Parametric Generation of Explosion Scenarios for Quantitative Risk Assessment of Gas Explosion in Offshore Plants
|
|
- Polly Logan
- 6 years ago
- Views:
Transcription
1 Parametric Generation of Explosion Scenarios for Quantitative Risk Assessment of Gas Explosion in Offshore Plants YeongAe Heo, a and Inwon Lee b a Department of Civil Engineering, Case Western Reserve University, Cleveland, OH, b Global Core Research Center for Ships and Offshore Plants (GCRC-SOP), Pusan National University, Busan, 46241, Korea; inwon@pusan.ac.kr (for correspondence) Published online 00 Month 2016 in Wiley Online Library (wileyonlinelibrary.com). DOI /prs In this study, probabilistic risk assessment has been carried out for the prediction of gas explosion loads due to hydrocarbon leaks and subsequent explosions in the topside of offshore platforms. In the initial phase of the risk assessment, the effect of various scenario parameters on the annual probability of gas explosion was quantified via a MATLAB code. For calculating the gas explosion frequency, the hydrocarbon leak frequencies and the ignition probabilities were derived from the HCR (HydroCarbon Release) database from the Health & Safety Executive (HSE, UK), and the IP (Ignition Probability) report from UKOOA (UK Offshore Operators Association), respectively. The MATLAB code has the algorithm to cope with the varying design practice in either Front End Engineering Design phase or detailed design phase. User-definable parameter setup and spreadsheet data input provide the user with the flexibility in selecting relevant level of elaboration for such design parameters as the leak size distribution, the hydrocarbon composition, etc. These features of the code enable controlling the number of explosion scenarios without any parameter range remaining unaccounted for. The present MATLAB code has been applied to generate hydrocarbon leak scenarios and corresponding explosion probability for the topside process modules of a specific oil Floating Production, Storage and Offloading. Varying the number of cases for each parameter leads to the variation of the number of explosion scenarios selected, which are either 48 or 24 in the particular case. For each explosion scenario, the gas leak and explosion simulation was carried out using the FLame Acceleration Simulator (FLACS) commercial S/W package, giving rise to the annual probability of exceedance for the explosion overpressure. Discussion of the influence of explosion scenario selection method on the change of the overpressure exceedance curves is made. VC 2016 American Institute of Chemical Engineers Process Saf Prog 000: , 2016 Keywords: Keywords: offshore plant; topside gas explosion; quantitative risk assessment; explosion frequency; exceedance curve This work was supported by Samsung Heavy Industry (SHI-GCRC joint research project); Korea government [MEST; through GCRC- SOP; National Research Foundation of Korea (NRF) grant] ( ). VC 2016 American Institute of Chemical Engineers INTRODUCTION The construction of offshore platforms such as oil rigs and Floating Production, Storage and Offloading (FPSOs) for deep sea exploitation of resources has been ever increasing due to prospective oil markets and the depletion of onshore and coastal oilfields. These offshore platforms, however, are vulnerable to vapor cloud explosion (VCE) which can lead to significant structural damages and casualties. The historical offshore accidents from Piper Alpha disaster in 1988 down to Deepwater Horizon BOP accident in 2010 showed us the severity of offshore explosion accidents. Therefore, the demand for detailed risk analysis for VCE for offshore projects has increased in order to adequately mitigate the risk. G undel et al. [1] developed a simple methodology to assess steel structural performance using hazard scenarios specified in FEMA 426 [2]. The FEMA 426 guidelines, however, are limited to the threat from bomb terrorist attacks whereas VCEs due to hydrocarbon leaks are the major hazards in offshore oil and gas industry. The intensity of VCEs is determined via the probabilistic assessment of diverse and random explosion scenario parameters. Intensive efforts have been sparked to develop probabilistic approaches to evaluate explosion loads due to VCE where large uncertainties are inherent since early 1990s through various joint industry projects (JIPs) sponsored by oil majors and the UK HSE (Health and Safety Executive) such as the Blast and Fire Engineering for Topside structures JIP [3] and the Gas Explosion Engineering JIP [4]. For explosion response, simple methodologies were widely adopted until 1990s such as TNT equivalent method [5], Baker Strehlow method [6], and Multi-Energy method [7]. Researchers [8 10] investigated blast waves generated by the simple methodologies using three-dimensional (3D) computational fluid dynamic (CFD) simulations. Demand for 3D CFD explosion analysis has been abruptly increased with the tremendous improvement of computer performance as well as growing attention to safety due to the regular occurrence of offshore accidents. Detailed procedures for the probabilistic prediction of gas explosion loads are described in informative manners in international guidelines and standards [[11 14]] based on 3D CFD explosion analyses. Process Safety Progress (Vol.00, No.00) Month
2 Figure 1. Leak frequency page of HCR database. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] It is critical to select an appropriate number of explosion scenarios for reliable Explosion Risk Assessment (ERA) results. More data produce better predictions in probabilistic approaches. Although informative procedures are described in the above mentioned guidelines and standards, no specific guidelines for the selection of explosion scenarios for VCE have been prepared yet. Hence, most engineers reduce the number of scenarios in practice due to computational cost and time according to their own assumptions without sufficient scientific evidence, which leads to biased ERA results. Also, a literature survey indicates that little attention has been paid to the generation of appropriate explosion scenarios. A robust explosion scenario generator can be an effective tool to evaluate ERA results for different sets of explosion scenarios. Such a numerical tool can also cope with frequent design changes at both Front End Engineering Design (FEED) phase and the detailed design phase in practice. In this study, a MATLAB code has been developed with a view to systematically generate explosion scenarios and the corresponding annual rate of occurrence for each explosion scenario. For the annual rate of occurrence for explosion scenarios, HCR Leak Database [15] was used to calculate the leak frequencies, and the UKOOA IP Model [16] was adopted for overall ignition probabilities considering the correlation between flammable gas cloud volume and operating conditions on offshore platforms. The code was applied to the ERA for a specific oil FPSO project where a process area is isolated from the accommodation area and utility area on the topside of the FPSO by two Fire and Blast walls. In this particular ERA study, five different sets of scenarios (hereinafter referred to as CASE) considering different leak conditions and wind conditions, consisting of scenarios each, and with the corresponding explosion probability for each scenario, were generated in order to show the effect of scenario selection on the result of the ERA study. The explosion overpressure for each scenario was then predicted by 3D CFD gas dispersion and explosion analysis using FLACS. The explosion overpressure exceedance curve can be generated by accumulating the annual probability of exceedance for each scenario in the order of the explosion pressure intensities. The significance of scenario selection in ERA for VCE is investigated by comparison of the explosion overpressure exceedance curves for five CASEs. CALCULATION OF GAS EXPLOSION FREQUENCY Overall Procedure The project to which the present code was applied to the topside of a specific oil FPSO, which consists of various modules in the weather deck and the process deck. The process modules have distinct functions such as turret, separation and stabilization, gas compression, dehydration, fuel gas production, flare and volatile organic compound recovery, produced water treatment, and water injection. Each module consists of a few isolatable sections which usually consist of various equipment items such as pipes, tanks, and pumps. Since each section is isolated from adjacent sections by shutdown valves, a section is considered as a basic unit of the leak frequency calculation. Owing to the random nature of various environmental parameters governing the release and dispersion of hydrocarbon, it is inevitable to use a probabilistic approach. Thus, the annual explosion frequency for the ith section is calculated as the joint probability of various variables as follows; fe i 5ki f i L H ðdþf LL i i ðx; Y ; ZÞfLD ðuþf WS i ðu Þf WD i ðuþ fil i i ðx; Y ; ZÞfIT ðsþ f I i ðmþ (1) Here, k i L is the annual gas leak frequency (times/year), which is a weighted sum of the annual gas leak frequency of each equipment comprising the section. fh i is the leak hole size (d) probability, fll i is the joint probability for the coordinates of leak location (X,Y,Z), fld i is the probability of leak direction (h), fws i and f WD i is the probability of wind speed (U) and direction (h), fil i and f IT i is the probability of ignition location (X,Y,Z) and time delay (s), and fi i is the ignition probability. The independent variables in Eq. (1) are random variables with probability distribution. In this study, the field data in the HydroCarbon Release (HCR) leak DB during 1992 through 2012 was used for k i L and f H i. The IP Look-up Correlation Model [16], which gives the ignition probability as a function of leak rate, was applied to fi i. Other random variables were assumed to have uniform distribution. Although the ignition location and the time delay s between gas leak and ignition could significantly affect the explosion, fil i and 2 Month 2016 Published on behalf of the AIChE DOI /prs Process Safety Progress (Vol.00, No.00)
3 Figure 2. Annual leak frequencies for equipment categories. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] fit i are treated as constants in this study. This is in order to focus on the leak and dispersion characteristics. Leak Frequency Based on the HCR Leak DB The HydroCarbon Release Database (hereinafter referred to as HCR DB) is a compilation of the leak accident data reported on North Sea offshore platforms since HCR DB, which is under the supervision of the Offshore Division of the HSE (Health and Safety Executive) of the British Government, is accessible through the internet ( hse.gov.uk/hcr3/). As shown in Figure 1, search criteria of leak data can be selected either by systems or equipment. For the selected criterion, the leak accidents are categorized into three; minor (leak rate under 0.1 kg/s), significant (leak rate kg/s), and major (leak rate over 1.0 kg/s) leak. Dividing the number of leaks by the total equipment years Process Safety Progress (Vol.00, No.00) Published on behalf of the AIChE DOI /prs Month
4 Figure 3. Calculated leak frequency for each isolated section. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] 4 Month 2016 Published on behalf of the AIChE DOI /prs Process Safety Progress (Vol.00, No.00)
5 Figure 4. Hole size distribution display of the HCR DB. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] (number of equipment items multiplied by the number of years) gives the annual leak frequency, which is times per year in the particular example in Figure 1. In this study, the equipment search criterion is selected as this allows to better represent the range of equipment items comprised in each section. Originally, HCR DB with equipment criteria is divided into total of 124 tertiary equipment categories, which is too detailed. Thus, the secondary equipment categories plus a few wildcard ones (84 in total) are employed in this study. Figure 2 exhibits the annual leak frequencies for 28 secondary categories out of 84 in total. Figure 3 illustrates how to calculate the leak frequency for each section consisting of several types of equipment. For instance, the LP Compression System (Section ID #7) consists of one centrifugal compressor, one cooler and ten flanges, and so on (note that the rows of Figure 3 only show the relevant categories). The composition of each section, column vector in green numbers in Figure 3, is a unique specification which will be treated as a file input to the calculation code. The leak frequencies for the equipment categories are given as a column vector written in black. Thus, the inner product between the section composition vector (green numbers) and the leak frequency vector (black numbers) gives the annual leak frequency of the corresponding section, written in red numbers. For example, the annual leak frequency of the LP Compression System (Section ID #7) is times per year. Leak Size Probability Based on the HCR Leak DB Leak hole size is one of the major parameters that determine the leak rate of hydrocarbon. The HCR DB compiles data on the hole size for all reported leaks. Clicking the Hole button in the leak frequency search window (Figure 1) displays the number of leaks in seven leak size ranges (<10 mm/10 25 mm/25 50 mm/50 75 mm/ mm/>5100 mm/n.a.) for the specific equipment category, as shown in Figure 4. The bottom row indicates the hole size distribution. Figure 5 exhibits the leak size distribution according to the 84 equipment categories used for a given leak frequency. Similarly as the leak frequency calculation, the leak size distribution for the section is calculated as the weighted average of the leak size distribution for each equipment category by the number of equipment of that section. The hole size distribution of the HCR DB can be considered as the probability of hole size defined for the seven discrete size ranges. From this, the discrete cumulative probability F(D) is defined as follows; FðDÞ5PðD d J Þ5 XJ i51 Pðd i D d i11 Þ5 XJ i P i (2) Here, D isthesamplevariablefortheholesize,d J is the upper limit of Jth size range in the HCR DB (e.g., d mm) and p i is the probability for the ith size range. For instance, p 2 (d mm) for the BOP Stacks-surface category is read as in Figure 5. Equation (2) implies that F(D) is the probability of the hole size being smaller than the upper limit of Jth size range. The diamonds connected by dotted line in Figure 6 show an example of such discrete probability, calculated for the Section ID #4, Test Separator. It is worthwhile to mention a couple of points; first, the seventh range (N.A.) probability is neglected because the hole sizes were not Process Safety Progress (Vol.00, No.00) Published on behalf of the AIChE DOI /prs Month
6 Figure 5. Hole size distribution for the equipment category. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] reported for these events. Second, the upper limit of the sixth range (>5 100 mm) is arbitrarily set as 150 mm. As such, the value of F(D) at the maximum hole size of 150 mm becomes 1, which means that hole size cannot exceed 150 mm. It is notable that the discrete cumulative probability in the above is defined in a similar manner as the Cumulative probability Distribution Function (CDF) for the continuous random variable. In this study, the CDF of hole size probability is obtained by curve fitting the discrete probability against a logarithmic function G(D) 5 alog(d) 1 b. The probability of hole size for an arbitrarily chosen size range (e.g., a D b) is simply given as G(b)-G(a). Compared with the fixed size ranges in HCR DB, this method provides the user higher case of flexibility in the risk assessment. Leak Rate and Ignition Probability The leak rate k (kg/s) is determined from the hole size and the material properties of the hydrocarbon inside the section. The following Det Norske Veritas-Centre or Marine and 6 Month 2016 Published on behalf of the AIChE DOI /prs Process Safety Progress (Vol.00, No.00)
7 Figure 6. Flow chart of Leak.m. Petroleum Technology (DNV-CMPT) formula was employed in this study; vffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffiffi g11 u g21 t g 2 k 5 C d AP O (3) ZR g T O g11 Here, C d is the discharge coefficient, usually taken as A is the area of the leak hole, c is the ratio of specific heats, c 5 C p /C v, Z is the compressibility factor, R O is the gas constant, and T O is absolute temperature. Except A which is determined by the hole size mentioned in the previous section, these parameters are determined by the average of the Process Safety Progress (Vol.00, No.00) Published on behalf of the AIChE DOI /prs Month
8 Figure 7. Algorithm for detailed design phase. Figure 8. Algorithm for FEED phase. Table 1. Some of explosion scenarios generated by Leak.m. Section ID Section Volume (m 3 ) Explosion Frequency (times/year) Leak Frequency (times/year) Hole Size (mm) Hole Prob. Leak Rate (kg/s) Ignition Prob properties of the gaseous hydrocarbon components inside the particular section considered. The ignition probability IP is calculated from the leak rate based on the look-up correlation of the UKOOA IP report as follows; log 10 IP5m log 10 k1c: (4) m and c are the empirical constants determined by the type of offshore platform and the leak rate. In this study, values corresponding to the Offshore FPSO liquid type are used. MATLAB CODE FOR THE CALCULATION OF GAS EXPLOSION FREQUENCY Input Data Based on the procedures described in the previous sections, a MATLAB code (Leak.m) has been developed to generate the gas explosion scenarios and to calculate the corresponding explosion frequencies. Emphasis has been given on the flexible application of the HCR DB to cope with various topside module arrangements and sections composition. Core input data is contained in the following spreadsheet files, which are input to the code. Input#1_Section_Info: consists of four sheets containing the following information. 1 Number of equipment items in each section 2 Volume of equipment items and length of pipes with different diameters in each section 3 Material properties of hydrocarbon in each section 4 Leak locations in each section Input#2_HCR_Leak_DB: annual leak frequency and hole size distribution for each equipment category Variation of Calculation Algorithm According to Design Phase The flow chart of the present MATLAB code is presented in Figure 6. The leak frequency and hole size probability 8 Month 2016 Published on behalf of the AIChE DOI /prs Process Safety Progress (Vol.00, No.00)
9 calculations are performed according to the procedures described earlier. The most distinct feature of this code is the ability to switch the procedure according to the design phase, that is, either the FEED phase or detailed design phase. The procedure described in the previous section is used to calculate the hole size probability and the corresponding leak rate based on the user-specified hole size and position, as shown in Figure 7. In the detailed design phase, such specification is possible because the detailed information regarding the modules and sections is available. On the contrary, the hole size and position can hardly be specified in the conceptual design FEED phases, in which the section and module information is unknown. For these initial design phases, the algorithm is switched to specify the leak rate first and then calculate the corresponding hole size, as shown in Figure 8. This switching algorithm helps to enhance the applicability of the developed code in various design environments. Results of Code Execution Consider an example for detailed design phase due to hydrocarbon gas release as follows: 1. three hole sizes of 5, 15, and 135 mm 2. three leak positions 3. two leak directions of 08 and 458 Figure 9. Histogram of explosion scenarios in Table 1. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] 4. three wind speeds m/s with a 0.1 probability 2.0 m/s with a 0.25 probability 2.5 m/s with a 0.2 probability of occurrence 5. two wind directions 458 with a 0.2 probability of occurrence, respectively 1358 with a 0.3 probability of occurrence, respectively This example leads to 108 explosion scenarios for each section and 1,728 scenarios for the topside modules comprising 16 sections zone of which is listed in Table 1. Each row in Table 1 corresponds to a single explosion scenario. It is seen that the explosion frequency for the first scenario is (times/year), implying that this event occurs about every 20 million years. As can be found in Eq. (1), the explosion frequency is the product of the leak frequency, the ignition probability, the hole size probability, and the probabilities of various environmental parameters for gas dispersion. Uniform distributions are assumed for such gas dispersion parameters in this study. As more number of cases for each parameter are considered, the number of scenarios increases. In this example, 108 scenarios were selected in total for each section. The density distribution of the explosion frequency for all of the selected scenarios is reported in the histogram shown in Figure 9. Here, the horizontal axis is given as the logarithm of the explosion frequency, so 25 indicates an explosion frequency of times/year. The explosion scenarios should be carefully selected so that the explosion response for each scenario can be appropriately distributed to avoid a biased expectation on explosion probabilities. Although it is beyond the scope of this study, it was observed that engineers select very coarse scenarios to save computational time and cost in practice, which generally yields an unreasonably conservative design blast load. The automatic scenario generation capability of the proposed MATLAB code will leverage efficient assessment for explosion scenario selection. RESULTS OF FLACS EXPLOSION SIMULATION Forty-eight explosion scenarios were selected for the FLACS gas dispersion and explosion CFD analysis. The reduction of the number of scenarios was carried out by selecting relevant isolated sections regarding gas leaks and reducing the number of cases for some parameters. For each explosion scenario, a FLACS simulation was then carried out for the six modules of the process deck of the oil FPSO used in this study. As shown in Figure 10, the leaks were assumed to occur within Modules 3 and 4 with two hole sizes (75 and 150 mm) selected. Three wind speeds (2.5, 7.5, and 12 m/s) and two wind directions (08 and 158) were applied. Table 2 Figure 10. Process area and scenario variables for CFD analysis. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] Process Safety Progress (Vol.00, No.00) Published on behalf of the AIChE DOI /prs Month
10 Table 2. Gas properties and composition. Item Module 3 Module 4 Inventory volume (m 3 ) Temperature (8C) Pressure (bar) Mass density (kg/m 3 ) Methane Ethane Propane i-butane n-butane i-pentane n-pentane C C Figure 11. Explosion exceedance curves. [Color figure can be viewed in the online issue, which is available at wileyonlinelibrary.com.] shows the properties and composition of the gaseous hydrocarbons for each leak. The FLACS simulation of each scenario gives the explosion overpressure and plotting the annual explosion frequency against the explosion overpressure gives the explosion overpressure exceedance curve. The exceedance curve obtained for the baseline 48 scenarios (CASE1) is plotted as the black curve in Figure 11. Dimensioning Accidental Load (DAL) is determined by intersecting a particular annual probability level called Allowable Annual Rate of Occurrence or Return Period for explosion and the explosion overpressure exceedance curve. According to international rules and regulations, or returning every 10 to 20,000 years is commonly used depending on the standards of each project. In this study, per year was selected as the allowable limit. To investigate of the effect of scenario selection method on the explosion overpressure exceedance curve, the scenario selection method was varied from the baseline 48 scenarios (CASE 1). For CASE2 through CASE5, 24 scenarios were randomly selected from the baseline scenarios as summarized in Table 3. Whereas one of two leaks was considered in CASE2 and CASE3, CASE4 and CASE5 considered only one leak size, either 75 or 150 mm. These CASEs can be compared in order to exhibit how the explosion scenario selection affects the probabilistic hazard analysis to estimate explosion DAL with respect to CASE1 as point of comparison. A closer inspection of Figure 11 and Table 4 indicates that CASE2 leads to a lower DAL than CASE3. While CASE3 and CASE4 exhibit conservative results (71% and 44% higher than the reference DAL), CASE5 exhibits about 20% lower DAL than the reference value, which will result in underdesign. On the other hand, the estimation of CASE2 is very close to CASE1. Although it requires more comprehensive studies with a bigger number of scenarios and more random scenario sets to appropriately categorize the types of scenario selection that will cause overestimation or underestimation, it is obvious that the scenario selection plays a critical role in blast load estimation and design. CONCLUSIONS In order to investigate the importance of scenario selection in ERA of VCE, first a reference scenario set which contains 48 explosion scenarios was carefully selected so that the explosion pressure responses can be appropriately distributed to avoid biased estimation of explosion probabilities. Twenty-four explosion scenarios were then randomly selected from the reference scenario set in four different ways for a comparative study. The gas dispersion and explosion simulations were carried out using FLACS commercial S/ W package to compute pressure responses for each explosion scenario. An explosion scenario generator was developed using MATLAB for explosion probability computation and scenario selection evaluation purposes. Explosion probability computation is based on the Metocean data for the offshore site, the HCR database from the UK HSE (Health & Safety Executive, UK) and the IP (Ignition Probability) report from UKOOA (UK Offshore Operators Association). Given input parameters accounting for wind, leak, and ignition conditions for an offshore oil and gas production unit, the proposed explosion scenario generator can efficiently generate explosion scenarios and compute explosion probabilities for the generated scenarios. This program can also generate explosion pressure exceedance curves providing CFD Table 3. Five different cases for scenario selection. CASE1 CASE2 CASE3 CASE4 CASE5 No. leak locations 2 1 (Module 3) 1 (Module 4) 2 2 No. leak sizes (150 mm) 1 (75 mm) No. leak directions No. wind directions No. wind speeds No. of scenarios Month 2016 Published on behalf of the AIChE DOI /prs Process Safety Progress (Vol.00, No.00)
11 Table 4. Design explosion load from different CASES. Design explosion load (bar) CASE1 CASE2 CASE3 CASE4 CASE analysis results for each scenario. Hence, the automatic process capability of the proposed program facilitates the comparative study to highlight the importance of scenario selection in ERA. The exceedance curves for four different scenario sets exhibit large variations in DAL estimation, which indicates that current probabilistic risk assessment is prone to either overdesign or underdesign depending on assumptions adopted in explosion scenario selection. It is clear that more sophisticated guidelines on explosion scenario selection in ERA are necessary for more reliable and robust design load estimation. Due to limitations in the time and resources of this study, the effect of ignition could not be included in discussion. Also, a quite limited number of cases for each scenario parameter and scenario set were used in this preliminary study. The fundamental findings of this study will be enhanced by more comprehensive investigations in future studies ACKNOWLEDGMENT The CFD analyses for explosion pressure responses used in this article were conducted by GexCon AS, Bergen, Norway. LITERATURE CITED 1. M. G undel, B. Hoffmeister, M. Feldmann, and B. Hauke, Design of high rise steel buildings against terrorist attacks, Comput Aided Civ Infrastruct Eng 27 (2012), FEMA. Reference Manual to Mitigate Potential Terrorists Attacks Against Buildings, Risk Management Series, FEMA-Report 426, Federal Emergency Management Agency (FEMA), Washington DC, C.A. Selby and B.A. Burgan, Blast and Fire Engineering for Topsides Structures Phase 2, Final Summary Report, SCI-P-253, The Steel Construction Institute, Ascot, UK, 1998, ISBN J. Czujko, Design of Offshore Facilities to Resist Gas Explosion Hazard, Engineering Handbook, CorrOcean, Sandvika, Norway, M.J. Steindler and W.B. Seefeldt, A method for estimating the challenge to an air-cleaning system resulting from an accidental explosive event, The 16th Department of Energy Conference on Nuclear Air Cleaning, Washington, DC and Boston, MA, R.A. Strehlow, R.T. Luckritz, A.A. Adamczyk, and S.A. Shimpi, The blast wave generated by spherical flames, Combust Flame 35 (1979), A.C. van den BERG, The Multi-Energy Method A Framework for Vapour Cloud Explosion Blast Prediction, J Hazard Mater 12 (1985), M.J. Tang and Q.A. Baker, A new set of blast curves from vapor cloud explosion, Process Saf Prog 18 (1999), A. Beccantini, A. Malczynski, and E. Studer, Comparison of TNT-equivalence approach, TNO multi-energy approach and a CFD approach in investigating hemispheric hydrogen-air vapor cloud explosions, Proceedings of the 5th International Seminar on Fire and Explosion Hazards, Edinburgh, UK, April 23 27, A. Sari, Comparison of TNO Multienergy and Baker Strehlow Tang Models, AIChE Process Saf Prog 30 (2011), ISO 17776:2000, Petroleum and Natural Gas Industries Offshore Production Installations Guidelines on Tools and Techniques for Hazard Identification and Risk Assessment, International Organization for Standardization, HSE, PM/Technical/12 - Fire, Explosion and Risk Assessment Topic Guidance, Health and Safety Executives, London, UK, UKOOA, Fire and Explosion Guidance, Part 0: Fire and Explosion Hazard Management, UK Offshore Operators Association Limited, London, UK, Norsok, Norsok Standard Z-013, Risk and Emergency Preparedness Assessment, 3rd Edition, Standards Norway, Lysaker, Norway, HCR Leak Database, Hydrocarbon Releases System, Offshore Division of Health and Safety Executive, , Available at UKOOA IP Model, Ignition Probability Review, Model Development and Look-Up Correlations, EI Research Report, Energy Institute, London, 2006, ISBN Process Safety Progress (Vol.00, No.00) Published on behalf of the AIChE DOI /prs Month
Determination of the Design Load for Structural Safety Assessment against Gas Explosion in Offshore Topside
Determination of the Design Load for Structural Safety Assessment against Gas Explosion in Offshore Topside Migyeong Kim a, Gyusung Kim a, *, Jongjin Jung a and Wooseung Sim a a Advanced Technology Institute,
More informationImproving Accuracy of Frequency Estimation of Major Vapor Cloud Explosions for Evaluating Control Room Location through Quantitative Risk Assessment
Improving Accuracy of Frequency Estimation of Major Vapor Cloud Explosions for Evaluating Control Room Location through Quantitative Risk Assessment Naser Badri 1, Farshad Nourai 2 and Davod Rashtchian
More informationUSE OF THE EXCEEDANCE CURVE APPROACH IN OCCUPIED BUILDING RISK ASSESSMENT
USE OF THE EXCEEDANCE CURVE APPROACH IN OCCUPIED BUILDING RISK ASSESSMENT Kieran J Glynn, Advisor Major Accident Risk, BP, UK The exceedance curve approach was developed following the issue of the 2003
More informationPRAGMATIC ASSESSMENT OF EXPLOSION RISKS TO THE CONTROL ROOM BUILDING OF A VINYL CHLORIDE PLANT
PRAGMATIC ASSESSMENT OF EXPLOSION RISKS TO THE CONTROL ROOM BUILDING OF A VINYL CHLORIDE PLANT L.P. Sluijs 1, B.J. Haitsma 1 and P. Beaufort 2 1 Vectra Group Ltd. 2 Shin-Etsu (contact details: Vectra Group
More informationREQUIREMENTS FOR VALIDATION OF MATHEMATICAL MODELS IN SAFETY CASES
REQUIREMENTS FOR VALIDATION OF MATHEMATICAL MODELS IN SAFETY CASES R F Evans Principal Specialist Inspector, Health & Safety Executive Offshore Safety Division, Bootle Merseyside. The Offshore Installations
More informationDIGITAL SOLUTIONS TRAINING CATALOGUE. QRA and CFD simulation. Phast, Safeti and KFX SAFER, SMARTER, GREENER
DIGITAL SOLUTIONS TRAINING CATALOGUE QRA and CFD simulation Phast, Safeti and KFX SAFER, SMARTER, GREENER 02 PHAST, SAFETI AND KFX Training catalogue Global training Our increased focus on global training,
More informationCFD Based Approach for VCE Risk Assessment
CFD Based Approach for VCE Risk Assessment 2009 MKOPSC International Symposium Anna Qiao, Steven Zhang, Asmund Huser DNV Energy Objective Determine the maximum design load at a specified frequency Provide
More informationComparison of Large-Scale Vented Deflagration Tests to CFD Simulations for Partially Congested Enclosures
Comparison of Large-Scale Vented Deflagration Tests to CFD Simulations for Partially Congested Enclosures Peter A. Diakow, Project II Consultant, Baker Engineering and Risk Consultants, Inc. J. Kelly Thomas,
More informationPrediction of gas explosion overpressure interacting with structures for blast-resistant design
Prediction of gas explosion overpressure interacting with structures for blast-resistant design Suhyun Ree 1) and *Thomas Kang 2) 1), 2) Department of Architecture & Architectural Engineering, Seoul National
More informationTitle of Paper Interpretation of IP15 in Process Plant Design: a Commonsense Approach ---------------------------------------------------------------------------------------------------------------------------
More informationBlast Damage Consideratons for Horizontal Pressure Vessel and Potential for Domino Effects
A publication of CHEMICAL ENGINEERING TRANSACTIONS VOL. 26, 2012 Guest Editors: Valerio Cozzani, Eddy De Rademaeker Copyright 2012, AIDIC Servizi S.r.l., ISBN 978-88-95608-17-4; ISSN 1974-9791 The Italian
More informationConsequences on port facilities of a tanker explosion
Structures Under Shock and Impact IX 279 Consequences on port facilities of a tanker explosion P. L. Metropolo 1 & A. E. P. Brown 2 1 Rhodia, Technology Research Centre, Brazil 2 Polytechnic College, University
More informationDevelopment of Accidental Collapse Limit State Criteria for Offshore Structures
Risk Acceptance and Risk Communication Stanford, March 26-27, 2007 Development of Accidental Collapse Limit State Criteria for Offshore Structures by Torgeir Moan Norwegian University of Science and Technology
More informationCHEMICAL ENGINEERING TRANSACTIONS
55 A publication of CHEMICAL ENGINEERING TRANSACTIONS VOL. 48, 2016 Guest Editors: Eddy de Rademaeker, Peter Schmelzer Copyright 2016, AIDIC Servizi S.r.l., ISBN 978-88-95608-39-6; ISSN 2283-9216 The Italian
More informationPart 2.5 Dispersion Modeling Using ALOHA
Part 2.5 Dispersion Modeling Using ALOHA Dr. Arshad Ahmad Email: arshad@utm.my 1 Software Commonly used for Risk Analysis Software SAFETI SFU CAFTAN ETRA HAZSEC. HAZTRAC. PHAST. WHAZAN EFFECTS. DAMAGE
More informationA Generic Model To Assess Major Incident Frequencies For Offshore Assets
A Generic Model To Assess Major Incident Frequencies For Offshore Assets Richard Emery, MMI Engineering Ltd, The Brew House, Wilderspool Park, Greenall s Avenue, Warrington, WA4 6HL. Quantitative risk
More informationAnalysis and Comparison of Calculation Methods for Physical Explosions of Compressed Gases
133 A publication of VOL. 32, 13 CHEMICAL ENGINEERING TRANSACTIONS Chief Editors: Sauro Pierucci, Jiří J. Klemeš Copyright 13, AIDIC Servizi S.r.l., ISBN 978-88-9568-23-5; ISSN 1974-9791 The Italian Association
More informationTHE SIGNIFICANCE OF HAZARD ENDPOINTS IN QUANTITATIVE RISK ANALYSIS
THE SIGNIFICANCE OF HAZARD ENDPOINTS IN QUANTITATIVE RISK ANALYSIS John B. Cornwell and Jeffrey D. Marx Presented At 6 Process Plant Safety Symposium Houston, Texas April -2, 6 Presented By Quest Consultants
More informationEngineering Models for Vented Lean Hydrogen Deflagrations
Engineering Models for Vented Lean Hydrogen Deflagrations Anubhav Sinha, Vendra Chandra and Jennifer X. Wen Warwick FIRE, School of Engineering University of Warwick, UK Outline Introduction Review of
More informationImprovement in Release Frequencies for Quantitative Risk Assessment
Improvement in Release Frequencies for Quantitative Risk Assessment Andrew Crerand, Simon Chynoweth and Steve Richardson, Shell Research Ltd, Shell Technology Centre Thornton, P.O. Box 1, Chester, CH1
More informationSteam generator tube rupture analysis using dynamic simulation
Steam generator tube rupture analysis using dynamic simulation Heat Exchangers are used to transfer heat from a hot fluid to a cold fluid. Most of the times these fluids are available at different pressures
More informationLoss of Normal Feedwater Analysis by RELAP5/MOD3.3 in Support to Human Reliability Analysis
Loss of Normal Feedwater Analysis by RELAP5/MOD3.3 in Support to Human Reliability Analysis ABSTRACT Andrej Prošek, Borut Mavko Jožef Stefan Institute Jamova cesta 39, SI-1 Ljubljana, Slovenia Andrej.Prosek@ijs.si,
More informationINHERENTLY SAFER DESIGN CASE STUDY OF RAPID BLOW DOWN ON OFFSHORE PLATFORM
INHERENTLY SAFER DESIGN CASE STUDY OF RAPID BLOW DOWN ON OFFSHORE PLATFORM Volton Edwards bptt Angus Lyon DNV Energy Alastair Bird DNV Energy INTRODUCTION A term now in common usage within the oil & gas
More informationA NEW PROCESS FOR IMPROVED LIQUEFACTION EFFICIENCY
WHITE PAPER A NEW PROCESS FOR IMPROVED LIQUEFACTION EFFICIENCY Author(s): Adam Jones and Grant Johnson, Costain Natural Resources First published: GPAE, September 2014 www.costain.com A New Process for
More informationDesign Accidental Load for Explosion Resistant Design
INTERNATIONAL JOURNAL OF COASTAL & OFFSHORE ENGINEERING IJCOE Vol.1/No. 3/ Autumn 2017 (41-49) Available online at: http://ijcoe.org/browse.php?a_code=a-10-121-2&sid=1&slc_lang=en Design Accidental Load
More informationVapor Cloud Explosion Analysis of Onshore Petrochemical Facilities
American Society of Safety Engineers Middle East Chapter 7 th Professional Development Conference & Exhibition Kingdom of Bahrain, March 18-22, 2006 ASSE-MEC-0306-38 Vapor Cloud Explosion Analysis of Onshore
More informationIgnition modelling Are our approaches aligned?
Ignition modelling Are our approaches aligned? Lars Rogstadkjernet Gexcon Outline Experience from 3 rd party reviews Areas of diverging approach Dispersion and ignition modelling 3 rd party reviews 3 rd
More informationThe Comparison of CFD with a Traditional Method Used in an Incident Investigation Case Happened in Taiwan
2005 Asia-Pacific Conference on Risk Management and Safety The Comparison of CFD with a Traditional Method Used in an Incident Investigation Case Happened in Taiwan Yet-Pole I* and Te-Lung Cheng Department
More informationModule 03 Accident modeling, risk assessment and management Lecture 04 Explosions
Health, Safety and Environmental Management in Offshore and Petroleum Engineering Prof. Srinivasan Chandrasekaran Department of Ocean Engineering Indian Institute of Technology, Madras Module 03 Accident
More informationEffects of directionality on wind load and response predictions
Effects of directionality on wind load and response predictions Seifu A. Bekele 1), John D. Holmes 2) 1) Global Wind Technology Services, 205B, 434 St Kilda Road, Melbourne, Victoria 3004, Australia, seifu@gwts.com.au
More informationRisk Analysis using Corrosion Rate Parameter on Gas Transmission Pipeline
IOP Conference Series: Materials Science and Engineering PAPER OPEN ACCESS Risk Analysis using Corrosion Rate Parameter on Gas Transmission Pipeline To cite this article: B Sasikirono et al 2017 IOP Conf.
More informationLEAK FREQUENCY MODELLING FOR OFFSHORE QRA BASED ON THE HYDROCARBON RELEASE DATABASE
LEAK FREQUENCY MODELLING FOR OFFSHORE QRA BASED ON THE HYDROCARBON RELEASE DATABASE Andreas Falck 1, Brian Bain 2 and Laila K. Rødsætre 3 1 DNV Energy, Norway 2 DNV Energy, UK 3 StatoilHydro ASA, Norway
More informationTurn Lane Warrants: Concepts, Standards, Application in Review
Turn Lane Warrants: Concepts, Standards, Application in Review David J. DeBaie P.E., P.T.O.E. 2004 ITE, District 1 Annual Meeting Burlington, Vermont Introduction Turning lanes at intersections reduce
More information44 (0) E:
FluidFlow Relief Valve Sizing Handbook Flite Software 2016 Flite Software N.I. Ltd, Block E, Balliniska Business Park, Springtown Rd, Derry, BT48 0LY, N. Ireland. T: 44 (0) 2871 279227 E: sales@fluidflowinfo.com
More informationGas Gathering System Modeling The Pipeline Pressure Loss Match
PETROLEUM SOCIETY CANADIAN INSTITUTE OF MINING, METALLURGY & PETROLEUM PAPER 2005-230 Gas Gathering System Modeling The Pipeline Pressure Loss Match R.G. MCNEIL, P.ENG. Fekete Associates Inc. D.R. LILLICO,
More informationIdentification and Screening of Scenarios for LOPA. Ken First Dow Chemical Company Midland, MI
Identification and Screening of Scenarios for LOPA Ken First Dow Chemical Company Midland, MI 1 Layers of Protection Analysis (LOPA) LOPA is a semi-quantitative tool for analyzing and assessing risk. The
More informationSafe Work Practices and Permit-to-Work System
CHAPTER 24 Safe Work Practices and Permit-to-Work System 24.1 INTRODUCTION OSHA s Process Safety Management (PSM) Standard (OSHA, 1992) requires employers to develop and implement safe work practices (SWPs)
More informationInternal Explosion Methodologies
2006 Baker Engineering and Risk Consultants, Inc. Internal Explosion Methodologies Presented October 18, 2006 A.J. Pierorazio, P.Eng. J.K. Thomas, Ph.D. M. Kolbe M.L. Goodrich BAKER ENGINEERING ANDRISKCONSULTANTS
More informationPOWER Quantifying Correction Curve Uncertainty Through Empirical Methods
Proceedings of the ASME 2014 Power Conference POWER2014 July 28-31, 2014, Baltimore, Maryland, USA POWER2014-32187 Quantifying Correction Curve Uncertainty Through Empirical Methods ABSTRACT Christopher
More informationMODELLING OF FUME EXTRACTORS C. R.
LD8 19th International Symposium of Ballistics, 7 11 May 21, Interlaken, Switzerland MODELLING OF FUME EXTRACTORS C. R. Woodley WS4 Guns and Warheads Department, Defence Evaluation and Research Agency,
More informationNitrogen subtraction on reported CO 2 emission using ultrasonic flare gas meter
Nitrogen subtraction on reported CO 2 emission using ultrasonic flare gas meter Kjell-Eivind Frøysa, Christian Michelsen Research AS, Bergen, Norway Henning Ekerhovd, StatoilHydro ASA, Kollsnes, Norway
More informationJournal of Applied and Industrial Sciences, 2014, 2 (4): , ISSN: (PRINT), ISSN: (ONLINE)
Research Article 181 Research Article Estimation of Blast over Pressures of Possible Explosion in a Furnace in Khartoum Refinery by Using MATLAB Software Mohamed Almustafa *1, M. H. M. Abuuznien 2 and
More informationAmerican Chemical Society (ACS) 246th ACS National Meeting Indianapolis, Indiana September 9, 2013
American Chemical Society (ACS) 246th ACS National Meeting Indianapolis, Indiana September 9, 2013 J. Kelly Thomas, Ph.D. Baker Engineering and Risk Consultants San Antonio, TX (KThomas@BakerRisk.com)
More informationQUANTIFYING THE TOLERABILITY OF POTENTIAL IGNITION SOURCES FROM UNCERTIFIED MECHANICAL EQUIPMENT INSTALLED IN HAZARDOUS AREAS
QUANTIFYING THE TOLERABILITY OF POTENTIAL IGNITION SOURCES FROM UNCERTIFIED MECHANICAL EQUIPMENT INSTALLED IN HAZARDOUS AREAS Steve Sherwen Senior Consultant, ABB Engineering Services, Daresbury Park,
More informationMODELLING OF POOL FIRE AND INJURY PREDICTION CONSIDERING DIFFERENT WIND SPEEDS AND DIRECTIONS IN OFFSHORE PLATFORM
MODELLING OF POOL FIRE AND INJURY PREDICTION CONSIDERING DIFFERENT WIND SPEEDS AND DIRECTIONS IN OFFSHORE PLATFORM Usama Muhammad Niazi 1, Mohammad Shakir Nasif 1, Masdi bin Muhammad 1 and Muhammad Imran
More information1 PIPESYS Application
PIPESYS Application 1-1 1 PIPESYS Application 1.1 Gas Condensate Gathering System In this PIPESYS Application, the performance of a small gascondensate gathering system is modelled. Figure 1.1 shows the
More informationPaper 2.2. Operation of Ultrasonic Flow Meters at Conditions Different Than Their Calibration
Paper 2.2 Operation of Ultrasonic Flow Meters at Conditions Different Than Their Calibration Mr William Freund, Daniel Measurement and Control Mr Klaus Zanker, Daniel Measurement and Control Mr Dale Goodson,
More informationStudy on Intensity of Blast Wave Generated from Vessel Bursting by Gas Explosion
5 th ICDERS August 7, 15 Leeds, UK Study on Intensity of Blast Wave Generated from Vessel Bursting by Gas Explosion Matsunaga, T., Mogi, T., Dobashi, R. Graduated School of Engineering, The University
More informationAssessing Combinations of Hazards in a Probabilistic Safety Analysis
Assessing Combinations of Hazards in a Probabilistic Safety Analysis Halbert Taekema a, and Hans Brinkman a a NRG, Arnhem, The Netherlands Abstract: Guidance on how to systematically address combination
More informationI. CHEM. E. SYMPOSIUM SERIES NO. 85
FIRE SURVIVAL OF PROCESS VESSELS CONTAINING GAS J. Nylund * The present work is a theoretical evaluation of the ability of process vessels to survive hydrocarbon fires when the vessels are designed and
More informationWorkshop 302-compressor-anti-surge
Workshop Objectives Workshop 302-compressor-anti-surge Illustrate how to create a simple anti-surge control on a compressor Workshop Description Flowsheeet: A feed stream at 1 bar with methane, ethane
More informationHYDROGEN RISK ANALYSIS FOR A GENERIC NUCLEAR CONTAINMENT VENTILATION SYSTEM
HYDROGEN RISK ANALYSIS FOR A GENERIC NUCLEAR CONTAINMENT VENTILATION SYSTEM u, Z. 1 and Jordan, T. 2 Karlsruhe Institute of Technology, P.O. Box 3640, 76021 Karlsruhe, Germany 1 zhanjie.xu@kit.edu, 2 thomas.jordan@kit.edu
More informationInternational Journal of Petroleum and Geoscience Engineering Volume 03, Issue 02, Pages , 2015
International Journal of Petroleum and Geoscience Engineering Volume 03, Issue 02, Pages 116- ISSN: 2289-4713 Improving Reservoir Recovery Factor Using Enhanced Electrical Submersible Pump Design; a Case
More informationReview of Source Term Modelling for Hydrocarbon Releases using Process Dynamic Simulation
Review of Source Term Modelling for Hydrocarbon Releases using Process Dynamic Simulation Conor Crowley and Mrudhul Raj, Atkins Limited, Kirkgate House, Upperkirkgate, Aberdeen AB10 1HW Andrew Ross, Chemical
More informationFire and Safety for Offshore drilling and production Ajey Walavalkar ANSYS Inc.
Fire and Safety for Offshore drilling and production Ajey Walavalkar ANSYS Inc. 1 ANSYS, Inc. September 12, Fire and safety related applications Gas Dispersion and Ventilation Formation of combustible
More informationE. Agu, M. Kasperski Ruhr-University Bochum Department of Civil and Environmental Engineering Sciences
EACWE 5 Florence, Italy 19 th 23 rd July 29 Flying Sphere image Museo Ideale L. Da Vinci Chasing gust fronts - wind measurements at the airport Munich, Germany E. Agu, M. Kasperski Ruhr-University Bochum
More informationTube rupture in a natural gas heater
Tube rupture in a natural gas heater Dynamic simulation supports the use of a pressure safety valve over a rupture disk in the event of a tube rupture HARRY Z HA and PATRICK STANG Fluor Canada Ltd A fast
More informationRisks Associated with Caissons on Ageing Offshore Facilities
Risks Associated with Caissons on Ageing Offshore Facilities D. Michael Johnson, DNV GL, Peter Joyce, BG Group, Sumeet Pabby, BG Group, Innes Lawtie, BG Group. Neil Arthur, BG Group, Paul Murray, DNV GL.
More informationANNEX AMENDMENTS TO THE INTERNATIONAL CODE FOR FIRE SAFETY SYSTEMS (FSS CODE) CHAPTER 15 INERT GAS SYSTEMS
Annex 3, page 2 ANNEX AMENDMENTS TO THE INTERNATIONAL CODE FOR FIRE SAFETY SYSTEMS (FSS CODE) CHAPTER 15 INERT GAS SYSTEMS The text of existing chapter 15 is replaced by the following: "1 Application This
More informationSLOP RECEPTION AND PROCESSING FACILITIES
RULES FOR CLASSIFICATION OF SHIPS NEWBUILDINGS SPECIAL SERVICE AND TYPE ADDITIONAL CLASS PART 5 CHAPTER 8 SLOP RECEPTION AND PROCESSING FACILITIES JANUARY 2011 CONTENTS PAGE Sec. 1 General Requirements...
More informationSimulation and modelling of water spray in the 3D explosion simulation program FLACS. Elin Kristin Dale
Simulation and modelling of water spray in the 3D explosion simulation program FLACS Elin Kristin Dale The University of Bergen 2004 1. Foreword...1 2. Summary...2 3. Introduction...4 3.1 Theme...4 3.2
More informationThe report gives a summary of the background and motivation for the audit activity and summarizes the observations made at the meetings.
Audit Report AUDIT REPORT (UNOFFICIAL TRANSLATION) AUDIT OF USE OF ANNULAR SAFETY VALVES IN GAS LIFT COMPLETIONS SUMMARY During the period from June 2003 to September 2004, the Petroleum Safety Authority
More informationOptimization of Separator Train in Oil Industry
Optimization of Separator Train in Oil Industry Pawan jain a M.E. Petroleum Engineering, Maharashtra Institute of Technology, Pune-411038 ---------------------------------------------------------------------***---------------------------------------------------------------------
More informationGerald D. Anderson. Education Technical Specialist
Gerald D. Anderson Education Technical Specialist The factors which influence selection of equipment for a liquid level control loop interact significantly. Analyses of these factors and their interactions
More informationModule No. # 03 Lecture No. # 01 Dose assessment, Safety regulations
Health, Safety and Environmental Management in Petroleum and offshore Engineering Prof. Dr. Srinivasan Chandrasekaran Department of Ocean Engineering Indian Institute of Technology, Madras Module No. #
More informationSAFETI OFFSHORE. Modelling of the progression of an offshore hydrocarbon release accident WHITEPAPER. Authors:
WHITEPAPER SAFETI OFFSHORE Modelling of the progression of an offshore hydrocarbon release accident Authors: Brian Bain, DNV GL, Aberdeen. E-mail : brian.bain@dnvgl.com David Worthington, DNV GL, London.
More informationNumerical Simulations of a Train of Air Bubbles Rising Through Stagnant Water
Numerical Simulations of a Train of Air Bubbles Rising Through Stagnant Water Hong Xu, Chokri Guetari ANSYS INC. Abstract Transient numerical simulations of the rise of a train of gas bubbles in a liquid
More informationOIL AND GAS INDUSTRY
This case study discusses the sizing of a coalescer filter and demonstrates its fouling life cycle analysis using a Flownex model which implements two new pressure loss components: - A rated pressure loss
More informationLab # 03: Visualization of Shock Waves by using Schlieren Technique
AerE545 Lab # 03: Visualization of Shock Waves by using Schlieren Technique Objectives: 1. To get hands-on experiences about Schlieren technique for flow visualization. 2. To learn how to do the optics
More informationA quantitative risk analysis method for the natural gas pipeline network
PI-195 A quantitative risk analysis method for the natural gas pipeline network Y.-D. Jo1, K.-S. Park1, H.-S. Kim1, J.-J. Kim1, J.-Y. Kim2 & J. W. Ko3 1 Institute of Gas Safety Technology, Korea Gas Safety
More informationThe Science of Quantitative Risk Assessment for Explosives Safety
The Science of Quantitative Risk Assessment for Explosives Safety By John Tatom (Manager, Explosives Safety Group, A-P-T Research, Inc. Quantitative risk assessment (QRA) tools, as described in the QRA
More informationBenefits of Detailed CFD Ventilation Analysis During Early Design Phases. Josué Quilliou Gexcon Consulting
Benefits of Detailed CFD Ventilation Analysis During Early Design Phases Josué Quilliou Gexcon Consulting 12 95 NORSOK S-001: Natural ventilation in hazardous areas shall be as good as possible and shall
More informationMETHOD 25A - DETERMINATION OF TOTAL GASEOUS ORGANIC CONCENTRATION USING A FLAME IONIZATION ANALYZER
1250 METHOD 25A - DETERMINATION OF TOTAL GASEOUS ORGANIC CONCENTRATION USING A FLAME IONIZATION ANALYZER 1.0 Scope and Application. 1.1 Analytes. Analyte CAS No. Sensitivity Total Organic Compounds N/A
More informationTransient Analyses In Relief Systems
Transient Analyses In Relief Systems Dirk Deboer, Brady Haneman and Quoc-Khanh Tran Kaiser Engineers Pty Ltd ABSTRACT Analyses of pressure relief systems are concerned with transient process disturbances
More informationEXPERIMENTAL STUDY ON THE DISCHARGE CHARACTERISTICS OF SLUICE FOR TIDAL POWER PLANT
EXPERIMENTAL STUDY ON THE DISCHARGE CHARACTERISTICS OF SLUICE FOR TIDAL POWER PLANT Sang-Ho Oh 1, Kwang Soo Lee 1 and Dal Soo Lee 1 The discharge characteristics of sluice caisson for tidal power plant
More informationDrilling Efficiency Utilizing Coriolis Flow Technology
Session 12: Drilling Efficiency Utilizing Coriolis Flow Technology Clement Cabanayan Emerson Process Management Abstract Continuous, accurate and reliable measurement of drilling fluid volumes and densities
More informationDynamic Simulation for T-9 Storage Tank (Holding Case)
Dynamic Simulation for T-9 Storage Tank (Holding Case) CASE 1: 19,642 Kg/Hr (Holding: 52 o C), No Liquid Draw Workshop Description Estimation of vapor flow rate coming out from the T-9 tank for holding
More informationAnalysis of the application and sizing of pressure safety valves for fire protection on offshore oil and gas installations Annex I
Analysis of the application and sizing of pressure safety valves for fire protection on offshore oil and gas installations Annex I Article draft The annex contains an article draft, based on an investigation
More informationCALCULATING THE SPEED OF SOUND IN NATURAL GAS USING AGA REPORT NO Walnut Lake Rd th Street Houston TX Garner, IA 50438
CALCULATING THE SPEED OF SOUND IN NATURAL GAS USING AGA REPORT NO. 10 Jerry Paul Smith Joel Clancy JPS Measurement Consultants, Inc Colorado Engineering Experiment Station, Inc (CEESI) 13002 Walnut Lake
More informationProcess Equipment Exposed to Fire. A Case Study on the Behaviour of a Fire Exposed LNG Segment.
Process Equipment Exposed to Fire. A Case Study on the Behaviour of a Fire Exposed LNG Segment. Arve Klavenes and Geir Berge Petrell AS Kjøpmannsgata 19, NO-713 Trondheim, Norway When pressurized equipment
More informationLOW PRESSURE EFFUSION OF GASES adapted by Luke Hanley and Mike Trenary
ADH 1/7/014 LOW PRESSURE EFFUSION OF GASES adapted by Luke Hanley and Mike Trenary This experiment will introduce you to the kinetic properties of low-pressure gases. You will make observations on the
More informationThe Split of Two-Phase-Flow at Horizontal Side-T-junctions in Unbalanced Pipe Systems for Clean Extinguishing Agents
The Split of Two-Phase-Flow at Horizontal Side-T-junctions in Unbalanced Pipe Systems for Clean Extinguishing Agents Abstract by Gudrun Fay Minimax GmbH & CO. KG Industriestraße 10-12, 23840 Bad Oldesloe,
More information16. Studio ScaleChem Calculations
16. Studio ScaleChem Calculations Calculations Overview Calculations: Adding a new brine sample Studio ScaleChem can be used to calculate scaling at one or more user specified temperatures and pressures.
More informationNational Fire Protection Association. 1 Batterymarch Park, Quincy, MA Phone: Fax:
National Fire Protection Association 1 Batterymarch Park, Quincy, MA 02169-7471 Phone: 617-770-3000 Fax: 617-770-0700 www.nfpa.org M E M O R A N D U M TO: FROM: NFPA Technical Committee on Electrical Equipment
More informationLOW PRESSURE EFFUSION OF GASES revised by Igor Bolotin 03/05/12
LOW PRESSURE EFFUSION OF GASES revised by Igor Bolotin 03/05/ This experiment will introduce you to the kinetic properties of low-pressure gases. You will make observations on the rates with which selected
More informationTechnical Brief - Wave Uprush Analysis Island Harbour Club, Gananoque, Ontario
Technical Brief - Wave Uprush Analysis RIGGS ENGINEERING LTD. 1240 Commissioners Road West Suite 205 London, Ontario N6K 1C7 October 31, 2014 Table of Contents Section Page Table of Contents... i List
More informationTutorial. BOSfluids. Relief valve
Tutorial Relief valve The Relief valve tutorial describes the theory and modeling process of a pressure relief valve or safety valve. It covers the algorithm BOSfluids uses to model the valve and a worked
More informationUncertainty in the analysis of the risk of BLEVE Fireball in process plants and in transportation
Uncertainty in the analysis of the risk of BLEVE Fireball in process plants and in transportation Joaquim Casal Centre for Studies on Technological Risk (CERTEC) EEBE, Universitat Politècnica de Catalunya
More informationWind Tunnel Testing Guidance. Arjan Voogt
Wind Tunnel Testing Guidance Arjan Voogt WIND TUNNEL TESTING Proven method for airplanes, city planning, car design competitive cycling, rockets trajectories and skiing BUT NOT ACCEPTED BY USCG IN STABILITY
More informationI.CHEM.E. SYMPOSIUM SERIES NO. 97 BUOYANCY-DRIVEN NATURAL VENTILATION OP ENCLOSED SPACES
BUOYANCY-DRIVEN NATURAL VENTILATION OP ENCLOSED SPACES M. R. Marshall* and P. L. Stewart-Darling* A simple mathematical model for the buoyancy driven ventilation of an enclosed space, using a two-pipe
More informationSTUDY OF SLUG CONTROL TECHNIQUES IN PIPELINE SYSTEMS
STUDY OF SLUG CONTROL TECHNIQUES IN PIPELINE SYSTEMS JOSÉ L. A,VIDAL Petrobrás Research Center - CENPES/PDEP/TOOL Av.Horácio de Macedo 95- Cidade Universitária 191-915 -Rio de Janeiro-RJ E-mail:josearias@petrobras.com.br
More informationBASF Flash Fire FRC Assessment Tool
BASF Flash Fire FRC Assessment Tool Introduction The assessment tool offered in this document was developed to assist BASF manufacturing units in evaluating the potential for flash fire occurrence and
More informationPump-Fan-Compressor Sizing
Pump-Fan-Compressor Sizing Introduction This program determines the fluid transportation characteristics of dominant pipeline process systems containing no loops. In addition, it determines the yearly
More informationMicro Channel Recuperator for a Reverse Brayton Cycle Cryocooler
Micro Channel Recuperator for a Reverse Brayton Cycle Cryocooler C. Becnel, J. Lagrone, and K. Kelly Mezzo Technologies Baton Rouge, LA USA 70806 ABSTRACT The Missile Defense Agency has supported a research
More informationSIMULATIONS OF HYDROGEN RELEASES FROM A STORAGE TANKS: DISPERSION AND CONSEQUENCES OF IGNITION
SIMULATIONS OF HYDROGEN RELEASES FROM A STORAGE TANKS: DISPERSION AND CONSEQUENCES OF IGNITION Angers, B. 1, Hourri, A. 1, Bénard, P. 1, Tessier, P. 2 and Perrin, J. 3 1 Hydrogen Research Institute, Université
More informationQuantitative Risk Analysis (QRA)
Quantitative Risk Analysis (QRA) A realistic approach to relief header and flare system design Siemens AG 2017, All rights reserved 1 Quantitative Risk Analysis Introduction Most existing pressure relief
More informationLaboratory studies of water column separation
IOP Conference Series: Materials Science and Engineering OPEN ACCESS Laboratory studies of water column separation To cite this article: R Autrique and E Rodal 2013 IOP Conf. Ser.: Mater. Sci. Eng. 52
More informationThis portion of the piping tutorial covers control valve sizing, control valves, and the use of nodes.
Piping Tutorial A piping network represents the flow of fluids through several pieces of equipment. If sufficient variables (flow rate and pressure) are specified on the piping network, CHEMCAD calculates
More informationA Software Model for the Assessment of the Consequences of Explosions in Congested and Confined Spaces on Personnel, Buildings and Process Equipment
535 A publication of VOL. 36, 2014 CHEMICAL ENGINEERING TRANSACTIONS Guest Editors: Valerio Cozzani, Eddy de Rademaeker Copyright 2014, AIDIC Servizi S.r.l., ISBN 978-88-95608-27-3; ISSN 2283-9216 The
More informationAbstract. 1 Introduction
Risk assessment study of the mutual interactive influence of working procedures on terminals handling dangerous goods in port of Koper (Slovenia) L. Battelino Water Management Institute, Maritime Engineering
More information