Page 53 | University of Utah Partnerships | J. Willard Marriott Digital Library

American Flame Research Committee

Contents | 53 of 53

Page 53

Download PDF | | Reference URL | Gallery View | Parent Record

Update Item Information

Title	Refinery Heater Simulation by the Hottel Zoning Method
Creator	Loftus, Jordan ScD
Publisher	Digitized by J. Willard Marriott Library, University of Utah
Date	1989
Spatial Coverage	presented at Short Hills, New Jersey
Abstract	The Heater Design System (HDS) is a comprehensive set of Fortran VS77 routines which simulates the behavior of refinery heaters. It is a heat transfer, mass and energy balance program featuring the Similarity of Jet Theory for flow field generation and Hottel Zoning for energy balance solution. The program is used to trouble-shoot plant problems, evaluate competing vendor designs and to revamp old heaters for new services. The data required to drive the program are readily accessible to the practicing engineer in a refinery or in an engineering department. On an IBH 3090 Hodel 600 mainframe under HVS/XA/TSO operating system, a cylindrical heater operating with a convection section is simulated in 10.3 CPU seconds when matching process duty and a box heater, 35.6 seconds at specified firing rate. The fuel is either gas, liquid and/or solid; oxidant is air, enriched air or gas turbine exhaust; diluent is a non-oxidant gas mixture, water or steam. The burner may be single or combination fuel fired. The user characterizes the burner by its minimum throat area, air jet angle, pressure drop coefficient and flame length. The flue gas is computed assuming complete combustion. User may specify either excess air, oxygen content or mass rates." The flue gas is simulated by either a 1 clear - 2 grey gas (gas firing) or 3 grey gas model (fuel oil firing). Process side linkage is provided by specifying its temperature and transport properties profile. The inside film heat transfer coefficient is based on equations provided by APIRP530. The program divides an axi-symmetrical cylindrical furnace into 5 by 10 gas volumes, and a box heater into 3 by 4 by 4 rectilinear gas volumes per gas-space. The user specifies the box dimensions, tube layout and burner(s) location. A maximum of 3 gas spaces with different heat transfer requirements is handled. The process coils are replaced by equivalent sink planes. The 3D box heater interchange areas are computed by the method of Hottel and Cohen. Errku data are used for 2D cylindrical heater.
Type	Text
Format	application/pdf
Language	eng
Rights	This material may be protected by copyright. Permission required for use in any form. For further information please contact the American Flame Research Committee.
Conversion Specifications	Original scanned with Canon EOS-1Ds Mark II, 16.7 megapixel digital camera and saved as 400 ppi uncompressed TIFF, 16 bit depth.
Scanning Technician	Cliodhna Davis
ARK	ark:/87278/s6571fkv
Setname	uu_afrc
ID	5479
Reference URL	https://collections.lib.utah.edu/ark:/87278/s6571fkv

Page Metadata

Title	Page 53
Format	application/pdf
OCR Text	Show PROPRIETARY PROPERTY OF TEXACO ENGINEERING DEPT. - HEATER DESIGN SYSTEM - IBM VERSION 02/89 Table 3R - Plant 2 08/14/89 GAS ONLY FIRNG PAGE 7 STREAM * 1 2 3 4 5 STATE: IDEALGAS OR NON-GAS ONLY GAS GAS GAS GAS FUEL AMBIENT FLUE GAS FLUE GAS GAS AIR TO TO OUT OF CRITICAL GASBURNR CONVECT CONVECT t-DLE WI' RANKINE PSIA QFUEL WET AIR FLUE GAS TITLE TITLE C1 16.043 343.1 667.2 32.347 0.000 0 .000 0.000 •••••••• H2O 18.015 1165.1 3197.8 0.000 1.257 17."090 17.090 •••••••• CO2 44.010 547.6 1069.9 0.000 0.000 9.450 9. 450 •••••••• B2 2.016 59.8 188.1 24.411 0.000 0.000 0.000 .. _.. .. N2 28.013 227.2 492.3 0.000 77.049 70.911 70 . 911 _.. .... 02 31. 999 278.3 731.9 0.000 20.726 1.658 1.658 _.. .... C2 30.070 549.7 708.3 18.759 0.000 0.000 0.000 _ ...... C3 44.097 665.6 615.8 21.044 0.000 0.000 0.000 •••••••• NC4 58.124 765.4 551.1 1.563 0.000 0.000 0.000 .. _ .... C2E 28.054 508.3 730.4 1.876 0.000 0.000 0.000 _.. .... AR 39.948 271.4 706.9 0.000 0.968 0.891 0.891 •• _ •••• 100.000 100.000 100.000 100.000 100 . 000 LB MJLES PER BR 267.20 3721.44 4043.57 4043.57 •••••••• LB / BR 5888. 107285. 113173. 113173 .•• _ •••• t-DLECULAR WEIGHT 22.04 28.83 27.99 27.99 •••••••• TEMPERATURE, DEGREES FAHRENHEIT 70. 74. 3552. 1807. • ••••••• PRESSURE PSIA 42. 15. 15 . 15. • ••••••• WEIGHT FRACTION LIQUID 0.00 0.00 0.00 0.00 •••••••• DENSITY @ T & P, PCF 0.16167 0.07398 0.00956 0.01691 •••••••• CFS ft T & P, 10.12 402.81 3290.01 1859.11 .... _.. VISCOS. @ T CENTIPOISE 0.0095 0.0177 0.0632 0.0454 •••••••• CONDUCT.@ T , BTU/BR-FT-DEG R 0.02372 0.01719 0.08845 0.05789 •••••••• HEAT FORMATION, . (02,C(S»-0 @ 0 RANKINE BTU / HR .. _.. .. •••••••• •••••••• •••••••• •••••••• MBTU / HR -4733. 8979. 4246. -62882. _ ...... r-t1BTU / HR -5. 9. 4. -63. • ••••••• SPECIFIC HEAT 0.485 0.240 0.347 0.322 •••• _ •• REDUCED TEMPERATURE 1.357 2.135 9 . 575 5. 411 •••••••• REDUCED PRESSURE 0.076 0.025 0.014 0.014 •••••••• WATER PARTIAL PRESSURE, PSIA •••••••• 0.185 2.512 2.512 •••••••• SATURATION TEMP., FARR. •• _.* •• 53 . 135. 135. . ... -.. 1 2 3 4 5 GRAVITY @ 60 FAHR. API 0.0 0.0 0.0 0.0 ...... - SPECIFIC 0.000 0.000 0.000 0.000 •••••••• POUND / SCF(60F) 0.0581 0.0760 0.0738 0.0738 •• _.* •• ULTIMATE ANALYSIS (AS FIRED) CARBON WI'. % 77 .941 0.000 4.055 4.055 •••••• . HYDROGEN WI'. % 22.059 0.088 1.231 1.231 - ••• - SULFUR WI'. % 0.000 0.000 0.000 0.000 _.. .... OXYGEN WI'. % 0.000 23.703 22.469 22.469 •••••• - NITROGEN WI'. % 0.000 74.869 70.973 70.973 •• * ••••• ARGON WI'. % 0.000 1. 341 1.271 1.271 -_ .... ASH WI'. % (INERTS) 0.000 0.000 0.000 0.000 .. - t-DISTURE WI'. % 0.000 0.000 0.000 0.000 _.. .... 100.000 100.000 100.000 100.000 100.000 CALORIFIC VALUE: LOWER , BTU/LB 21144.0 0.0 0.0 0.0 ••••• - CALORIFIC VALUE: HIGHER, BTU/LB 23233.5 8 .3 116.6 116.6 •••••••• ENTHALPY RELATIVE TO LHV @60F, BTU/LB 4.83 3.36 1103.52 510.38 •••• * ••
Setname	uu_afrc
ID	5478
Reference URL	https://collections.lib.utah.edu/ark:/87278/s6571fkv/5478

Back to Search Results