of Chemical Engineers AIChE J, 63: 3778–3789, 2017     

浮式LNG生产储卸装置关键设计技术对比分析

海上石油伴生气的液化及储存是一个复杂的系统工程,对装置有特殊的要求,主要体现在：狭小空间场地、海浪和船体的晃动对设备的影响、海上LNG储槽中液体晃动的安全问题、LNG从FPSO向运输船的安全卸载外输方式等。根据我国南海海域的自然条件及油田伴生气源组分特点,作者对浮式LNG生产储卸装置的关键技术进行了一系列的研究,包括FPSO总体方案、净化流程工艺、液化流程工艺、LNG储存、LNG卸载运输、FPSO动力、安全与平面布局等,取得了一定进展,本文对上述问题做了扼要阐述和介绍。     

Methanol Synthesis by Direct Oxidation of Natural Gas at Thermal Power Plants

Methanol synthesis by the partial oxidation of natural gas before its combustion in a power unit is considered as an alternative to modern large-scale methanol synthesis from natural gas through synthesis gas. The process suggested makes it possible to reduce nitrogen oxide emission by diluting the combustible mixture with nitrogen without extra capital expenditures.     

煤制甲醇工艺甲醇合成塔的工艺设计探讨

以30万吨/年焦炉气制甲醇项目各工序的压力、温度、介质成分、流量等工艺条件,确定合成塔设备排热量及结构形式。甲醇合成塔又称甲醇合成反应器,是甲醇装置中的核心设备之一,也是合成工段中最关键的设备,合成塔为立式绝热管壳型反应器,管内装有C306型低压合成甲醇催化剂,本设计的目的是按照工艺要求设计甲醇合成工段甲醇合成塔,为压力容器设计提供理论依据。     

15万t/a双甲氨合成联合装置设计

从工艺路线的比较、压力等级的选择、主要设备的选型等方面阐述了双甲氨合成联合装置的设计特点。结合生产运行实践,分析了双甲氨合成工艺路线的运行参数,与采用不同工艺的生产消耗和产品成本进行了对比。结果表明,该工艺吨氨节约成本80元,精醇成本为1112.6元/t,经济效益显著且生产运行稳定。     

油脂的含量对食品质量的影响及防止措施

通过对含油食品的酸价和过氧化值的实验测定说明油脂对食品质量的影响，并分析说明防止油脂食品氧化变质应采用的措施。     

Supply chain networks servicing upstream operations in oil and gas fields after the shale revolution

The recent irruption of shale resources in the oil and gas (O&G) industry has dramatically changed the paradigm for managing upstream operations. Unconventional production is largely driven by drilling new wells, yielding a much larger scale of material and service flows that need to be efficiently planned. This article presents an optimization framework for the design of integrated supply chain networks (SCNs) servicing upstream operations. Novel aspects addressed in this work are the integrated planning of material and service supplies; the economies of scale in operating, transportation and capital expenditures; the concept of waiting cost to quantify production losses; and the reverse flow of materials within closed-loop supply chains. The merits of the proposed approach are assessed through real-world case studies from the Argentine O&G industry. Optimal designs yield significant cost savings and confirm that the integrated planning of the SCN is critical for O&G operators after the shale revolution.     

Capital and total cost targets for mass exchange networks: Part 1: Simple capital cost models

This paper presents a method for targeting the capital and total cost of a mass exchange network. This part of the paper considers stagewise systems and uses a simplified capital cost correlation in order to convey the fundamentals. The method starts by determining the number of stages required, using the y−x composite curve plot presented previously, and then converts this to a capital cost. This target is combined with utility targets to give a target for the total annual cost. Simple design guidelines are presented, which allow these targets to be approached to within a few percent. The method is applied to a coke-oven gas sweetening example, which is a case involving two mass separating agents (MSAs) which do not overlap. It is also applied to an example involving phenol removal, in which there are overlapping MSAs. A final example deals with multicomponent transfer by extending the coke-oven gas problem. The paper introduces a new graphical tool, the y−y* composite curve plot, for handling systems with overlapping MSAs. The paper demonstrates that, contrary to previous belief, using the minimum number of units does not necessarily lead to a minimum cost design.     

Multistream heat exchangers: Equation‐oriented modeling and flowsheet optimization

Multistream heat exchangers (MHEXs), typically of the plate‐fin or spiral‐wound type, are a key enabler of heat integration in cryogenic processes. Equation‐oriented modeling of MHEXs for flowsheet optimization purposes is challenging, especially when streams undergo phase transformations. Boolean variables are typically used to capture the effect of phase changes, adding considerable difficulty to solving the flowsheet optimization problem. A novel optimization‐oriented MHEX modeling approach that uses a pseudo‐transient approach to rapidly compute stream temperatures without requiring Boolean variables is presented. The model also computes an approximate required heat exchange area to determine the optimal tradeoff between operating and capital expenses. Subsequently, this model is seamlessly integrated in a previously‐introduced pseudo‐transient process modeling and flowsheet optimization framework. Our developments are illustrated with two optimal design case studies, an MHEX representative of air separation operation and a natural gas liquefaction process. © 2015 American Institute of Chemical Engineers AIChE J, 61: 1856–1866, 2015     

Theoretical analysis of natural gas recovery from marginal wells with a deep well reactor

Current natural gas harvesting technologies are only economically viable at high gas flow rates. Subsequently, a significant quantity of gas remains unused in abandoned wells. Methanotrophic organisms are under development to capitalize on this resource given their preference for ambient conditions, however capital and methane mass transfer costs must be minimized. We propose using the well as the bioreactor negating capital costs, and leveraging the gas pressure for mass transfer. We evaluate the Deep Well Reactor's feasibility by developing mathematical models to simulate mass transfer and explore how operating parameters impact ethanol production. The results show sufficient mass transfer for 100% conversion, despite minimal complexity. Current aerobic methanotrophs and inorganic catalysts provide sufficient reaction rates. Conversely, anaerobic methanotrophs rates must be improved by a factor of 1200. With an appropriate catalyst, this technology allows the recovery of methane at flow rates an order of magnitude lower than current technologies. © 2017 American Institute of Chemical Engineers AIChE J, 63: 3642–3650, 2017     

等高压醇烷化改造运行总结

论述了利用原有φ800合成塔,将原料气净化系统由铜洗工艺改造为等高压醇烷化双甲工艺的实施过程.介绍了高压醇化和高压烷化的反应原理、工艺流程和主要设备;对比了改造前后的运行参数和工艺消耗指标;提出了进一步整改措施.结果表明,改造后吨氨成本由64.9元降低到14元,甲醇产能增加1t/d.     

Energy optimization of bioethanol production via gasification of switchgrass

In this article, we address the conceptual design of the bioethanol process from switchgrass via gasification. A superstructure is postulated for optimizing energy use that embeds direct or indirect gasification, followed by steam reforming or partial oxidation. Next, the gas composition is adjusted with membrane‐PSA or water gas shift. Membrane separation, absorption with ethanol‐amines and PSA are considered for the removal of sour gases. Finally, two synthetic paths are considered, high alcohols catalytic process with two possible distillation sequences, and syngas fermentation with distillation, corn grits, molecular sieves and pervaporation as alternative dehydration processes. The optimization of the superstructure is formulated as an mixed‐integer nonlinear programming problem using short‐cut models, and solved through a special decomposition scheme that is followed by heat integration. The optimal process consists of direct gasification followed by steam reforming, removal of the excess of hydrogen and catalytic synthesis, yielding a potential operating cost of $0.41/gal. © 2011 American Institute of Chemical Engineers AIChE J, 2011