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     ‫א‬ -٢-
‫ﻃﺒﻘﺎ ﻟﻘﻮﺍﻧﲔ ﺍﳌﻠﻜﻴﺔ ﺍﻟﻔﻜﺮﻳﺔ‬ ‫א‬ ‫א‬ ‫א‬ ‫.‬ ‫אא‬ ‫א‬ ‫)ﻋـﱪ ﺍﻻﻧﱰﻧـﺖ ﺃﻭ‬ ‫א‬ ‫אא‬ ‫ﻟﻠﻤﻜﺘﺒــﺎﺕ ﺍﻻﻟﻜﱰﻭﻧﻴــﺔ ﺃﻭ ﺍﻷﻗــﺮﺍﺹ ﺍﳌﺪﳎــﺔ ﺃﻭ ﺍﻯ‬ ‫א‬ ‫ﻭﺳﻴﻠﺔ ﺃﺧﺮﻯ (‬ ‫א‬ ‫א‬ ‫.‬ ‫.‬ ‫א א‬
‫‪‬‬ ‫:ﺍﻟﻨﻅﺭﻴﺎﺕ ﺍﻷﺴﺎﺴﻴﺔ ﻓﻲ ﺍﻟﺘﺼﻤﻴﻤﺎﺕ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴﺔ - ٦ -‬ ‫ﺍﻟﺒﺎﺏ ﺍﻷﻭل‬ ‫: ﺘﺼﻤﻴﻡ ﺨﻁﻭﻁ ﺃﻨﺎﺒﻴﺏ ﻨﻘل ﺍﻟﺒﺘﺭﻭل .......... - ٣٤ -‬ ‫ﺍﻟﺒﺎﺏ ﺍﻟﺜﺎﻨﻲ‬ ‫ﺍﻟﺒﺎﺏ ﺍﻟﺜﺎﻟﺙ : ﺘﻁﺒﻴﻘﺎﺕ ﻋﻠﻰ ﺍﻟﺘﺼﻤﻴﻤﺎﺕ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴﺔ ...... - ٧٧ -‬ ‫ﺍﻟﺒﺎﺏ ﺍﻟﺭﺍﺒﻊ : ﺘﺼﻤﻴﻡ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ ................... - ٢١١ -‬ ‫-٣-‬
-٤-
‫‪‬‬ ‫ﻤﻨﺫ ﻋﺩﺓ ﺴﻨﻭﺍﺕ ﻭﺍﻟﺤﺎﺠﺔ ﻤﺎﺴﺔ ﺇﻟـﻰ ﺒﺤـﺙ ﻤﺘﺨﺼـﺹ‬ ‫ﻴﺘﻨﺎﻭل ﻤﻭﻀﻭﻉ ﺍﻟﺘﺼﻤﻴﻤﺎﺕ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴﺔ ﻟﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫ﻭﺘﻁﺒﻴﻘﺎﺘﻬﺎ ﻓﻲ ﻤﺠﺎل ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﻭﻗﺩ ﺃﻋﺩﺩﺕ ﻫﺫﺍ ﺍﻟﺒﺤﺙ ﺁﻤﻼ‬ ‫ﹰ‬ ‫ﺃﻥ ﻴﻭﻀﺢ ﺍﻟﻤﻭﻀﻭﻋﺎﺕ ﺍﻟﺘﻲ ﻗﺩ ﺘﻜﻭﻥ ﻤﺒﻬﻤﺔ ﻓﻲ ﻫﺫﺍ ﺍﻟﻤﺠﺎل‬ ‫ﻜﻤﺎ ﺃﻥ ﺇﺤﺘﻭﺍﺀ ﻫﺫﺍ ﺍﻟﺒﺤﺙ ﻋﻠﻰ ﺒﻌﺽ ﺍﻟﻤﻌﺎﺩﻻﺕ ﻭﺍﻟﺠـﺩﺍﻭل‬ ‫ﻭﺍﻟﻘﻭﺍﻋ ـﺩ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴ ـﺔ ﺍﻟﻤﺴ ـﺘﻨﺘﺠﺔ ﺒﻤﻌﺭﻓﺘ ـﻰ ﻭﺍﻷﻤﺜﻠ ـﺔ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ﻭﺍﻟﺭﺴﻭﻤﺎﺕ ﺍﻟﺘﻭﻀﻴﺤﻴﺔ ﻭﺍﻟﺘﻲ ﺤﺎﻭﻟـﺕ ﺠﺎﻫـﺩﺍ ﺃﻥ ﺃﺠﻌﻠﻬـﺎ‬ ‫ﹰ‬ ‫ﻤﺒﺴﻁﺔ ﺤﺘﻰ ﻴﺘﺴﻨﻰ ﻟﻜل ﺩﺍﺭﺱ ﺃﻭ ﻤﺘﺨﺼﺹ ﻓﻲ ﻫﺫﺍ ﺍﻟﻤﺠﺎل‬ ‫ﺃﻥ ﻴﺘﻨﺎﻭﻟﻬﺎ ﺒﻜل ﺴﻼﺴﺔ ﻭﻴﺴﺭ ﺁﻤﻼ ﻤﻥ ﺍﷲ ﻋﺯ ﻭﺠل ﺃﻥ ﻴﻌﻭﺩ‬ ‫ﹰ‬ ‫ﻫﺫﺍ ﺍﻟﺒﺤﺙ ﺒﺎﻟﻨﻔﻊ ﻋﻠﻰ ﺠﻤﻴﻊ ﺍﻟﻤﻬﺘﻤﻴﻥ ﺒﻬﺫﺍ ﺍﻟﻤﺠﺎل.‬ ‫-٥-‬
  ‫א‬ ‫א‬ ‫א‬ ‫א‬ ‫א‬ ‫א‬ -٦-
‫ﺍﻟﻜﺜﺎﻓﺔ )‪:(Density‬‬ ‫ﻭﻫﻰ ﺘﻌﺒﺭ ﻋﻥ ﻜﺘﻠﺔ ﻭﺤﺩﺓ ﺍﻟﺤﺠﻭﻡ ﻤﻥ ﺍﻟﻤﺎﺩﺓ ﻭﻴﺭﻤﺯ ﻟﻬـﺎ‬ ‫ﺒﺎﻟﺭﻤﺯ ‪ ρ‬ﻭﻭﺤﺩﺘﻬﺎ ﻫﻰ ﻜﺘﻠﺔ ﺍﻟﺠﺭﺍﻡ ﻟﻜل ﺴـﻨﺘﻴﻤﺘﺭ ﻤﻜﻌـﺏ‬ ‫)ﺠﻡ/ﺴﻡ٣( ﻭﺘﻌﺘﻤﺩ ﻜﺜﺎﻓﺔ ﺍﻟﺴﺎﺌل ﻋﻠﻰ ﻨﻭﻋﻪ ﻭﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ،‬ ‫ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺀ ﺘﺴﺎﻭﻯ ١ﺠﻡ/ﺴﻡ٣ ﻋﻨﺩ ٦,٥١‪º‬ﻡ.‬ ‫ﺍﻟﻭﺯﻥ ﺍﻟﻨﻭﻋﻰ )‪:(Specific weight‬‬ ‫ﻭﻫﻭ ﻴﻌﺒﺭ ﻋﻥ ﻭﺯﻥ ﻭﺤﺩﺓ ﺍﻟﺤﺠﻭﻡ ﻤﻥ ﺍﻟﻤﺎﺩﺓ ﻭﻴﺭﻤﺯ ﻟـﻪ‬ ‫ﺒﺎﻟﺭﻤﺯ ‪ w‬ﻭﻭﺤﺩﺘﻪ ﻫﻰ ﻗﻭﺓ ﺍﻟﺠﺭﺍﻡ ﻟﻜـل ﺴـﻨﺘﻴﻤﺘﺭ ﻤﻜﻌـﺏ‬ ‫)ﺠﻡ/ﺴﻡ٣( ﻤﻊ ﻤﻼﺤﻅﺔ ﺃﻥ ‪ w = ρg‬ﺤﻴﺙ ﺃﻥ ‪ g‬ﻫﻰ ﻋﺠﻠـﺔ‬ ‫ﺍﻟﺠﺎﺫﺒﻴﺔ ﺍﻷﺭﻀﻴﺔ ﻭﺘﺴﺎﻭﻯ ٧٦٠٨,٩ ﻤﺘﺭ/ﺜﺎﻨﻴﺔ٢.‬ ‫-٧-‬
‫ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ )‪:(Specific Gravity‬‬ ‫ﻭﺘﻌﺭﻑ ﺒﺄﻨﻬﺎ ﺍﻟﻨﺴﺒﺔ ﺒﻴﻥ ﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺩﺓ ﺃﻭ ﻭﺯﻨﻬـﺎ ﺍﻟﻨـﻭﻋﻰ‬ ‫ﻭﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺀ ﺃﻭ ﻭﺯﻨﻪ ﺍﻟﻨﻭﻋﻰ ﻭﻴﺭﻤﺯ ﻟﻬﺎ ﺒﺎﻟﺭﻤﺯ ‪ sp.gr‬ﻭﻫﻰ‬ ‫ﻨﺴﺒﺔ ﺒﺩﻭﻥ ﻭﺤﺩﺍﺕ، ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ ﻟﻠﻤـﺎﺀ‬ ‫ﺘﺴﺎﻭﻯ ١ ﻭﻟﻠﺯﺌﺒﻕ ﺘﺴـﺎﻭﻯ ٦,٣١ ﻭﻓـﻲ ﺍﻟﻨﻅـﺎﻡ ﺍﻟﻤﺘـﺭﻯ‬ ‫ﻟﻠﻭﺤﺩﺍﺕ )ﺴﻨﺘﻴﻤﺘﺭ – ﺠﺭﺍﻡ – ﺜﺎﻨﻴﺔ( ﺘﻜﻭﻥ ﺍﻟﻜﺜﺎﻓـﺔ ﺍﻟﻨﺴـﺒﻴﺔ‬ ‫ﺘﺴﺎﻭﻯ ﺍﻟﻜﺜﺎﻓﺔ ﻋﺩﺩﻴﺎ.‬ ‫ﹰ‬ ‫ﺍﻟﻀﻐﻁ )‪:(Pressure‬‬ ‫ﻴﻌﺭﻑ ﺍﻟﻀﻐﻁ ﺒﺄﻨﻪ ﺍﻟﻘﻭﺓ ﺍﻟﻤﺅﺜﺭﺓ ﻋﻠﻰ ﻭﺤـﺩﺓ ﺍﻟﻤﺴـﺎﺤﺔ‬ ‫ﻭﺘﻜﻭﻥ ﺍﻟﻘﻭﺓ ﻤﺘﻌﺎﻤﺩﺓ ﻋﻠﻰ ﺍﻟﻤﺴﺎﺤﺔ ﻭﻭﺤﺩﺘﻪ ﻫـﻰ ﻜﻴﻠـﻭﺠﺭﺍﻡ‬ ‫ﻟﻜل ﺴﻨﺘﻴﻤﺘﺭ ﻤﺭﺒﻊ )ﻜﺠﻡ/ﺴﻡ٢( ﻭﻓﻲ ﺤﺎﻟﺔ ﻭﺠﻭﺩ ﺴﺎﺌﻠﻴﻥ ﻟﻬـﻡ‬ ‫ﻜﺜﺎﻓﺔ ١، ٥,٠ ﻜﻤﺎ ﺒﺎﻟﺸﻜل )١( ﻓﺈﻥ ﺍﻟﺴﺎﺌل ﺫﻭ ﺍﻟﻜﺜﺎﻓﺔ ﺍﻷﻗـل‬ ‫ﻻﺒﺩ ﺃﻥ ﻴﺼﻌﺩ ﺇﻟﻰ ﺇﺭﺘﻔﺎﻉ ﻋﻤﻭﺩ ﺃﻋﻠﻰ ﻟﻜﻲ ﻴﻭﻟﺩ ﻨﻔﺱ ﺍﻟﻀﻐﻁ‬ ‫ﻋﻨﺩ ﻨﻔﺱ ﺍﻟﻤﺴﺘﻭﻯ ﻤﺜل ﺍﻟﺴﺎﺌل ﺍﻷﺜﻘل ﻭﻴﻜﻭﻥ ﺍﻟﻀـﻐﻁ ﻋﻨـﺩ‬ ‫ﺃﺴﻔل ﺍﻟﻌﻤﻭﺩ ‪ H‬ﻟﻜل ﺴﺎﺌل ﻴﺴﺎﻭﻯ ﻭﺯﻥ ﺍﻟﺴﺎﺌل ﻓـﻭﻕ ﻨﻘﻁـﺔ‬ ‫ﻗﻴﺎﺱ ﺍﻟﻀﻐﻁ ﻤﻘﺴﻭﻤﺎ ﻋﻠﻰ ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁـﻊ ‪ A‬ﻋﻨـﺩ ﻨﻔـﺱ‬ ‫ﹰ‬ ‫ﺃﻯ ﻴﺴﺎﻭﻯ ‪ WH‬ﻭﺒﺫﻟﻙ ﻴﻤﻜﻨﻨﺎ ﺍﻟﺘﻌﺒﻴﺭ ﻋـﻥ‬ ‫ﺍﻟﻨﻘﻁﺔ‬ ‫‪AHW‬‬ ‫‪A‬‬ ‫-٨-‬
‫ﺍﻟﻀﻐﻁ ﺒﺩﻻﻟﺔ ﺇﺭﺘﻔﺎﻉ ﻋﻤﻭﺩ ﺴﺎﺌل ﻤﻌﻴﻥ ﻭﻫـﻭ ﻤـﺎ ﻴﺴـﻤﻰ‬ ‫‪ Head‬ﺃﻭ ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ‪ Pressure Energy‬ﻭﻭﺤﺩﺘﻪ ﻫـﻰ‬ ‫ﻜﺠﻡ.ﻤﺘﺭ/ﻜﺠﻡ ﺃﻯ ﺍﻟﻤﺘﺭ ﻤﻊ ﻤﻼﺤﻅﺔ ﺃﻥ )‪ (Head‬ﺒـﺎﻟﻤﺘﺭ =‬ ‫ﺍﻟﻀﻐﻁ ﺒﺎﻟﻜﺠﻡ/ﺴﻡ٢×٠١/ ‪Sp.gr‬‬ ‫ﺸﻜل )١(‬ ‫-٩-‬
‫ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ ﻴﺴﺎﻭﻯ ٣٠,١ﻜﺠﻡ/ﺴﻡ٢‬ ‫ﻋﻨﺩ ﻤﺴﺘﻭﻯ ﺴﻁﺢ ﺍﻟﺒﺤﺭ ﻭﻫﻭ ﻴﺴﺎﻭﻯ ﺍﻟﻀﻐﻁ ﺍﻟﻨﺎﺘﺞ ﻤﻥ ﻭﺯﻥ‬ ‫01 × 30.1‬ ‫ﺃﻯ ٣,٠١ ﻤﺘﺭ ﻭﻴﺴﺎﻭﻯ ﺃﻴﻀﺎ‬ ‫ﹰ‬ ‫ﻋﻤﻭﺩ ﻤﺎﺀ ﺇﺭﺘﻔﺎﻋﻪ‬ ‫1‬ ‫ـﻪ‬ ‫ـﻕ ﺇﺭﺘﻔﺎﻋـ‬ ‫ـﻭﺩ ﺯﺌﺒـ‬ ‫ـﻐﻁ ﺍ ـﺎﺘﺞ ـﻥ ﻭﺯﻥ ﻋﻤـ‬ ‫ﻤـ‬ ‫ﻟﻨـ‬ ‫ﺍﻟﻀـ‬ ‫01 × 30.1‬ ‫ﺃﻯ ٦٧ﺴﻡ.‬ ‫‪= 0.76 mt‬‬ ‫6.31‬ ‫ﺍﻟﻀﻐﻭﻁ ﺍﻟﻌﻴﺎﺭﻴﺔ ﻭﺍﻟﻤﻁﻠﻘﺔ:‬ ‫ﺸﻜل )٢(‬ ‫- ٠١ -‬
‫ﻜﻤﺎ ﻴﺘﻀﺢ ﻤﻥ ﺸﻜل )٢( ﺃﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻌﻴـﺎﺭﻯ ) ‪Gage‬‬ ‫‪ (pressure‬ﻫﻭ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻨﺴـﻭﺏ ﺇﻟـﻰ ﺍﻟﻀـﻐﻁ ﺍﻟﺠـﻭﻯ‬ ‫)‪ (Atmospheric pressure‬ﺒﺈﻋﺘﺒﺎﺭ ﺃﻥ ﺍﻟﻀـﻐﻁ ﺍﻟﺠـﻭﻯ‬ ‫ﻴﺴﺎﻭﻯ ﺼﻔﺭ ﻓﻬﻭ ﺇﻤﺎ ﺃﻋﻠﻰ ﻤﻥ ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ ﻓﻴﺴﻤﻰ ﻀﻐﻁ‬ ‫)‪ (pressure‬ﺃﻭ ﺃﻗل ﻤﻥ ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ ﻓﻴﺴـﻤﻰ ﺘﻔﺭﻴـﻎ ﺃﻭ‬ ‫ﺨﻠﺨﻠﺔ )‪ (vacuum‬ﻭﻴﻘﺎﺱ ﻫﺫﺍ ﺍﻟﻀﻐﻁ ﺒﻭﺍﺴﻁﺔ ﺃﺠﻬﺯﺓ ﻤﺜـل‬ ‫ﺍﻟﻤ ـﺎﻨﻭﻤﺘﺭﺍﺕ ﻭﺃﻨﺒﻭﺒ ـﺔ ﺒ ـﻭﺭﺩﻭﻥ ﺃﻤ ـﺎ ﺍﻟﻀ ـﻐﻁ ﺍﻟﻤﻁﻠ ـﻕ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ ـ‬ ‫ـ‬ ‫)‪ (Absolute pressure‬ﻓﻬﻭ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻨﺴﻭﺏ ﺇﻟﻰ ﺍﻟﺼـﻔﺭ‬ ‫ﺍﻟﻤﻁﻠﻕ ﺤﻴﺙ ﺃﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻁﻠـﻕ = ﺍﻟﻀـﻐﻁ ﺍﻟﻌﻴـﺎﺭﻯ +‬ ‫ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ.‬ ‫ﻀﻐﻁ ﺍﻟﺒﺨﺎﺭ )‪:(Vapor pressure‬‬ ‫ﻭﻴﻌﺭﻑ ﺒﺄﻨﻪ ﺍﻟﻀﻐﻁ ﺍﻟﺫﻯ ﻋﻨﺩﻩ ﻴﺘﺤﻭل ﺍﻟﺴﺎﺌل ﺇﻟﻰ ﺒﺨـﺎﺭ‬ ‫ﻭﻴﻌﺘﻤﺩ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﻭﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ ﻭﻴﺘﻡ ﺍﻟﺘﻌﺒﻴﺭ ﻋﻨـﻪ‬ ‫ﺒﺎﻟﻘﻴﻡ ﺍﻟﻤﻁﻠﻘﺔ ﻟﻠﻀﻐﻭﻁ، ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻀﻐﻁ ﺍﻟﺒﺨﺎﺭ ﻟﻠﻤﺎﺀ‬ ‫ـﺔ )٦,٣٢‪º‬ﻡ( ـﺎﻭﻯ‬ ‫ﻴﺴـ‬ ‫ـﺭﺍﺭﺓ ﺍﻟﻌﺎﺩﻴـ‬ ‫ـﺎﺕ ﺍﻟﺤـ‬ ‫ـﺩ ﺩﺭﺠـ‬ ‫ﻋﻨـ‬ ‫٣٠,٠ﻜﺠﻡ/ﺴﻡ٢ ﻤﻁﻠﻕ ﻤﻌﻨﻰ ﺫﻟﻙ ﺃﻨﻪ ﻟﻭ ﺘﻡ ﺨﻠﺨﻠﺔ ﺍﻟﻔﺭﺍﻍ ﻓﻭﻕ‬ ‫ﺴﻁﺢ ﺍﻟﻤﺎﺀ ﺤﺘﻰ ﻴﺼل ﺍﻟﻀﻐﻁ ﺇﻟﻰ ﻫﺫﻩ ﺍﻟﻘﻴﻤﺔ ﻓـﺈﻥ ﺍﻟﻤـﺎﺀ‬ ‫ﻴﺘﺒﺨﺭ ﻋﻨﺩ ﺩﺭﺠﺎﺕ ﺍﻟﺤﺭﺍﺭﺓ ﺍﻟﻌﺎﺩﻴﺔ.‬ ‫- ١١ -‬
‫ﺸﻜل )٣(‬ ‫ﺃﻗﺼﻰ ﻀﻐﻁ ﺴﺎﻟﺏ:‬ ‫ﻜﻤﺎ ﻴﺘﻀﺢ ﻤﻥ ﺸﻜل )٣( ﺃﻨﻪ ﺇﺫﺍ ﺘﻡ ﻋﻤـل ﺨﻠﺨﻠـﺔ ﻓـﻲ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﺍﻟﺭﺃﺴﻴﺔ ﻓﺈﻥ ﺍﻟﻤﺎﺀ ﻴﺼﻌﺩ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﺒﺘﺄﺜﻴﺭ ﺍﻟﻀـﻐﻁ‬ ‫ﺍﻟﺠﻭﻯ ﺤﺘﻰ ﻴﺼل ﺇﻟﻰ ﺤﺩ ﻤﻌﻴﻥ ﻴﻜﻭﻥ ﺍﻟﻀﻐﻁ ﻋﻨﺩﻩ ﻴﺴـﺎﻭﻯ‬ ‫ﻀﻐﻁ ﺍﻟﺒﺨﺎﺭ ﻭﻴﻁﻠﻕ ﻋﻠﻰ ﺍﻹﺭﺘﻔﺎﻉ ﻤﻥ ﺴﻁﺢ ﺍﻟﺴﺎﺌل ﺒﺎﻹﻨـﺎﺀ‬ ‫ﺤﺘﻰ ﻫﺫﺍ ﺍﻟﺤﺩ ﺒﺄﻗﺼﻰ ﻀﻐﻁ ﺴﺎﻟﺏ )ﻓﻲ ﺼﻭﺭﺓ ‪ (Head‬ﻭﻫﻭ‬ ‫]30.0 − 30.1[ × 01‬ ‫ﻟﻠﻤـﺎﺀ ﻋﻨـﺩ ﺩﺭﺠـﺎﺕ‬ ‫ﻴﺴﺎﻭﻯ ‪= 10 mt‬‬ ‫1‬ ‫ﺍﻟﺤﺭﺍﺭﺓ ﺍﻟﻌﺎﺩﻴﺔ.‬ ‫- ٢١ -‬
‫ﺍﻟﻠﺯﻭﺠﺔ )‪:(Viscosity‬‬ ‫ﻴﻁﻠﻕ ﺇﺴﻡ ﺍﻟﻤﻭﺍﺌﻊ ﻋﻠﻰ ﺍﻟﺴﻭﺍﺌل ﻭﺍﻟﻐﺎﺯﺍﺕ ﻭﺘﺴﻤﻰ ﺨﺎﺼﻴﺔ‬ ‫ﺍﻟﺴﺎﺌل ﺍﻟﺘﻲ ﺘﻭﻟﺩ ﻤﻘﺎﻭﻤﺔ ﻟﻘﻭﻯ ﺍﻟﻘﺹ ﻓﻲ ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻠﺯﻭﺠـﺔ‬ ‫ﻭﺇﺫﺍ ﺘﻡ ﻤلﺀ ﺍﻟﻔﺭﺍﻍ ﺒﻴﻥ ﺴﻁﺤﻴﻥ ﻤﺴﺘﻭﻴﻴﻥ ﺒﺴﺎﺌل ﻓﻴﻠﺯﻡ ﻗـﻭﺓ‬ ‫ﻟﻜﻲ ﻴﺘﺤﺭﻙ ﺇﺤﺩﻯ ﺍﻟﺴﻁﺤﻴﻥ ﺒﺴﺭﻋﺔ ﺜﺎﺒﺘﺔ ﺒﺎﻟﻨﺴـﺒﺔ ﻟﻶﺨـﺭ‬ ‫ﻭﺘﺘﻐﻴﺭ ﺴﺭﻋﺔ ﺍﻟﺴﺎﺌل ﺨﻁﻴﺎ ﺒﻴﻥ ﺍﻟﺴﻁﺤﻴﻥ ﻭﺍﻟﻨﺴﺒﺔ ﺒﻴﻥ ﺍﻟﻘـﻭﺓ‬ ‫ﹰ‬ ‫ﻟﻜل ﻭﺤﺩﺓ ﻤﺴﺎﺤﺔ )ﺇﺠﻬﺎﺩ ﺍﻟﻘﺹ( ﺇﻟﻰ ﺍﻟﺴﺭﻋﺔ ﻟﻜـل ﻭﺤـﺩﺓ‬ ‫ﻤﺴﺎﻓﺔ ﺒﻴﻥ ﺍﻟﺴﻁﺤﻴﻥ )ﻤﻌﺩل ﺍﻟﻘﺹ( ﺘﻜﻭﻥ ﻤﻘﻴـﺎﺱ ﻟﺯﻭﺠـﺔ‬ ‫ﺍﻟﺴﺎﺌل ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﺃﻭ ﺍﻟﻤﻁﻠﻘﺔ ﻭﺍﻟﺴﻭﺍﺌل ﺍﻟﺘﻲ ﺘﺘﻨﺎﺴـﺏ ﻓﻴﻬـﺎ‬ ‫ﺇﺠﻬﺎﺩﺍﺕ ﺍﻟﻘﺹ ﻤﻊ ﻤﻌﺩﻻﺕ ﺍﻟﻘﺹ ﺘﻜﻭﻥ ﻟﻬﺎ ﻤﻌﺎﻤﻼﺕ ﻟﺯﻭﺠﺔ‬ ‫ﺜﺎﺒﺘﺔ ﻋﻨﺩ ﻀﻐﻁ ﻭﺩﺭﺠﺔ ﺤﺭﺍﺭﺓ ﻤﺤﺩﺩﻴﻥ ﻭﻴﻁﻠﻕ ﻋﻠﻴﻬﺎ ﺇﺴـﻡ‬ ‫ﺍﻟﺴـﻭﺍﺌل ﺍﻟﺤﻘﻴﻘﻴـﺔ ‪ Newtonian Liquids‬ﻭﻓﻴﻬـﺎ ﺘﺯﻴـﺩ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﻭﻤﻘﺎﻭﻤﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻤﻊ ﻨﻘﺹ ﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ.‬ ‫ﻭﺘﻜﻭﻥ ﻭﺤـﺩﺓ ﺍﻟﻠﺯﻭﺠـﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴـﺔ ﺃﻭ ﺍﻟﻤﻁﻠﻘـﺔ ﻫـﻰ‬ ‫ﺩﺍﻴﻥ.ﺜﺎﻨﻴﺔ/ﺴﻡ٢ ﻭﺘﺴـﻤﻰ ﺒـﻭﻴﺯ )‪ (poise‬ﻭﺘﺴـﺎﻭﻯ ﻋـﺩﺩﻴﺎ‬ ‫ﹰ‬ ‫ﺠﻡ/ﺴﻡ.ﺜﺎﻨﻴﺔ ﻭﺍﻟﻘﻴﺎﺱ ﺍﻟﺸﺎﺌﻊ ﻟﻠﺯﻭﺠﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﺃﻭ ﺍﻟﻤﻁﻠﻘـﺔ‬ ‫× ‪Centipoise‬‬ ‫ﻴﻜﻭﻥ ﺴﻨﺘﻰ ﺒﻭﻴﺯ )١/٠٠١ﺒﻭﻴﺯ( ﺤﻴﺙ ﺃﻥ‬ ‫‪.١٠-٣ = N.sec/m٢ = Pa.sec‬‬ ‫- ٣١ -‬
‫‪N – Newton‬‬ ‫٢‪Pa – Pascal = N/m‬‬ ‫ﻭﺃﺤﻴﺎﻨﺎ ﻴﻌﺒﺭ ﻋﻥ ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺒﺎﻟﻠﺯﻭﺠـﺔ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴـﺔ‬ ‫ﹰ‬ ‫ﻭﻫﻰ ﺘﺴﺎﻭﻯ ﺍﻟﻠﺯﻭﺠﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﻤﻘﺴﻭﻤﺔ ﻋﻠﻰ ﺍﻟﻜﺜﺎﻓﺔ )‪(w/g‬‬ ‫ﻭﻭﺤ ـﺩﺘﻬﺎ ﺍﻟﻤﺘﺭﻴ ـﺔ ﻫ ـﻰ ﺴ ـﻡ٢/ﺜﺎﻨﻴ ـﺔ ﻭﺘﺴ ـﻤﻰ ﺴ ـﺘﻭﻙ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ ـ ـ‬ ‫ـ‬ ‫)‪ (stoke‬ﻭﺍﻟﻘﻴﺎﺱ ﺍﻟﺸﺎﺌﻊ ﻟﻠﺯﻭﺠﺔ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴﺔ ﻴﻜـﻭﻥ ﺴـﻨﺘﻰ‬ ‫ﺴﺘﻭﻙ )١/٠٠١ ﺴﺘﻭﻙ( ﺤﻴﺙ ﺃﻥ‬ ‫‪Centistoke = mm٢/sec‬‬ ‫‪Centistoke × ١٠-٦ = m٢/sec‬‬ ‫ﻭﺘﻌﺘﻤﺩ ﺍﻟﻠﺯﻭﺠﺔ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﻭﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ، ﻋﻠـﻰ‬ ‫ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻟﺯﻭﺠﺔ ﺍﻟﻤـﺎﺀ ﺘﺴـﺎﻭﻯ ٣١١٠,٠ ﺒـﻭﻴﺯ ﻋﻨـﺩ‬ ‫٦,٥١‪º‬ﻡ ﻭﻓﻲ ﺍﻟﻨﻅﺎﻡ ﺍﻟﻤﺘﺭﻯ ﻟﻠﻭﺤﺩﺍﺕ )ﺴﻡ.ﺠﻡ.ﺜﺎﻨﻴﺔ( ﺘﻜـﻭﻥ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴﺔ ﺒﺎﻟﺴﻨﺘﻰ ﺴﺘﻭﻙ = ﺍﻟﻠﺯﻭﺠﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﺃﻭ‬ ‫ﺍﻟﻤﻁﻠﻘﺔ ﺒﺎﻟﺴﻨﺘﻰ ﺒﻭﻴﺯ/‪ Sp.gr‬ﻭﺍﻟﺘﺤﻭﻴل ﻤﻥ ﺍﻟﻭﺤﺩﺍﺕ ﺍﻟﻤﺘﺭﻴﺔ‬ ‫ﺇﻟﻰ ﺍﻟﻭﺤﺩﺍﺕ ﺍﻹﻨﺠﻠﻴﺯﻴﺔ )ﻗـﺩﻡ – ﺭﻁـل – ﺜﺎﻨﻴـﺔ( ﻴﻜـﻭﻥ‬ ‫ﺭﻁل.ﺜﺎﻨﻴﺔ/ﻗﺩﻡ٢ = ٥٥٨٨٠٢٠٠٠٠,٠ ﺴﻨﺘﻰ ﺒﻭﻴﺯ.‬ ‫ﻗﺩﻡ٢/ﺜﺎﻨﻴﺔ = ٩٣٦٧٠١,٠ ﺴﻨﺘﻰ ﺴﺘﻭﻙ.‬ ‫- ٤١ -‬
‫ﻭﺍﻟﻤﺎﺌﻊ ﺍﻟﻤﺜﺎﻟﻰ ﻫﻭ ﺍﻟﻤﺎﺌﻊ ﺍﻟﺫﻯ ﻨﻌﺘﺒﺭﻩ ﺨﺎل ﻤﻥ ﺍﻟﻠﺯﻭﺠـﺔ‬ ‫ﻭﺘﺴﻬﻴﻼ ﻟﺩﺭﺍﺴﺔ ﺍﻟﻤﻌﺎﺩﻻﺕ ﻨﻌﺘﺒﺭ ﺍﻟﻤﺎﺌﻊ ﻤﺜﺎﻟﻴﺎ ﺒﺈﻫﻤﺎل ﺘـﺄﺜﻴﺭ‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﺜﻡ ﺇﺩﺨﺎل ﻤﻌﺎﻤﻼﺕ ﺍﻟﺘﺼﺤﻴﺢ ﺍﻟﺘﻲ ﻴـﺘﻡ ﺍﻟﺤﺼـﻭل‬ ‫ﻋﻠﻴﻬﺎ ﻤﻥ ﺍﻟﺘﺠﺎﺭﺏ ﺍﻟﻤﻌﻤﻠﻴﺔ.‬ ‫ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ )‪:(Continuity Equation‬‬ ‫ﺸﻜل )٤(‬ ‫- ٥١ -‬
‫ﺘﺭﺒﻁ ﻫﺫﻩ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺒﻴﻥ ﺍﻟﺴﺭﻋﺔ ﺍﻟﻤﺘﻭﺴـﻁﺔ ‪ V‬ﺍﻟﻌﻤﻭﺩﻴـﺔ‬ ‫ﻋﺒﺭ ﻤﻘﻁﻊ ﻓﻲ ﺃﻨﺒﻭﺒﺔ ﻭﺒﻴﻥ ﺍﻟﻤﺴﺎﺤﺔ ‪ A‬ﻟﻬﺫﺍ ﺍﻟﻤﻘﻁـﻊ ﻭﻜﻤـﺎ‬ ‫ﻴﺘﻀﺢ ﻤﻥ ﺸﻜل )٤( ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )١( ﺇﺫﺍ ﻜﺎﻨﺕ ﺍﻟﻤﺴﺎﺤﺔ ١‪A‬‬ ‫ﻭﺍﻟﺴﺭﻋﺔ ١‪ V‬ﻭﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺌﻊ ١‪ ρ‬ﺘﻜﻭﻥ ﻜﺘﻠﺔ ﺍﻟﻤﺎﺌﻊ ﺍﻟﻤﺎﺭ ﻓـﻲ‬ ‫ﺍﻟﺜﺎﻨﻴﺔ ﺍﻟﻭﺍﺤﺩﺓ ﺨﻼل ﻫﺫﺍ ﺍﻟﻤﻘﻁﻊ ﻫﻰ ١‪ ρ١A١V‬ﻓﻠـﻭ ﺘﻐﻴـﺭ‬ ‫ﺍﻟﻤﻘﻁﻊ ﺇﻟﻰ )٢( ﻭﻜﺎﻨﺕ ﻤﺴﺎﺤﺘﻪ ٢‪ A‬ﻓﻼﺒﺩ ﺃﻥ ﻴﺤﺩﺙ ﺘﻐﻴﺭ ﻓﻲ‬ ‫ﻗﻴﻡ ٢‪ ρ٢,V‬ﻟﺘﻅل ﺍﻟﻜﺘﻠﺔ ﺜﺎﺒﺘﺔ ﻭﻓﻲ ﺤﺎﻟﺔ ﺍﻟﻤﻭﺍﺌﻊ ﺍﻟﻐﻴﺭ ﻗﺎﺒﻠـﺔ‬ ‫ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل ﻟﻡ ﺘﺘﻐﻴﺭ ﺍﻟﻜﺜﺎﻓﺔ ﺃﻯ ﺘﻅل ﺜﺎﺒﺘﺔ ﺃﻯ ﺃﻥ‬ ‫ﻤﻘﺩﺍﺭ ﺜﺎﺒﺕ = ٢‪A١V١=A٢V‬‬ ‫ﻭﻴﻁﻠﻕ ﻋﻠﻰ ﻫﺫﺍ ﺍﻟﻤﻘﺩﺍﺭ ﺍﻟﺜﺎﺒﺕ ﺇﺴﻡ ﻤﻌـﺩل ﺍﻟﺴـﺭﻴﺎﻥ ﺃﻭ‬ ‫ﺍﻟﻜﻤﻴﺔ )‪ (Flow Rate‬ﻭﻴﺭﻤﺯ ﻟﻪ ﺒﺎﻟﺭﻤﺯ ‪ Q‬ﻭﻴﻌـﺭﻑ ﺒﺄﻨـﻪ‬ ‫ﺤﺠﻡ ﺍﻟﺴﺎﺌل ﺍﻟﻤﺎﺭ ﻓﻲ ﻭﺤﺩﺓ ﺍﻟﺯﻤﻥ ﻭﻭﺤﺩﺘﻪ ﻫﻰ ﻤﺘﺭ٣/ﺴﺎﻋﺔ.‬ ‫ﺍﻟﻁﺎﻗﺔ )‪:(Energy‬‬ ‫ﺘﻜﻭﻥ ﻁﺎﻗﺔ ﺍﻟﻤﻭﺍﺌﻊ ﺍﻟﻐﻴﺭ ﻗﺎﺒﻠﺔ ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل ﻓﻲ‬ ‫ﺜﻼﺙ ﺼﻭﺭ ﻫﻰ ﺴﺭﻋﺔ، ﻀﻐﻁ ﻭﺇﺭﺘﻔﺎﻉ ﻭﻴﺘﻡ ﺍﻟﺘﻌﺒﻴﺭ ﻋﻨﻬﺎ ﻓﻲ‬ ‫ﺼﻭﺭﺓ ﻁﺎﻗﺔ ﻟﻭﺤﺩﺓ ﺍﻷﻭﺯﺍﻥ ﻭﻭﺤﺩﺘﻬﺎ ﻫﻰ ﻜﺠﻡ.ﻤﺘﺭ/ﻜﺠـﻡ ﺃﻭ‬ ‫ﺍﻟﻤﺘﺭ ﻋﻴﺎﺭﻯ ﺃﻭ ﻤﻁﻠﻕ.‬ ‫- ٦١ -‬
‫ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ )‪:(Velocity Head‬‬ ‫2‪V‬‬ ‫( ﻭﻭﺤـﺩﺘﻬﺎ ﻫـﻰ‬ ‫ﻭﻴﻌﺒﺭ ﻋﻨﻬﺎ ﻓﻲ ﺼﻭﺭﺓ ﺴـﺭﻋﺔ )‬ ‫‪2g‬‬ ‫ﻜﺠﻡ.ﻤﺘﺭ/ﻜﺠﻡ ﺃﻯ ﺍﻟﻤﺘﺭ ﻭﺴـﺭﻋﺔ ﺍﻟﺴـﻭﺍﺌل ﻓـﻲ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫ﻭﺍﻟﻘﻨﻭﺍﺕ ﺍﻟﻤﻔﺘﻭﺤﺔ ﺘﺘﻐﻴﺭ ﻋﺒﺭ ﺃﻯ ﻤﻘﻁﻊ ﻭﺍﺤﺩ ﻤﻥ ﺍﻟﻤﺠـﺭﻯ‬ ‫ﻭﻟﺫﻟﻙ ﻓﺈﻨﻪ ﻤﻥ ﺍﻟﺩﻗﺔ ﺍﻟﻜﺎﻓﻴﺔ ﺃﻥ ﻨﺴﺘﺨﺩﻡ ﺍﻟﺴﺭﻋﺔ ﺍﻟﻤﺘﻭﺴﻁﺔ ‪V‬‬ ‫ﺍﻟﻤﺤﺴﻭﺒﺔ ﺒﻘﺴﻤﺔ ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ ﻋﻠﻰ ﻤﺴﺎﺤﺔ ﻤﻘﻁﻊ ﺍﻟﻤﺠﺭﻯ.‬ ‫ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ )‪:(Pressure Head‬‬ ‫‪10 4 P‬‬ ‫ﻭﻭﺤﺩﺘﻬﺎ‬ ‫ﻭﻴﻌﺒﺭ ﻋﻨﻬﺎ ﻓﻲ ﺼﻭﺭﺓ ‪ Head‬ﻭﺘﺴﺎﻭﻯ‬ ‫‪w‬‬ ‫ﺍﻟﻤﺘﺭ ﺤﻴﺙ ﺃﻥ ‪ P‬ﺍﻟﻀﻐﻁ ﺒﺎﻟﻜﺠﻡ/ﺴﻡ٢، ‪ w‬ﺍﻟـﻭﺯﻥ ﺍﻟﻨـﻭﻋﻰ‬ ‫ﻟﻠﺴﺎﺌل ﺒﺎﻟﻜﺠﻡ/ﻤﺘﺭ٣.‬ ‫ﻁﺎﻗﺔ ﺍﻟﻭﻀﻊ )‪:(Elevation Head‬‬ ‫ﻭﻴﻌﺒﺭ ﻋﻨﻬﺎ ﺒﺎﻹﺭﺘﻔﺎﻉ ‪ Z‬ﻋـﻥ ﻤﺴـﺘﻭﻯ ﻗﻴﺎﺴـﻲ ﻤﻌـﻴﻥ‬ ‫‪ Datum Plane‬ﻭﻋﺎﺩﺓ ﻴﻜﻭﻥ ﻤﺴﺘﻭﻯ ﺴﻁﺢ ﺍﻟﺒﺤﺭ ﻭﻭﺤﺩﺘﻬﺎ‬ ‫ﺍﻟﻤﺘﺭ.‬ ‫- ٧١ -‬
‫ﻨﻅﺭﻴﺔ ﺒﺭﻨﻭﻟﻠﻰ )‪:(Bernoulli's Equation‬‬ ‫ﻨﻅﺭﻴﺔ ﺒﺭﻨﻭﻟﻠﻰ ﻟﻠﻤﻭﺍﺌﻊ ﺍﻟﻐﻴﺭ ﻗﺎﺒﻠﺔ ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل‬ ‫ﺘﻨﺹ ﻋﻠﻰ ﺃﻨﻪ ﻓﻲ ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻤﺴﺘﻘﺭ ‪ Steady Flow‬ﺒـﺩﻭﻥ‬ ‫ﻓﻭﺍﻗﺩ )ﻤﺎﺌﻊ ﻤﺜﺎﻟﻰ( "ﺍﻟﻁﺎﻗﺔ ﻋﻨﺩ ﺃﻯ ﻨﻘﻁﺔ ﺘﺴـﺎﻭﻯ ﻤﺠﻤـﻭﻉ‬ ‫ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ ﻭﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ﻭﻁﺎﻗﺔ ﺍﻟﻭﻀـﻊ ﻭﻴﻜـﻭﻥ ﻫـﺫﺍ‬ ‫ﺍﻟﻤﺠﻤﻭﻉ ﺜﺎﺒﺕ ﻋﻠﻰ ﻁﻭل ﺨﻁ ﺍﻟﺴﺭﻴﺎﻥ ﻓﻲ ﺍﻟﻤﺠﺭﻯ" ﻭﻫـﺫﻩ‬ ‫ﺍﻟﻁﺎﻗﺔ ﺘﺴﺎﻭﻯ‬ ‫4‬ ‫2‬ ‫‪10 P V‬‬ ‫=‪H‬‬ ‫+‬ ‫‪+z‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﻭﻋﻨﺩ ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻤﺴﺘﻘﺭ ﻟﻠﻤﺎﺌﻊ ﺍﻟﻤﺜﺎﻟﻰ ﻴﻤﻜـﻥ ﻟﻠﻁﺎﻗـﺔ ﺃﻥ‬ ‫ﺘﺘﻐﻴﺭ ﻤﻥ ﺼﻭﺭﺓ ﻷﺨﺭﻯ ﻓﺈﺫﺍ ﺯﺍﺩﺕ ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ ﺇﻨﺨﻔﻀـﺕ‬ ‫ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ﺃﻭ ﻁﺎﻗﺔ ﺍﻟﻭﻀﻊ ﻭﺴﻭﻑ ﻨﻭﻀﺢ ﺘﻁﺒﻴﻘﺎﺕ ﻨﻅﺭﻴﺔ‬ ‫ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺒﻌﺽ ﺤﺎﻻﺕ ﺍﻟﺴﺭﻴﺎﻥ ﻓﻲ ﺃﺠﻬﺯﺓ ﻗﻴﺎﺱ ﻤﻌـﺩل‬ ‫ﺍﻟﺴﺭﻴﺎﻥ )ﺍﻟﻜﻤﻴﺔ(.‬ ‫- ٨١ -‬
‫١- ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ )‪:(Orifice Meter‬‬ ‫ﺸﻜل )٥(‬ ‫- ٩١ -‬
‫ﻴﺘﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻤﻘﻴﺎﺱ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ D‬ﻴﻜـﻭﻥ‬ ‫ﺃﻜﺒﺭ ﻤﻥ ٥ﺴﻡ ﻭﻤﺭﻜﺏ ﺒﻬﺎ ﻗﺭﺹ ﺒﻪ ﻓﺘﺤﺔ ﻗﻁﺭﻫﺎ ‪ d‬ﺃﺼـﻐﺭ‬ ‫ﻤﻥ ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒﺔ ﻭﻻ ﻴﻘل ﻋﻥ ٦ﻤﻡ ﻜﻤﺎ ﺒﺎﻟﺸﻜل )٥( ﺒﺤﻴـﺙ‬ ‫ﻓﻲ ﺤـﺩﻭﺩ ٢,٠ – ٨,٠ ﻭﻻ ﺘﺯﻴـﺩ‬ ‫ﺘﻜﻭﻥ ﻨﺴﺒﺔ ﺍﻷﻗﻁﺎﺭ‬ ‫‪d‬‬ ‫‪D‬‬ ‫2‬ ‫ﻨﺴﺒﺔ ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁﻊ ⎞ ⎛ ﻋـﻥ ٧,٠، ﺒﺘﻁﺒﻴـﻕ ﻤﻌﺎﺩﻟـﺔ‬ ‫‪d‬‬ ‫⎟ ⎜‬ ‫⎠‪⎝D‬‬ ‫ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺍﻟﻨﻘﻁﺘﻴﻥ )١(، )٢( ﻭﺇﻋﺘﺒﺎﺭ ﺍﻟﻤﺎﺌﻊ ﻤﺜﺎﻟﻴﺎ‬ ‫ﹰ‬ ‫ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ)١(= ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ)٢(= ﺜﺎﺒﺕ‬ ‫2‪10 4 P‬‬ ‫22‪V‬‬ ‫21‪10 4 P1 V‬‬ ‫+‬ ‫= 2‪+ Z‬‬ ‫+‬ ‫1‪+ Z‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﻤﻊ ﺃﺨﺫ ﺍﻟﻤﺴﺘﻭﻯ ﺍﻟﻘﻴﺎﺴﻰ ﻫﻭ ﻤﺤـﻭﺭ ﺍﻷﻨﺒﻭﺒـﺔ ﻭﺇﻫﻤـﺎل‬ ‫ﺍﻟﺴﺭﻋﺔ ١‪ V‬ﺒﺈﻋﺘﺒﺎﺭﻫﺎ ﺃﻗل ﺒﻜﺜﻴﺭ ﻤﻥ ٢‪V‬‬ ‫) 2 ‪V22 10 4 ( p1 − p‬‬ ‫=‬ ‫‪= H1 − H 2 = h‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪V 2 = 2 gh‬‬ ‫ﻭﺇﺫﺍ ﺘﻜﻠﻤﻨﺎ ﻋﻥ ﺘﺄﺜﻴﺭ ﺍﻟﻠﺯﻭﺠﺔ ﻴﺘﺒﻴﻥ ﺃﻨﻪ ﻋﻨﺩ ﺴﺭﻴﺎﻥ ﺍﻟﻤﺎﺌﻊ‬ ‫ﻴﻀﻴﻊ ﺠﺯﺀ ﻤﻥ ﺍﻟﻁﺎﻗﺔ ﻋﻥ ﻁﺭﻴﻕ ﺍﻹﺤﺘﻜـﺎﻙ ﺍﻟﻨﺎﺸـﺊ ﻤـﻥ‬ ‫ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺃﻯ ﺃﻨﻪ ﺇﺫﺍ ﺘﻡ ﻗﻴﺎﺱ ﺍﻟﺴﺭﻋﺔ ٢‪ V‬ﻟﻭﺠﺩﻨﺎ ﺃﻨﻬـﺎ‬ ‫ﻷﻥ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ )٢( ﺘﻜﻭﻥ ﺃﻗـل‬ ‫ﺃﻗل ﻤﻥ ‪2 gh‬‬ ‫- ٠٢ -‬
‫ﻤﻥ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ )١( ﻨﺘﻴﺠﺔ ﻓﻘﺩ ﺠﺯﺀ ﻤﻨﻬﺎ ﺒﺈﺤﺘﻜﺎﻙ‬ ‫ﺍﻟﻤﺎﺌﻊ ﻤﻊ ﺠﺩﺭﺍﻥ ﺍﻟﻤﻘﻴﺎﺱ ﻋﻨﺩ ﺨﺭﻭﺠﻪ ﻤﻥ ﺍﻟﻔﺘﺤـﺔ، ﺤﻴـﺙ‬ ‫ﻴﻨﺘﻘل ﺍﻟﺴﺎﺌل ﻤﻥ ﻨﻘﻁﺔ ﺇﻟﻰ ﺃﺨﺭﻯ ﻨﺘﻴﺠﺔ ﻓﺭﻕ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴـﺔ‬ ‫ﺒﻴﻥ ﺍﻟﻨﻘﻁﺘﻴﻥ‬ ‫ﻭﺒﺫﻟﻙ ﺘﻜﻭﻥ ﺍﻟﺴﺭﻋﺔ ٢‪ V‬ﺘﺴﺎﻭﻯ ‪ K V 2 gh‬ﺤﻴـﺙ ‪Kv‬‬ ‫ﻴﺴﻤﻰ ﻤﻌﺎﻤل ﺍﻟﺴﺭﻋﺔ ﻭﻫﻭ ﺃﻗل ﻤﻥ ١ ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻤﻌـﺩل‬ ‫ﺍﻟﺴﺭﻴﺎﻥ )ﺍﻟﻜﻤﻴﺔ( ‪ Q‬ﺍﻟﻤﺎﺭ ﺨﻼل ﺍﻟﻔﺘﺤﺔ ﻤﻥ ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ‬ ‫٢‪ Q = A٢V‬ﺤﻴﺙ ﺃﻥ ﺍﻟﺴﺭﻋﺔ ﺘﻜﻭﻥ ﻋﻤﻭﺩﻴﺔ ﻋﻠﻰ ﺍﻟﻤﺴـﺎﺤﺔ‬ ‫ﻋﻨﺩ ﺍﻹﻨﻜﻤﺎﺵ ﺃﻯ ﻋﻨﺩ ﺍﻟﻨﻘﻁـﺔ )٢( ﻭﻟـﻴﺱ ﻋﻨـﺩ ﺍﻟﻔﺘﺤـﺔ‬ ‫‪ Orifice‬ﺫﺍﺘﻬﺎ ﻭﺒﺫﻟﻙ ﺘﻜﻭﻥ ﻤﺴﺎﺤﺔ ﻤﻘﻁﻊ ﺍﻹﻨﻜﻤﺎﺵ ٢‪ A‬ﺃﻗل‬ ‫‪π‬‬ ‫ﻤﻥ ﻤﺴﺎﺤﺔ ﻤﻘﻁﻊ ﺍﻟﻔﺘﺤﺔ ﻨﻔﺴﻬﺎ 2 ‪d‬‬ ‫4‬ ‫‪π‬‬ ‫‪A2 = K C‬‬ ‫2‪d‬‬ ‫4‬ ‫ﺤﻴﺙ ﺃﻥ ‪ Kc‬ﻴﺴﻤﻰ ﻤﻌﺎﻤل ﺇﻨﻜﻤﺎﺵ ﻤﻘﻁﻊ ﺍﻟﺴﺭﻴﺎﻥ ﻭﻫـﻭ‬ ‫ﺃﻗل ﻤﻥ ١ ﻭﺒﺫﻟﻙ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ ﺨﻼل ﺍﻟﻔﺘﺤﺔ ﺘﺴﺎﻭﻯ‬ ‫‪π‬‬ ‫‪π‬‬ ‫‪Q = KC‬‬ ‫‪d 2 K V 2 gh = K d‬‬ ‫‪d 2 2 gh‬‬ ‫4‬ ‫4‬ ‫)١(‬ ‫- ١٢ -‬
‫ﺤﻴﺙ ﺃﻥ ‪ Kd‬ﻫﻭ ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ﻭﻴﺴﺎﻭﻯ ‪ KvKc‬ﻭﻴﻜﻭﻥ‬ ‫ﺃﻗل ﻤﻥ ١ ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻗﻴﻤﺔ ﻫﺫﺍ ﺍﻟﻤﻌﺎﻤل ﻤـﻥ ﺍﻟﺘﺠـﺎﺭﺏ‬ ‫ﺍﻟﻤﻌﻤﻠﻴﺔ ﻭﻟﺘﺴﻬﻴل ﺍﻟﺤﺴﺎﺒﺎﺕ ﻴﻤﻜﻥ ﺇﻋﺘﺒﺎﺭ ﺍﻟﻘﻴﻤﺔ ﺍﻟﺘﻘﺭﻴﺒﻴﺔ ﻟﻬﺫﺍ‬ ‫ﺍﻟﻤﻌﺎﻤل ﺘﺴﺎﻭﻯ ٦٩٥,٠، ﻭﺒﻬﺫﻩ ﺍﻟﻁﺭﻴﻘﺔ ﻴﺘﻡ ﻗﻴـﺎﺱ ﺍﻟﻜﻤﻴـﺔ‬ ‫ﺒﻤﻌﺭﻓﺔ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺒﻴﻥ ﻗﺒل ﻭﺒﻌﺩ ﺍﻟﻔﺘﺤﺔ ﻭﻴﺘـﺭﺍﻭﺡ ﻀـﻐﻁ‬ ‫ﺍﻟﻨﻔﺙ ‪ Jet‬ﺍﻟﺨﺎﺭﺝ ﻤﻥ ﺍﻟﻔﺘﺤﺔ ﺒﻴﻥ ﺃﻗل ﻗﻴﻤﺔ ﻟﻪ ﻋﻨﺩ ﺍﻹﻨﻜﻤﺎﺵ‬ ‫ﻭﺃﻗﺼﻰ ﻗﻴﻤﺔ ﻟﻪ ﺒﻌﺩ ﺤﻭﺍﻟﻰ ٤ ﺃﻭ ٥ ﺃﻤﺜﺎل ﺍﻟﻘﻁـﺭ ‪ D‬ﺒﻌـﺩ‬ ‫ﺍﻟﻔﺘﺤﺔ ﻓﻲ ﺇﺘﺠﺎﻩ ﺍﻟﺴﺭﻴﺎﻥ.‬ ‫ﻭﺍﻟﻌﻴﺏ ﺍﻷﺴﺎﺴﻰ ﻟﻠﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ ﺒﺎﻟﻤﻘﺎﺭﻨﺔ ﺒﺎﻟﻤﻘﻴﺎﺱ ﺫﻭ‬ ‫ﺍﻟﻔﻭﻫﺔ ﺃﻭ ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﻫﻭ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ ﻜﺒﻴـﺭ ﻭﻤـﻥ‬ ‫ﻨﺎﺤﻴﺔ ﺃﺨﺭﻯ ﻓﺈﻨﻪ ﻏﻴﺭ ﻤﺭﺘﻔﻊ ﺍﻟﺜﻤﻥ ﻭﺒﺈﻤﻜﺎﻨﻪ ﻗﻴـﺎﺱ ﺍﻟﻜﻤﻴـﺔ‬ ‫ﺒﺩﻗﺔ، ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻟﺤﺴﺎﺏ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘـﺎﺱ ﻋﺒـﺭ‬ ‫ﺍﻟﻔﺘﺤﺔ ‪ Orifice‬ﻟﺨﻁ ﺃﻨﺎﺒﻴﺏ ﻗﻁﺭﻩ ٢١ ﺒﻭﺼﺔ ﻭﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ‬ ‫ﺤﻭﺍﻟﻰ ٠٠٤ ﻤﺘﺭ ﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ :‬ ‫ﻨﻔﺘﺭﺽ ﺃﻥ ﻗﻁﺭ ﺍﻟﻔﺘﺤﺔ ﻴﺴﺎﻭﻯ ٥٧٦,٠ ﻗﻁـﺭ ﺍﻟﺨـﻁ ﺃﻯ‬ ‫ﻴﺴﺎﻭﻯ ٨ ﺒﻭﺼﺔ، ﺒﺘﻁﺒﻴﻕ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺭﻗﻡ )١( ﻭﺇﻋﺘﺒـﺎﺭ = ‪Kd‬‬ ‫‪π‬‬ ‫‪Q = Kd‬‬ ‫‪d 2 2 gh‬‬ ‫٦٩٥,٠‬ ‫4‬ ‫- ٢٢ -‬
‫⎞ 45.2 × 8 ⎛ ‪π‬‬ ‫2‬ ‫٦٨٦,١ = ‪2 × 9.8h , h‬‬ ‫004‬ ‫⎜ 695.0 =‬ ‫⎟‬ ‫0063‬ ‫⎠ 001 ⎝ 4‬ ‫‪mt‬‬ ‫ﻭﺒﻔﺭﺽ ﺃﻥ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺯﻴﺕ ﻜﺜﺎﻓﺘﻪ ٢٨٨,٠ ﺠﻡ/ ﺴﻡ٣‬ ‫ﻴﻜﻭﻥ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘﺎﺱ ﻋﺒﺭ ﺍﻟﻔﺘﺤﺔ ﻴﺴﺎﻭﻯ‬ ‫288.0‬ ‫× 686.1 = ‪∆P‬‬ ‫2 ‪= 0.148 kg / cm‬‬ ‫01‬ ‫ﻭﻋﻨﺩ ﺇﺨﺘﻴﺎﺭ ﻤﻘﻴﺎﺱ ﺍﻟﻔﺘﺤﺔ ﻴﺠﺏ ﻤﺭﺍﻋﺎﺓ ﺍﻟﺤـﺩ ﺍﻷﻗﺼـﻰ‬ ‫ﻟﻠﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻟﻠﻀﻐﻁ ﻋﺒﺭ ﺍﻟﻤﻘﻴﺎﺱ ‪ Head loss‬ﺤﻴﺙ ﻴﺠﺏ ﺃﻥ‬ ‫ﻴﻜﻭﻥ ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻟﻠﻀﻐﻁ ﺃﻗل ﻤﺎ ﻴﻤﻜﻥ ﻭﻴﻨﺒﻐﻰ ﺃﻻ ﺘﺼل ﻗﻴﻤﺔ‬ ‫ﻫﺫﺍ ﺍﻟﻔﺎﻗﺩ ﺇﻟﻰ ٥٢,٠ ﻜﺠﻡ/ﺴﻡ٢ ﺒﺄﻯ ﺤﺎل ﻤـﻥ ﺍﻷﺤـﻭﺍل ﻷﻥ‬ ‫ﻫﺫﺍ ﻤﻌﻨﺎﻩ ﺤﺩﻭﺙ ﻓﻘﺩ ﻜﺒﻴﺭ ﻨﺴﺒﻴﺎ ﻓﻲ ﻁﺎﻗﺔ ﺍﻟﺴﺎﺌل ﻤﻘﺎﺒل ﻗﻴﺎﺱ‬ ‫ﹰ‬ ‫ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ.‬ ‫ﻤﻠﺤﻭﻅﺔ: ﻴﻤﻜﻥ ﺘﻁﺒﻴﻕ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺭﻗﻡ )١( ﻓﻲ ﺤﺎﻟﺔ ﻗﻴـﺎﺱ‬ ‫ﺍﻟﻜﻤﻴﺔ ﻟﻠﻤﻭﺍﺌﻊ ﺍﻟﻘﺎﺒﻠﺔ ﻟﻼﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﻐﺎﺯﺍﺕ ﺒﺸﺭﻁ ﺃﻻ ﺘﺯﻴﺩ‬ ‫ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﺍﻟﻐﺎﺯ ﻋﻥ ٠٠١ ﻤﺘﺭ ﻓﻲ ﺍﻟﺜﺎﻨﻴﺔ ﺤﻴﺙ ﺃﻨﻪ ﻋﻨـﺩ‬ ‫ﻫﺫﻩ ﺍﻟﺴﺭﻋﺔ ﺘﺘﻐﻴﺭ ﻜﺜﺎﻓﺔ ﺍﻟﻐﺎﺯ ﺘﻐﻴﺭ ﻁﻔﻴﻑ ﺠﺩﺍ ﺃﻯ ﺃﻨﻪ ﻴﻤﻜﻥ‬ ‫ﹰ‬ ‫ﺇﻫﻤﺎل ﺘﺄﺜﻴﺭ ﺇﻨﻀﻐﺎﻁﻴﺔ ﺍﻟﻐﺎﺯ ﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻭﺇﻋﺘﺒﺎﺭ ﺍﻟﻐـﺎﺯ‬ ‫ﻜﻤﺎﺌﻊ ﻏﻴﺭ ﻗﺎﺒل ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل.‬ ‫- ٣٢ -‬
‫ﺸﻜل )٦(‬ ‫- ٤٢ -‬
‫٢- ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﻭﻫﺔ)‪:(Flow-Nozzle Meter‬‬ ‫ﻴﺘﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻤﻘﻴﺎﺱ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ D‬ﻴﻜـﻭﻥ‬ ‫ﺃﻜﺒﺭ ﻤﻥ ٥ﺴﻡ ﻭﻤﺭﻜﺏ ﺩﺍﺨﻠﻬﺎ ﺃﻨﺒﻭﺒﺔ ﻗﺼﻴﺭﺓ ﻤﺘﻐﻴﺭﺓ ﺍﻟﻤﻘﻁـﻊ‬ ‫ﺒﺈﻨﺘﻅﺎﻡ ﻭﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ d‬ﻜﻤﺎ ﺒﺎﻟﺸﻜل )٦( ﺒﺤﻴﺙ ﺘﻜﻭﻥ ﻨﺴﺒﺔ‬ ‫2‬ ‫⎞ ⎛ ﻓﻲ ﺤﺩﻭﺩ ٢,٠ ﺇﻟﻰ ٥٥,٠، ﺒﺘﻁﺒﻴـﻕ‬ ‫ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁﻊ‬ ‫‪d‬‬ ‫⎟ ⎜‬ ‫⎠‪⎝D‬‬ ‫ﻤﻌﺎﺩﻟﺔ ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺍﻟﻨﻘﻁﺘﻴﻥ )١(، )٢( ﻤﻊ ﻭﻀـﻊ ﺘـﺄﺜﻴﺭ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﻓﻲ ﺍﻹﻋﺘﺒﺎﺭ.‬ ‫21‪10 4 P1 V‬‬ ‫22‪10 4 P2 V‬‬ ‫+‬ ‫= 1‪+ Z‬‬ ‫+‬ ‫‪+ Z2 + hf‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ hf‬ﻫﻭ ﺍﻟﻔﺎﻗﺩ ﺒﺎﻹﺤﺘﻜﺎﻙ ﺒﻴﻥ ﺍﻟﻨﻘﻁﺘـﻴﻥ )١(، )٢(‬ ‫ﻤـﻊ ﺇﻋﺘﺒـﺎﺭ ﺍﻟﻤﺴـﺘﻭﻯ ﺍﻟﻘﻴﺎﺴـﻰ ﻫـﻭ ﻤﺤـﻭﺭ ﺍﻷﻨﺒﻭﺒـﺔ‬ ‫ـ‬ ‫ـ‬ ‫ـ ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫22‪10 4 P1 V12 10 4 P2 V‬‬ ‫+‬ ‫=‬ ‫+‬ ‫‪+ hf‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﺒﺈﺴﺘﺨﺩﺍﻡ ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ ٢‪ A١V١=A٢V‬ﻭﺇﺩﺨﺎل ﻤﻌﺎﻤل‬ ‫ﺍﻟﺴﺭﻋﺔ ‪ KV‬ﻟﻴﺤل ﻤﺤل ﺍﻟﻔﺎﻗﺩ ﺒﺎﻻﺤﺘﻜﺎﻙ ‪hf‬‬ ‫) ‪10 4 P1 (V2 / K V‬‬ ‫) ‪10 4 P2 (V2 / K V‬‬ ‫2‬ ‫2‪⎛ A‬‬ ‫⎞‬ ‫2‬ ‫2‬ ‫+‬ ‫⎜‬ ‫‪⎜A‬‬ ‫= ⎟‬ ‫⎟‬ ‫+‬ ‫‪w‬‬ ‫‪2g‬‬ ‫1 ⎝‬ ‫⎠‬ ‫‪w‬‬ ‫‪2g‬‬ ‫- ٥٢ -‬
‫) 2‪10 4 (P1 − P‬‬ ‫⎤ ⎞ 2‪V22 ⎡ ⎛ A‬‬ ‫2‬ ‫=‬ ‫‪⎢1 − ⎜ ⎟ ⎥ = H 1 − H 2 = h‬‬ ‫⎥ ⎠ 1‪2 gK v2 ⎢ ⎜ A‬‬ ‫⎟‬ ‫⎝ ⎣‬ ‫‪w‬‬ ‫⎦‬ ‫‪2 gh‬‬ ‫‪V2 = K v‬‬ ‫‪⎡ ⎛A‬‬ ‫⎞‬ ‫2‬ ‫⎤‬ ‫2 ⎜ − 1⎢‬ ‫⎜‬ ‫⎟‬ ‫⎟‬ ‫⎥‬ ‫1‪⎢ ⎝ A‬‬ ‫⎣‬ ‫⎠‬ ‫⎥‬ ‫⎦‬ ‫ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ )ﺍﻟﻜﻤﻴﺔ( ‪ Q‬ﺍﻟﻤـﺎﺭ ﺨـﻼل‬ ‫ﺍﻟﻔﻭﻫﺔ ﻤﻥ ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ‬ ‫‪π‬‬ ‫= 2‪Q = A2V‬‬ ‫2 ‪d 2V‬‬ ‫4‬ ‫‪π‬‬ ‫‪2 gh‬‬ ‫. ‪= Kd‬‬ ‫2‪d‬‬ ‫4‬ ‫⎤ 4⎞ ‪⎡ ⎛ d‬‬ ‫⎥ ⎟ ⎜ − 1⎢‬ ‫⎥ ⎠‪⎢ ⎝D‬‬ ‫⎣‬ ‫⎦‬ ‫ﺤﻴﺙ ﺃﻥ ‪ Kd=KV‬ﻭﻫﻭ ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ﻭﻴﻜﻭﻥ ﺃﻗل ﻤﻥ‬ ‫١ ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻗﻴﻤﺔ ﻫﺫﺍ ﺍﻟﻤﻌﺎﻤل ﻤﻥ ﺍﻟﺘﺠﺎﺭﺏ ﺍﻟﻤﻌﻤﻠﻴﺔ ﻭﻓﻲ‬ ‫ﻤﻌﻅﻡ ﺍﻷﺤﻴﺎﻥ ﻟﺘﺴﻬﻴل ﺍﻟﺤﺴﺎﺒﺎﺕ ﻴﻤﻜﻥ ﺇﻋﺘﺒﺎﺭ ﺍﻟﻘﻴﻤﺔ ﺍﻟﺘﻘﺭﻴﺒﻴﺔ‬ ‫ﻟﻬﺫﺍ ﺍﻟﻤﻌﺎﻤل ﺘﺘـﺭﺍﻭﺡ ﺒـﻴﻥ ٥٣٩,٠ ﻟﻸﻗﻁـﺎﺭ ﻭﺍﻟﺴـﺭﻋﺎﺕ‬ ‫ﺍﻟﺼﻐﻴﺭﺓ ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )٢( ﺇﻟﻰ ٨٨٩,٠ ﻟﻸﻗﻁﺎﺭ ﻭﺍﻟﺴـﺭﻋﺎﺕ‬ ‫ﺍﻟﻜﺒﻴﺭﺓ ﻨﺴﺒﻴﺎ ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )٢( ﻭﺒﻬﺫﻩ ﺍﻟﻁﺭﻴﻘﺔ ﻴﻤﻜـﻥ ﻗﻴـﺎﺱ‬ ‫ﹰ‬ ‫ﺍﻟﻜﻤﻴﺔ ﺒﻤﻌﺭﻓﺔ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺒﻴﻥ ﻗﺒل ﻤﺩﺨل ﺍﻟﻔﻭﻫـﺔ ﻭﻋﻨـﺩ‬ ‫ﻤﺨﺭﺠﻬﺎ.‬ ‫- ٦٢ -‬
‫ﻭﺍﻟﺭﺴﻡ ﺒﺎﻟﺸﻜل )٦( ﻴﻭﻀﺢ ﺘﻐﻴﺭ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻤﻊ ﺍﻟﻁﻭل‬ ‫ﻟﻜﻤﻴﺔ ﻤﻌﻴﻨﺔ ﺨﻼل ﺍﻟﻔﻭﻫﺔ ﺒﺈﻋﺘﺒـﺎﺭ ﺃﻥ ﺍﻟﻤﺴـﺘﻭﻯ ﺍﻟﻘﻴﺎﺴـﻰ‬ ‫ﺍﻟﻤﻨﺎﺴﺏ ﻫﻭ ﻤﺤﻭﺭ ﺍﻟﻔﻭﻫﺔ ﻭﻨﺤﺩﺩ ﺍﻷﻁﻭﺍل ﻋﻠﻴﻪ ﺃﻤﺎ ﺍﻟﻤﺤـﻭﺭ‬ ‫ﺍﻟﺭﺃﺴﻰ ﻓﻴﻤﺜل ﺼﻭﺭ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻤﺨﺘﻠﻔﺔ ﻓﻌﻨﺩ ﺍﻟﻨﻘﻁـﺔ )١( ﻨﺒـﺩﺃ‬ ‫1‪10 4 P‬‬ ‫ﻭﻨﻀـﻴﻑ‬ ‫ﺒﺘﻭﻗﻴﻊ ﻤﺴﺎﻓﺔ ﺭﺃﺴﻴﺔ ﺘﻤﺜل ﻁﺎﻗﺔ ﺍﻟﻀـﻐﻁ‬ ‫‪w‬‬ ‫2‪V‬‬ ‫ﺇﻟﻴﻬﺎ ﻤﺴﺎﻓﺔ ﺃﺨﺭﻯ ﺘﻤﺜل ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ 1 ﻓﻨﺤﺼـل ﻋﻠـﻰ‬ ‫‪2g‬‬ ‫ﻨﻘﻁﺔ ﺘﻤﺜل ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ )١( ﻭﻨﻜـﺭﺭ ﺫﻟـﻙ ﻋﻨـﺩ‬ ‫ﺍﻟﻨﻘﻁﺔ )٢( ﻓﻨﺤﺼل ﻋﻠﻰ ﻨﻘﻁﺔ ﺃﺨﺭﻯ ﺘﻤﺜل ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ‬ ‫ﻨﻘﻁﺔ )٢( ﻭﻨﻜﺭﺭ ﻫﺫﻩ ﺍﻟﻌﻤﻠﻴﺔ ﻋﻨﺩ ﺃﻭﻀﺎﻉ ﻤﺨﺘﻠﻔﺔ ﻋﻠﻰ ﻁﻭل‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﻭﺫﻟﻙ ﺒﻤﻘﻴﺎﺱ ﺭﺴﻡ ﻤﻌﻴﻥ ﻭﺒﺘﻭﺼـﻴل ﻫـﺫﻩ ﺍﻟـﻨﻘﻁ‬ ‫ﻨﺤﺼل ﻋﻠﻰ ﺨﻁ ﻴﻤﺜل ﺘﻐﻴﺭ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴـﺔ ﺨـﻼل ﺍﻟﻔﻭﻫـﺔ‬ ‫ﻭﻴﻁﻠﻕ ﻋﻠﻴﻪ ﺇﻨﺤـﺩﺍﺭ ﺍﻟﻁﺎﻗـﺔ ‪(E.G) Energy Gradient‬‬ ‫ﻭﺘﻜﻭﻥ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻤﺨﺭﺝ ﺍﻟﻔﻭﻫﺔ ﺃﻗل ﻤﻨﻬﺎ ﻋﻨﺩ ﻤﺩﺨﻠﻬﺎ‬ ‫ﺒﻤﻘﺩﺍﺭ ‪ hf‬ﻭﺇﺫﺍ ﺘﻡ ﺘﻭﺼﻴل ﻨﻘﻁ ﺘﻭﻗﻴﻊ ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ﻨﺤﺼـل‬ ‫ﻋﻠﻰ ﺨﻁ ﻴﻤﺜل ﺘﻐﻴﺭ ﺍﻟﻀﻐﻁ ﺨﻼل ﺍﻟﻔﻭﻫـﺔ ﻭﻴﻁﻠـﻕ ﻋﻠﻴـﻪ‬ ‫ﺇﻨﺤﺩﺍﺭ ﺍﻟﻀﻐﻁ ‪ (H.G) Hydraulic Gradient‬ﻭﻴﺘﻀﺢ ﺃﻥ‬ ‫ﺇﻨﺤﺩﺍﺭ ﺍﻟﻀﻐﻁ ﻴﻨﺨﻔﺽ ﻋﻥ ﺇﻨﺤﺩﺍﺭ ﺍﻟﻁﺎﻗﺔ ﺒﻘﺩﺭ ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ‬ ‫- ٧٢ -‬
‫2‪V‬‬ ‫ﻋﻨﺩ ﻫﺫﻩ ﺍﻟﻨﻘﻁﺔ ﻭﻨﻼﺤﻅ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ﻋﺒﺭ ﺍﻟﻤﻘﻴـﺎﺱ‬ ‫‪2g‬‬ ‫ﻴﺴﺎﻭﻯ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ ﻋﺒﺭ ﺍﻟﻤﻘﻴﺎﺱ ﻭﺫﻟﻙ ﻟﺘﺴـﺎﻭﻯ ﺍﻟﺴـﺭﻋﺔ‬ ‫ﻭﻜﺫﻟﻙ ﻁﺎﻗﺔ ﺍﻟﻭﻀﻊ ﻋﻨﺩ ﻤﺩﺨل ﻭﻤﺨﺭﺝ ﺍﻟﻤﻘﻴـﺎﺱ ﻭﻴﺴـﺒﺏ‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﻭﻫﺔ ﻓﺎﻗﺩ ﻀﻐﻁ ﺃﻜﺒﺭ ﻤﻥ ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﻭﺃﻗل‬ ‫ﻤﻥ ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ.‬ ‫٣- ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ‪:Venturi Meter‬‬ ‫ﺸﻜل )٧(‬ ‫- ٨٢ -‬
‫ﻴﺘﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻤﻘﻴﺎﺱ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ D‬ﻴﻜـﻭﻥ‬ ‫ﺃﻜﺒﺭ ﻤﻥ ٥ ﺴﻡ ﻭﻴﻅل ﻴﺼﻐﺭ ﺤﺘﻰ ﻴﺼل ﺇﻟﻰ ﺍﻟﻘﻁـﺭ ‪ d‬ﺜـﻡ‬ ‫ﻴﻜﺒﺭ ﺍﻟﻘﻁﺭ ﺘﺩﺭﻴﺠﻴﺎ ﻟﻴﺼل ﺇﻟﻰ ﻗﻴﻤﺘﻪ ﺍﻷﺼﻠﻴﺔ ﻜﻤـﺎ ﺒﺎﻟﺸـﻜل‬ ‫ﹰ‬ ‫2‬ ‫)٧( ﺒﺤﻴﺙ ﺘﻜﻭﻥ ﻨﺴﺒﺔ ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁـﻊ ⎞ ⎛ ﻓـﻲ ﺤـﺩﻭﺩ‬ ‫‪d‬‬ ‫⎟ ⎜‬ ‫⎠‪⎝D‬‬ ‫٥٠,٠ ﺇﻟﻰ ٥٥,٠.‬ ‫ﺒﺘﻁﺒﻴﻕ ﻤﻌﺎﺩﻟﺔ ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺍﻟﻨﻘﻁﺘﻴﻥ )١(، )٢( ﻤﻊ ﻭﻀﻊ‬ ‫ﺘﺄﺜﻴﺭ ﺍﻟﻠﺯﻭﺠﺔ ﻓﻲ ﺍﻹﻋﺘﺒﺎﺭ ﻭﺇﺴـﺘﺨﺩﺍﻡ ﻤﻌﺎﺩﻟـﺔ ﺍﻹﺴـﺘﻤﺭﺍﺭ‬ ‫ﻭﺇﺩﺨﺎل ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ‪ Kd‬ﻟﻴﺤل ﻤﺤل ﺍﻟﻔﺎﻗﺩ ﺒﺎﻹﺤﺘﻜﺎﻙ ‪hf‬‬ ‫ﻜﻤﺎ ﺘﻡ ﻟﻠﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﻭﻫﺔ ﻴﻤﻜﻥ ﺤﺴﺎﺏ ﺍﻟﻜﻤﻴـﺔ ‪ Q‬ﺍﻟﻤـﺎﺭﺓ‬ ‫ﺨﻼل ﺍﻟﻔﻨﺸﻭﺭﻯ‬ ‫‪π‬‬ ‫‪2 gh‬‬ ‫‪Q = Kd‬‬ ‫2‪d‬‬ ‫4‬ ‫⎤ 4⎞ ‪⎡ ⎛ d‬‬ ‫⎥ ⎟ ⎜ − 1⎢‬ ‫⎥ ⎠‪⎢ ⎝D‬‬ ‫⎣‬ ‫⎦‬ ‫ﻭﺒﻬﺫﻩ ﺍﻟﻁﺭﻴﻘﺔ ﻴﺘﻡ ﻗﻴﺎﺱ ﺍﻟﻜﻤﻴﺔ ﺒﻤﻌﺭﻓﺔ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺒـﻴﻥ‬ ‫ﻗﺒل ﺒﺩﺍﻴﺔ ﺘﺼﻐﻴﺭ ﺍﻟﻘﻁﺭ ﻭﻋﻨﺩ ﺃﻗل ﻗﻁﺭ ﻭﻴﻤﻜﻥ ﺭﺴﻡ ﺇﻨﺤـﺩﺍﺭ‬ ‫ﺍﻟﻁﺎﻗﺔ ﻭﺍﻟﻀﻐﻁ ﻭﻴﺘﻀﺢ ﻤﻨﻪ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ‪ hf‬ﺘﻘﺎﺒل ﺇﺴﺘﺨﺩﺍﻡ‬ ‫ﺍﻟﻤﻌﺎﻤل ‪ ،kd‬ﻭﻴﺴﺒﺏ ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﻓﺎﻗﺩ ﻀﻐﻁ ﺼﻐﻴﺭ ﺠﺩﺍ‬ ‫ﹰ‬ ‫ﻭﻴﺘﺭﺍﻭﺡ ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ﻟﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﺒﻴﻥ ﻗﻴﻤﺔ ﺘﻘﺭﻴﺒﻴﺔ‬ ‫ﻗﺩﺭﻫﺎ ٥٣٩,٠ ﻟﻸﻗﻁﺎﺭ ﻭﺍﻟﺴﺭﻋﺎﺕ ﺍﻟﺼﻐﻴﺭﺓ ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )٢(‬ ‫- ٩٢ -‬
‫ﺇﻟﻰ ٨٨٩,٠ ﻟﻸﻗﻁﺎﺭ ﻭﺍﻟﺴﺭﻋﺎﺕ ﺍﻟﻜﺒﻴﺭﺓ ﻨﺴﺒﻴﺎ ﻋﻨﺩ ﺍﻟﻤﻘﻁـﻊ‬ ‫ﹰ‬ ‫)٢( ﻭﻟﺘﺴﻬﻴل ﺍﻟﺤﺴﺎﺒﺎﺕ ﻴﻤﻜﻥ ﺇﻋﺘﺒﺎﺭ ﺍﻟﻘﻴﻤﺔ ﺍﻟﺘﻘﺭﻴﺒﻴـﺔ ﻟﻬـﺫﺍ‬ ‫ﺍﻟﻤﻌﺎﻤـل ﺘﺴـﺎﻭﻯ ٨٩,٠ – ٩٩,٠ ﻭﺘﻜـﻭﻥ ﻗﻴﻤـﺔ ﻤﻌﺎﻤـل‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ﺍﻟﺘﺼﺭﻴﻑ ﻟﻠﻬﻭﺍﺀ ﺤﻭﺍﻟﻰ ٩٩,٠‬ ‫ﻭﺍﻟﺠﺩﻭل ﺭﻗﻡ )١( ﻴﻭﻀﺢ ﻤﻘﺎﺭﻨﺔ ﻟﻘﻴﻤـﺔ ﺍﻟﻔﺎﻗـﺩ ﺍﻟﻜﻠـﻰ‬ ‫ﻟﻠﻀﻐﻁ ﻋﺒﺭ ﺍﻟﻤﻘﻴﺎﺱ ﻭﺫﻟﻙ ﻟﻸﻨﻭﺍﻉ ﺍﻟﺜﻼﺜﺔ ﺍﻟﺴﺎﺒﻘﺔ ﻷﺠﻬـﺯﺓ‬ ‫ﻗﻴﺎﺱ ﺍﻟﻜﻤﻴﺔ ﻭﺫﻟﻙ ﺒﺈﻋﺘﺒﺎﺭ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘﺎﺱ ﻤﻘﺩﺍﺭ ﺜﺎﺒـﺕ‬ ‫ﻭﻴﺴﺎﻭﻯ ٠٣ﺴﻡ ﺯﺌﺒﻕ )٤,٠ﻜﺠﻡ/ﺴﻡ٢(.‬ ‫ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ‬ ‫ﻓﺭﻕ ﺍﻟﻀﻐﻁ‬ ‫ﻨﺴﺒﺔ‬ ‫ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻟﻠﻀﻐﻁ ﻋﺒﺭ‬ ‫ﻟﻠﻀﻐﻁ ﻋﺒﺭ‬ ‫ﺍﻟﻤﻘﺎﺱ ﻋﻨﺩ‬ ‫ﺍﻷﻗﻁﺎﺭ‬ ‫ﻨﻭﻉ‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﻜﻨﺴﺒﺔ ﻤﺌﻭﻴﺔ ﻤﻥ‬ ‫ﺍﻟﻤﻘﻴﺎﺱ‬ ‫ﺍﻟﻤﺂﺨﺫ ﺍﻟﻤﻼﺌﻤﺔ‬ ‫‪d‬‬ ‫ﺍﻟﻤﻘﻴﺎﺱ‬ ‫ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘﺎﺱ‬ ‫) (‬ ‫)٢‪(kg/cm‬‬ ‫)٢‪(kg/cm‬‬ ‫‪D‬‬ ‫٦١٢,٠‬ ‫٤٥%‬ ‫٤,٠‬ ‫٥٧٦,٠‬ ‫ﺫﻭ ﺍﻟﻔﺘﺤﺔ‬ ‫‪orifice‬‬ ‫٨١,٠‬ ‫٥٤%‬ ‫٤,٠‬ ‫٢٥٦,٠‬ ‫ﺫﻭ ﺍﻟﻔﻭﻫﺔ‬ ‫-‪Flow‬‬ ‫‪Nozzle‬‬ ‫٤٠,٠‬ ‫٠١%‬ ‫٤,٠‬ ‫٥,٠-‬ ‫ـﻭﺭﻯ‬‫ﻓﻨﺸـ‬ ‫٥٧٦,٠‬ ‫‪Venturi‬‬ ‫ﺠﺩﻭل )١(‬ ‫- ٠٣ -‬
‫ﺃﻁﻭﺍل ﺍﻷﻨﺎﺒﻴﺏ ﻗﺒل ﺃﺠﻬﺯﺓ ﺍﻟﻘﻴﺎﺱ ﻭﺒﻌﺩﻫﺎ:‬ ‫ﻋﻨﺩ ﺇﺴﺘﺨﺩﺍﻡ ﺃﺠﻬﺯﺓ ﻟﻘﻴﺎﺱ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ ﻓﻲ ﺍﻷﻨﺎﺒﻴﺏ ﻴﺠﺏ‬ ‫ﺃﻥ ﻴﺴﺒﻕ ﺍﻟﺠﻬﺎﺯ ﻁﻭل ﻤﺴﺘﻘﻴﻡ ﻤﻥ ﺍﻷﻨﺒﻭﺒـﺔ ‪Straight Run‬‬ ‫ﻟﻀﻤﺎﻥ ﺇﻨﺘﻅﺎﻡ ﺍﻟﺴﺭﻴﺎﻥ ﻗﺒل ﺍﻟﺠﻬـﺎﺯ ﻭﺨﺎﺼـﺔ ﺇﺫﺍ ﺇﺤﺘـﻭﺕ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﻋﻠﻰ ﺘﺭﻜﻴﺒﺎﺕ ﻤﺜل ﺍﻷﻜـﻭﺍﻉ، ﺍﻟﺘﻴﻬـﺎﺕ ﻭﺍﻟﻤﺤـﺎﺒﺱ‬ ‫ﻭﻜﺫﻟﻙ ﻴﺠﺏ ﺃﻥ ﻴﻠﻰ ﺍﻟﺠﻬﺎﺯ ﻁﻭل ﻤﺴﺘﻘﻴﻡ ﻤﻥ ﺍﻷﻨﺒﻭﺒﺔ ﻭﺫﻟـﻙ‬ ‫ﺤﺘﻰ ﻻ ﺘﺅﺜﺭ ﺍﻟﻀﻐﻭﻁ ﺍﻟﺨﻠﻔﻴﺔ ‪ Back pressure‬ﻋﻠﻰ ﺩﻗـﺔ‬ ‫ﺘﺘﺭﺍﻭﺡ ﺒـﻴﻥ‬ ‫ﺍﻟﺠﻬﺎﺯ ﻭﺇﺫﺍ ﻜﺎﻨﺕ ﺍﻟﻨﺴﺒﺔ ﺍﻟﺘﻘﺭﻴﺒﻴﺔ ﻟﻸﻗﻁﺎﺭ‬ ‫‪d‬‬ ‫‪D‬‬ ‫٢٥٦,٠ – ٥٧٦,٠ ﻴﻜﻭﻥ ﺍﻟﻁﻭل ﺍﻟﻤﺴـﺘﻘﻴﻡ ﺍﻟﺘﻘﺭﻴﺒـﻰ ﻗﺒـل‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ ‪ orifice‬ﻴﺴﺎﻭﻯ ٠٢ ﻤﺜل ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒـﺔ‬ ‫)‪ (٢٠ D‬ﻭﻴﻜﻭﻥ ﺍﻟﻁﻭل ﺍﻟﻤﺴﺘﻘﻴﻡ ﺍﻟﺘﻘﺭﻴﺒﻰ ﻗﺒـل ﺍﻟﻤﻘﻴـﺎﺱ ﺫﻭ‬ ‫ﺍﻟﻔﻭﻫﺔ ‪ Flow-Nozzle‬ﻭﻗﺒل ﻤﻘﻴـﺎﺱ ﻓﻨﺸـﻭﺭﻯ ‪Venturi‬‬ ‫ﻴﺴﺎﻭﻯ ٠٣ ﻤﺜل ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒﺔ )‪ (٣٠D‬ﻭﺫﻟﻙ ﻓﻲ ﺃﺴﻭﺃ ﺤﺎﻟـﺔ‬ ‫‪ Worst Case‬ﻤﻥ ﺃﻨﻭﺍﻉ ﺍﻟﺘﺭﻜﻴﺒﺎﺕ ﻭﻓﻲ ﺃﻏﻠﺏ ﺍﻷﺤﻴﺎﻥ ﻴﻜﻭﻥ‬ ‫ﺍﻟﻁﻭل ﺍﻟﻤﺴﺘﻘﻴﻡ ﺍﻟﺘﻘﺭﻴﺒﻰ ﺒﻌﺩ ﺍﻟﺠﻬﺎﺯ ﻴﺴﺎﻭﻯ ﺨﻤﺴـﺔ ﺃﻤﺜـﺎل‬ ‫ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒﺔ )‪ (٥D‬ﻭﺫﻟﻙ ﻟﻜل ﺃﺠﻬﺯﺓ ﺍﻟﻘﻴﺎﺱ ﺍﻟﺴﺎﺒﻘﺔ.‬ ‫- ١٣ -‬
‫٤- ﺃﻨﺒﻭﺒﺔ ‪:Pitot‬‬ ‫ﺸﻜل )٨(‬ ‫ﺸﻜل )٩(‬ ‫- ٢٣ -‬
‫ﺘﺘﻜﻭﻥ ﺃﻨﺒﻭﺒﺔ ‪ Pitot‬ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻋﻠﻰ ﻫﻴﺌﺔ ﺯﺍﻭﻴـﺔ ﻗﺎﺌﻤـﺔ‬ ‫ﻭﻋﻨﺩﻤﺎ ﻴﻐﻤﺭ ﺍﻟﺠﺯﺀ ﺍﻟﻤﺜﻨﻰ ﺠﺯﺌﻴﺎ ﺘﺤﺕ ﺍﻟﻤﺎﺀ ﻭﻴﻭﺠﻪ ﻤﺒﺎﺸﺭﺓ‬ ‫ﹰ‬ ‫ﻹﺘﺠﺎﻩ ﺍﻟﺴﺭﻴﺎﻥ ‪ Flow‬ﻓﺈﻨﻪ ﻴﺒﻴﻥ ﺴﺭﻋﺔ ﺍﻟﺴـﺭﻴﺎﻥ ﺒﺎﻟﻤﺴـﺎﻓﺔ‬ ‫ﺍﻟﺘﻲ ﻴﺭﺘﻔﻌﻬﺎ ﺍﻟﻤﺎﺀ ﻓﻲ ﺍﻟﺠﺯﺀ ﺍﻟﺭﺃﺴﻰ ﻤﻥ ﺍﻷﻨﺒﻭﺒﺔ ﻋﻥ ﺴﻁﺢ‬ ‫2‪V‬‬ ‫ﻜﻤﺎ ﻫﻭ‬ ‫ﺍﻟﻤﺎﺀ ﺤﻴﺙ ﺃﻥ ﻫﺫﻩ ﺍﻟﻤﺴﺎﻓﺔ ﺘﺴﺎﻭﻯ ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ‬ ‫‪2g‬‬ ‫ﺒﺎﻟﺸﻜل )٨(.‬ ‫ﻭﺍﻟﺸﻜل ﺍﻟﻤﺘﻜﺎﻤل ﻟﻬﺫﻩ ﺍﻷﻨﺒﻭﺒﺔ ﻴﻌﺭﻑ ﺒﺈﺴﻡ ‪Pitot-Static‬‬ ‫ﻜﻤﺎ ﺒﺎﻟﺸﻜل )٩( ﻭﻫﻰ ﺘﺘﻜﻭﻥ ﻤﻥ ﺠﺯﺌﻴﻥ ﺃﺴﺎﺴﻴﻴﻥ ﻤﻨﻔﺼـﻠﻴﻥ‬ ‫ﻭﻤﺘﻭﺍﺯﻴﻴﻥ ﺃﺤﺩﻫﻡ ﻴﺒﻴﻥ ﻤﺠﻤﻭﻉ ﺍﻟﻀﻐﻁ ﺍﻟﻜﻠﻰ )ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ(‬ ‫ﻭﺍﻵﺨﺭ ﻴﺒﻴﻥ ﺍﻟﻀﻐﻁ ﺍﻹﺴﺘﺎﺘﻴﻜﻰ )ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ( ﻓﻘـﻁ ﻭﻴـﺘﻡ‬ ‫ﺍﻟﺤﺼﻭل ﻋﻠﻰ ﺍﻟﻀﻐﻁ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻰ )ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜـﺔ( ﺒﻁـﺭﺡ‬ ‫ﺍﻟﻀﻐﻁ ﺍﻹﺴﺘﺎﺘﻴﻜﻰ ﻤﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻜﻠﻰ ﺤﻴﺙ ﺃﻥ ﺃﻨﺒﻭﺒﺔ -‪Pitot‬‬ ‫‪ static‬ﺘﻘﻴﺱ ﺍﻟﻔﺭﻕ ﺒﻴﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻜﻠﻰ ﻭﺍﻟﻀﻐﻁ ﺍﻹﺴـﺘﺎﺘﻴﻜﻰ‬ ‫ﻋﻨﺩ ﻨﻘﻁﺔ ﻭﺤﻴﺩﺓ ﻭﺘﺴﺘﺨﺩﻡ ﺍﻟﻤﺎﻨﻭﻤﺘﺭﺍﺕ ﺒﺼﻭﺭﺓ ﺸﺎﺌﻌﺔ ﻟﻘﻴﺎﺱ‬ ‫ﻫﺫﻩ ﺍﻟﻀﻐﻭﻁ.‬ ‫- ٣٣ -‬
‫ﻭﻴﻭﻀﺢ ﺸﻜل )٠١( ﺇﺴﺘﺨﺩﺍﻡ ﺃﻨﺒﻭﺒﺔ ‪ Pitot-Static‬ﻟﻘﻴﺎﺱ‬ ‫ﺍﻟﻜﻤﻴﺔ )ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ( ﻓـﻲ ﺍﻟﻘﻨـﻭﺍﺕ ﺍﻟﻤﻔﺘﻭﺤـﺔ ﻟﻠﺴـﺭﻴﺎﻥ‬ ‫ﺍﻟﻤﻨﺨﻔﺽ ﺍﻟﺴﺭﻋﺔ ﺤﻴﺙ ﺃﻨﻪ ﻴﺼﻌﺏ ﻗﻴﺎﺱ ﺇﺭﺘﻔﺎﻉ ﺍﻟﻤﺎﺀ ﻓـﻲ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﻓﻭﻕ ﺴﻁﺢ ﺍﻟﻤﺎﺀ ﺍﻟﻤﺘﺩﻓﻕ ﻭﻴﺘﻡ ﺫﻟﻙ ﺒﺘﻭﺼﻴل ﻁﺭﻓﻲ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﺒﺒﻌﺽ ﻤﻥ ﺃﻋﻠﻰ ﺒﻭﺍﺴﻁﺔ ﻭﺼﻠﺔ ﻋﻠﻰ ﺸﻜل ﺤـﺭﻑ‬ ‫‪ T‬ﻭﻴﻭﺼل ﺍﻟﻁﺭﻑ ﺍﻟﺜﺎﻟﺙ ﻟﻬﺎ ﺒﺨﻁ ﻴﻤﻜﻥ ﺘﻭﻟﻴﺩ ﺨﻠﺨﻠﺔ ﺠﺯﺌﻴﺔ‬ ‫ﺒﻪ ﻭﺒﻌﺩ ﺃﺨﺫ ﺍﻟﻬﻭﺍﺀ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ‪ Pitot‬ﻴﺭﺘﻔﻊ ﺍﻟﻤﺎﺀ ﻷﻋﻠﻰ ﺇﻟﻰ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﺤﺘﻰ ﺍﻹﺭﺘﻔﺎﻉ ﺍﻟﻤﻘﺘﺭﺡ ﻟﺘﺴﻬﻴل ﺍﻟﻘﺭﺍﺀﺓ ﺜﻡ ﻴﻐﻠﻕ ﺨﻁ‬ ‫ﺍﻟﺨﻠﺨﻠﺔ ﻭﺘﺅﺜﺭ ﺍﻟﺨﻠﺨﻠﺔ ﺍﻟﺠﺯﺌﻴـﺔ ﺒﺎﻟﺘﺴـﺎﻭﻯ ﻋﻠـﻰ ﻁﺭﻓـﻲ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﻭﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻟﻡ ﻴﺘﻐﻴﺭ ﻓﺭﻕ ﺍﻟـ ‪.Head‬‬ ‫ﺸﻜل )٠١(‬ ‫- ٤٣ -‬
‫ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ﻓﻲ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﻨﻘﺴﻡ ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ﻓﻲ ﺍﻷﻨﺎﺒﻴﺏ ﺇﻟﻰ ﻨﻭﻋﻴﻥ ﻫﻤﺎ :‬ ‫١- ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻨﺘﻴﺠﺔ ﺇﺠﻬﺎﺩﺍﺕ ﺍﻟﻘﺹ ﺍﻟﻠﺯﺝ ﺩﺍﺨـل‬ ‫ﺍﻟﺴﺎﺌل ﻭﺍﻹﻀﻁﺭﺍﺏ ﻋﻨﺩ ﺠﺩﺍﺭ ﺍﻷﻨﺒﻭﺒﺔ.‬ ‫٢- ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻨﺘﻴﺠﺔ ﻭﺠﻭﺩ ﺘﻐﻴﺭ ﻓـﻲ ﺴـﺭﻋﺔ ﺃﻭ‬ ‫ﺇﺘﺠﺎﻩ ﺍﻟﺴﺭﻴﺎﻥ ﻭﻨﻼﺤﻅ ﺃﻥ ﺘﻘﻠﻴل ﺍﻟﺴﺭﻋﺔ ﻴﺘﺴﺒﺏ ﻓﻲ‬ ‫ﻓﺎﻗﺩ ﻀﻐﻁ ﺃﻋﻠﻰ ﻤﻥ ﺯﻴﺎﺩﺓ ﺍﻟﺴﺭﻋﺔ.‬ ‫١- ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ‪:Friction Head Loss‬‬ ‫ﻴﻌﺘﻤﺩ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﺍﻟﻤـﺎﺭ‬ ‫ﻭﺴﺭﻋﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻭﺃﺒﻌﺎﺩ ﺍﻷﻨﺒﻭﺒﺔ ﻭﺍﻟﻤـﺎﺩﺓ ﺍﻟﻤﺼـﻨﻭﻉ ﻤﻨﻬـﺎ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﻭﻫﻭ ﻴﺴﺎﻭﻯ.‬ ‫‪l‬‬ ‫2 ‪⎛ V 2 ⎞ 0.81057 flQ‬‬ ‫‪hf = f‬‬ ‫⎜‬ ‫= ⎟ ‪⎜ 2g‬‬ ‫⎟‬ ‫‪d‬‬ ‫⎝‬ ‫⎠‬ ‫5 ‪gd‬‬ ‫2‪V‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ l‬ﻁﻭل ﺍﻷﻨﺒﻭﺒﺔ، ‪ d‬ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﻸﻨﺒﻭﺒﺔ،‬ ‫‪2g‬‬ ‫ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ، ‪ Q‬ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ ﺃﻭ ﺍﻟﻜﻤﻴﺔ‬ ‫- ٥٣ -‬
‫‪ f‬ﻤﻌﺎﻤل ﺍﻹﺤﺘﻜﺎﻙ ﻭﺘﻌﺘﻤﺩ ﻗﻴﻤﺘﻪ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴـﺭﻴﺎﻥ ﻓـﻲ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﺤﻴﺙ ﻴﻭﺠﺩ ﻨﻭﻋﺎﻥ ﻤﻥ ﺍﻟﺴﺭﻴﺎﻥ ﻓﻲ ﺍﻷﻨﺎﺒﻴـﺏ ﻫﻤـﺎ‬ ‫ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﺭﻗﺎﺌﻘﻰ ‪ Laminar Flow‬ﻭﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻤﻀـﻁﺭﺏ‬ ‫‪ Turbulent Flow‬ﻭﻟﻜﻲ ﻴﺘﻡ ﻨﻘل ﺍﻟﺴﻭﺍﺌل ﺒﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ‬ ‫ﺒﺼﻭﺭﺓ ﺇﻗﺘﺼﺎﺩﻴﺔ ﺒﻤﻌﻨﻰ ﺘﺤﻘﻴﻕ ﺃﻗل ﺘﻜﻠﻔﺔ ﻜﻠﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ ﻓﺈﻥ‬ ‫ﺫﻟﻙ ﻴﺴﺘﻭﺠﺏ ﺃﻥ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴـﺎﺕ ﺍﻟﻤﻨﻘﻭﻟـﺔ ﺒـﺎﻟﺨﻁ ﻜﺒﻴـﺭﺓ‬ ‫ﻭﺒﺎﻟﺘﺎﻟﻰ ﻴﻜـﻭﻥ ﺍﻟﺴـﺭﻴﺎﻥ ﻤﻀـﻁﺭﺏ ‪Turbuleut FLow‬‬ ‫ﻭﻴﺘﺤﺩﺩ ﻨﻭﻉ ﺍﻟﺴﺭﻴﺎﻥ ﻋﻥ ﻁﺭﻴﻕ ﺭﻗﻡ ﺒﺩﻭﻥ ﻭﺤـﺩﺍﺕ ﻴﺴـﻤﻰ‬ ‫ﺭﻗﻡ ﺭﻴﻨﻭﻟﺩ ‪ Reynold's Number‬ﻭﻴﺭﻤﺯ ﻟﻪ ﺒـﺎﻟﺭﻤﺯ ‪RN‬‬ ‫ﻭﻫﻭ ﻴﺴﺎﻭﻯ‬ ‫)‪sp.gr × V (cm / sec) × d (cm‬‬ ‫= ‪RN‬‬ ‫)‪µ ( poise‬‬ ‫)‪25400 × V (mt / sec) × d (inch‬‬ ‫=‬ ‫) ‪γ (cst‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ sp.gr‬ﻫﻰ ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ ﻟﻠﺴﺎﺌل ﻭﻫﻰ ﺭﻗﻡ ﺒﺩﻭﻥ‬ ‫ﻭﺤﺩﺍﺕ ﻭﺘﺴﺎﻭﻯ ﻋﺩﺩﻴﺎ ﻜﺜﺎﻓﺔ ﺍﻟﺴﺎﺌل ﺒﺎﻟﺠﺭﺍﻡ/ ﺴﻨﺘﻴﻤﺘﺭ ﻤﻜﻌﺏ‬ ‫ﹰ‬ ‫‪ V‬ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﺍﻟﺴﺎﺌل ﺩﺍﺨل ﺍﻷﻨﺒﻭﺒﺔ‬ ‫‪ d‬ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﻸﻨﺒﻭﺒﺔ‬ ‫- ٦٣ -‬
‫‪ µ‬ﺃﻭ ‪ γ‬ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ )ﺍﻟﻤﻁﻠﻘﺔ( ﺃﻭ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴﺔ‬ ‫ﻭﻗﺩ ﻭﺠﺩ ﺃﻨﻪ ﺇﺫﺍ ﻜﺎﻥ ﺭﻗﻡ ﺭﻴﻨﻭﻟﺩ ﺃﻗل ﻤـﻥ ٠٠٠٢ ﻜـﺎﻥ‬ ‫ﺍﻟﺴﺭﻴﺎﻥ ﺭﻗﺎﺌﻘﻰ )ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﻤﻨﺨﻔﻀﺔ ﻨﺴﺒﻴﺎ( ﻭﻓـﻲ ﻫـﺫﻩ‬ ‫ﹰ‬ ‫ﺍﻟﺤﺎﻟﺔ ﺘﻜﻭﻥ ﺍﻟﻠﺯﻭﺠﺔ ﻫﻰ ﺍﻟﺴﺒﺏ ﺍﻷﻜﺒﺭ ﻟﻤﻘﺎﻭﻤﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻭﻓﻘﺩ‬ ‫ﺍﻟﻀﻐﻁ، ﻭﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻴﻜﻭﻥ‬ ‫) ‪γ (Cst‬‬ ‫7870.0 < ) ‪V (mt / sec‬‬ ‫)‪d (inch‬‬ ‫)‪Q(mt٣/hr) < ٠,١٤٣٦γ (cst). d(inch‬‬ ‫ﻭﺃﻴﻀﺎ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻴﺴﺎﻭﻯ‬ ‫ﹰ‬ ‫‪γlQ‬‬ ‫7177.2 = ‪h f‬‬ ‫4‪d‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ hf‬ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﺒﺎﻟﻤﺘﺭ‬ ‫‪l‬‬ ‫‪ γ‬ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺒﺎﻟﺴﻨﺘﻰ ﺴﺘﻭﻜﺱ‬ ‫ﻁﻭل ﺍﻷﻨﺒﻭﺒﺔ ﺒﺎﻟﻜﻴﻠﻭﻤﺘﺭ‬ ‫‪ Q‬ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ ﺃﻭ ﺍﻟﻜﻤﻴﺔ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴـﺎﻋﺔ،‬ ‫‪ d‬ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﻸﻨﺒﻭﺒﺔ ﺒﺎﻟﺒﻭﺼﺔ‬ ‫- ٧٣ -‬
‫ﻭﺇﺫﺍ ﻜﺎﻥ ﺭﻗﻡ ﺭﻴﻨﻭﻟﺩ ﺃﻜﺒﺭ ﻤـﻥ ٠٠٠٤ ﻜـﺎﻥ ﺍﻟﺴـﺭﻴﺎﻥ‬ ‫ﻤﻀﻁﺭﺏ )ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﻋﺎﻟﻴﺔ ﻨﺴﺒﻴﺎ ﻭﺃﻜﺜﺭ ﺇﻨﺘﻅﺎﻤﺎ(، ﻭﻓـﻲ‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻴﻜﻭﻥ ﺍﻟﺴﺒﺏ ﺍﻟﻤﻠﺤﻭﻅ ﺃﻜﺜﺭ ﻟﻤﻘﺎﻭﻤﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻫـﻭ‬ ‫ﻨﺘﻴﺠﺔ ﺨﺸﻭﻨﺔ ﺠﺩﺍﺭ ﺍﻷﻨﺒﻭﺒﺔ ﻭﺍﻹﻀﻁﺭﺍﺏ ﻭﻓﻲ ﻫـﺫﻩ ﺍﻟﺤﺎﻟـﺔ‬ ‫ﻴﻜﻭﻥ‬ ‫) ‪γ (Cst‬‬ ‫84751.0 > )‪V (mt / sec‬‬ ‫)‪d (inch‬‬ ‫)‪Q(mt / hr ) > 0.287 γ (cst ). d (inch‬‬ ‫3‬ ‫ﻭﺃﻴﻀﺎ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻴﺴﺎﻭﻯ‬ ‫ﹰ‬ ‫57.1 ‪γ 0.25 l Q‬‬ ‫5245.71 = ‪h f‬‬ ‫57.4 ‪d‬‬ ‫ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓـﻲ ﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫‪hf‬‬ ‫ﺤﻴﺙ ﺃﻥ‬ ‫ﺒﺎﻟﻤﺘﺭ‬ ‫ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺴﻨﺘﻰ‬ ‫‪γ‬‬ ‫ﺴﺘﻭﻜﺱ‬ ‫ﻁﻭل ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﻜﻴﻠﻭﻤﺘﺭ‬ ‫‪l‬‬ ‫ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ‬ ‫‪Q‬‬ ‫ﻓﻲ ﺍﻟﺴﺎﻋﺔ‬ ‫- ٨٣ -‬
‫ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺒﻭﺼﺔ‬ ‫‪d‬‬ ‫٢- ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ‪:Minor losses‬‬ ‫⎞ 2 ‪⎛V‬‬ ‫⎞ 2 ‪⎛V‬‬ ‫ﻭﻫﻰ ﺘﺴﺎﻭﻯ ⎟ ⎜ ‪ hs = K‬ﺤﻴﺙ ﺃﻥ ⎟ ⎜ ﻫﻰ ﻁﺎﻗـﺔ‬ ‫⎟ ‪⎜ 2g‬‬ ‫⎟ ‪⎜ 2g‬‬ ‫⎝‬ ‫⎠‬ ‫⎝‬ ‫⎠‬ ‫ﺍﻟﺤﺭﻜﺔ، ‪ K‬ﻤﻌﺎﻤل ﻴﻌﺘﻤﺩ ﻋﻠﻰ ﻤﺼﺩﺭ ﺍﻟﻔﺎﻗﺩ ﻭﻴﻤﻜـﻥ ﺇﻴﺠـﺎﺯ‬ ‫ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻜﻤﺎ ﻓﻲ ﺍﻟﺠﺩﻭل )٢(.‬ ‫ﻤﻌﺎﻤل ﺍﻟﻔﺎﻗﺩ ‪K‬‬ ‫ﺍﻟﻔـــــﺎﻗﺩ‬ ‫٥,٠‬ ‫ﻓﻲ ﻤﺩﺨل ﺍﻷﻨﺒﻭﺒﺔ‬ ‫١‬ ‫ﻋﻨﺩ ﻤﺨﺭﺝ ﺍﻷﻨﺒﻭﺒﺔ‬ ‫٥,٠‬ ‫ﻋﻨﺩ ﺘﻘﻠﻴل ﻤﻘﻁﻊ ﺍﻷﻨﺒﻭﺒﺔ ﻓﺠﺄﺓ‬ ‫٥٠,٠‬ ‫ﻋﻨﺩ ﺘﻘﻠﻴل ﻤﻘﻁﻊ ﺍﻷﻨﺒﻭﺒﺔ ﺘﺩﺭﻴﺠﻴﺎ‬ ‫ﹰ‬ ‫١‬ ‫ﻓﻲ ﺍﻟﻜﻭﻉ ٠٩‪º‬‬ ‫٥,٠‬ ‫ﻓﻲ ﺍﻟﻜﻭﻉ ٥٤‪º‬‬ ‫٩,٠‬ ‫ﻓﻲ ﺍﻟﻭﺼﻠﺔ ﺘﻴﻪ‬ ‫٢,٠‬ ‫ﻓﻲ ﺍﻟﻤﺤﺒﺱ ﺍﻟﻤﻔﺘﻭﺡ ﺘﻤﺎﻤﺎ‬ ‫ﹰ‬ ‫ﺠﺩﻭل )٢(‬ ‫- ٩٣ -‬
‫ﻭﺘﻭﺠﺩ ﻁﺭﻴﻘﺔ ﺃﺨﺭﻯ ﻟﺤﺴﺎﺏ ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻫﻰ ﻁﺭﻴﻘـﺔ‬ ‫ﺍﻷﻁـﻭﺍل ﺍﻟﻤﻜﺎﻓﺌـﺔ ‪ Equivalent Length‬ﺒﻤﻌﻨـﻰ ﺃﻥ ﺃﻯ‬ ‫ﻤﺼﺩﺭ ﻤﻥ ﻤﺼﺎﺩﺭ ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻴﻌﻁﻰ ﻓﻲ ﺼﻭﺭﺓ ﻁـﻭل‬ ‫ﻤﺴﺘﻘﻴﻡ ﻤﻥ ﺍﻷﻨﺒﻭﺒﺔ ﺒﺸﺭﻁ ﺃﻥ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓـﻲ ﻫـﺫﺍ‬ ‫ﺍﻟﻁﻭل ﻴﺴﺎﻭﻯ ﺍﻟﻔﺎﻗﺩ ﺍﻟﺜﺎﻨﻭﻯ ﻭﻫﻭ ﻴﺴﺎﻭﻯ‬ ‫2 ‪leq ⎛ V 2 ⎞ 0.81057 f leq Q‬‬ ‫‪hs = f‬‬ ‫⎜‬ ‫=⎟‬ ‫⎟ ‪d ⎜ 2g‬‬ ‫⎝‬ ‫⎠‬ ‫5 ‪gd‬‬ ‫- ٠٤ -‬
(٣) ‫ ﻟﻤﺼﺎﺩﺭ ﺍﻟﻔﺎﻗﺩ ﺒﺎﻟﻤﺘﺭ ﻜﻤﺎ ﺒﺎﻟﺠﺩﻭل‬leq ‫ﻭﺘﻌﻁﻰ ﻗﻴﻡ‬ Welding Bends Valves Elbows Ratio Of Pipe Bend Long Short Welding Size Radius Radius Radius Tee Swing (Inch) To Pipe Gate Globe Angle Check Size ٥=‫ﻨﻕ=٦ ﻨﻕ‬ = ‫ﻨﻕ‬ ‫ﻨﻕ=٥,١ﺍﻟﻘﻁﺭ‬ ‫ﺍﻟﻘﻁﺭ ﺍﻟﻘﻁﺭ‬ ‫ﺍﻟﻘﻁﺭ‬ ١ ٠,١٥٠,١٨ ٠,٣٣ ٠,٤٣ ١,١٩ ٠,١٨ ٨,٨٤ ٤,٥٧ ٢,٢٢ ١,٢٥ ٠,١٨٠,٢٤ ٠,٤٣ ٠,٥٥ ١,٥٨ ٠,٢٤ ١١,٥٨ ٥,٧٩ ٢,٩٣ ١,٥ ٠,٢٤٠,٢٧ ٠,٤٩ ٠,٦٤ ١,٨٣ ٠,٢٧ ١٣,٧٢ ٦,٧ ٣,٣٥ ٢ ٠,٣٠٠,٣٣ ٠,٦٤ ٠,٨٥ ٢,٣٨ ٠,٣٦ ١٧,٣٧ ٨,٨٤ ٤,٢٧ ٢,٥ ٠,٣٦٠,٤٠ ٠,٧٦ ١ ٢,٨٣ ٠,٤٣ ٢١,٠٣ ١٠,٣٦ ٥,١٨ ٣ ٠,٤٦٠,٥٢ ٠,٩٤ ١,٢٥ ٣,٣٥ ٠,٥٥ ٢٥,٩١ ١٣,١١ ٦,٤ ٤ ٠,٦١٠,٦٧ ١,٢٢ ١,٦٤ ٤,٥٧ ٠,٧٣ ٣٤,١٤ ١٧,٠٧ ٨,٥٣ ٥ ٠,٧٦٠,٨٥ ١,٥٥ ٢,٠٤ ٥,٧٩ ٠,٨٨ ٤٢,٦٧ ٢١,٣٤١٠,٦٧ ٦ ٠,٩١ ١ ١,٨٦ ٢,٤٧ ٧ ١,٠٧ ٥١,٢١ ٢٥,٦ ١٢,٨ ٨ ١,١٩١,٣١ ٢,٤٤ ٣,٣٥ ٩,١٤ ١,٤٣ ٦٧,٦٧ ٣٣,٨٣١٧,٠٧ ١٠ ١,٤٩١,٦٨ ٣,٠٥ ٣,٩٦ ١١,٥٨ ١,٨ ٨٤,٧٣ ٤٢,٣٧٢١,٣٤ ١٢ ١,٧٧١,٩٥ ٣,٦٦ ٤,٨٨ ١٣,٧٢ ٢,١٣١٠١,١٩ ٥٠,٦ ٢٥,٣ ١٤ ١,٨٩٢,٠٧ ٣,٩٦ ٥,٤٩ ١٤,٩٣ ٢,٣٥١١٠,٩٥٥٥,٤٧٢٧,٧٤ ١٦ ٢,١٦٢,٣٨ ٤,٥٧ ٦,١ ١٧,٠٧ ٢,٦٨ ١٢٧,١ ٦٣,٤ ٣١,٧ - ٤١ -
‫٨١,٥ ٨٦,٢٤٤,٢ ٨١‬ ‫٧‬ ‫٦٦,٥٣٢٣,١٧٥٩,٢٤١٢٠,٣ ٢,٩١‬ ‫٩٧,٥ ٩٩,٢٤٧,٢ ٠٢‬ ‫٢٦,٧‬ ‫٣٩,٩٣٥٥,٩٧ ١,٩٥١ ٥٣,٣ ٤٦,١٢‬ ‫٦٦,٣٥٣,٣ ٤٢‬ ‫٧‬ ‫٤١,٩‬ ‫٥٨,٧٤١٧,٥٩٢٧,١٩١٦٩,٣ ١٩,٥٢‬ ‫ﺠﺩﻭل )٣(‬ ‫ﻭﻗﺩ ﻴﺘﻀﺢ ﻤﻥ ﺍﻟﺨﺒﺭﺓ ﺍﻟﻌﻤﻠﻴﺔ ﺃﻥ ﺍﻟﺒﻠﻭﻑ ﻤﻥ ﻨﻭﻉ ,‪Gate‬‬ ‫‪ Ball, Plug And Butterfly‬ﻟﻬﺎ ﻤﻘﺎﻭﻤﺔ ﻤﻨﺨﻔﻀﺔ ﻟﻠﺴﺭﻴﺎﻥ‬ ‫ﺃﻤﺎ ﺍﻟﺒﻠﻭﻑ ﺍﻷﺨﺭﻯ ﻤـﻥ ﻨـﻭﻉ ‪ Globe And Angle‬ﻟﻬـﺎ‬ ‫ﻤﻘﺎﻭﻤﺔ ﻤﺭﺘﻔﻌﺔ ﻟﻠﺴﺭﻴﺎﻥ.‬ ‫ﻭﻴﻁﻠﻕ ﻋﻠﻰ ﻤﺠﻤﻭﻉ ﻜﻼ ﻤﻥ ﻓﺎﻗـﺩ ﺍﻹﺤﺘﻜـﺎﻙ ﻭﺍﻟﻔﻭﺍﻗـﺩ‬ ‫ﹰ‬ ‫ﺍﻟﺜﺎﻨﻭﻴﺔ ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﻭﻫﻭ ﻴﺴﺎﻭﻯ‬ ‫2 ‪l + leq ⎛ V 2 ⎞ 0.81057 f (l + leq)Q‬‬ ‫‪ht = h f + hs = f‬‬ ‫⎜‬ ‫=⎟‬ ‫⎟ ‪d ⎜ 2g‬‬ ‫⎝‬ ‫⎠‬ ‫5 ‪gd‬‬ ‫ﻭﻓﻲ ﺤﺎﻟﺔ ﺍﻟﺨﻁﻭﻁ ﺍﻟﻁﻭﻴﻠﺔ ﺘﻜﻭﻥ ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﺼـﻐﻴﺭﺓ‬ ‫ﺠﺩﺍ ﺒﺎﻟﻨﺴﺒﺔ ﻟﻔﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻭﺒﺎﻟﺘﺎﻟﻰ ﻴﻤﻜﻥ ﺇﻫﻤﺎﻟﻬﺎ ﺃﻤﺎ ﻓﻲ ﺤﺎﻟﺔ‬ ‫ﹰ‬ ‫ﺍﻟﺨﻁﻭﻁ ﺍﻟﻘﺼﻴﺭﺓ ﻤﺜل ﺸﺒﻜﺎﺕ ﺍﻟﺨﻁﻭﻁ ﺍﻟﺩﺍﺨﻠﻴﺔ ﻓﺈﻨﻪ ﻻ ﻴﻤﻜﻥ‬ ‫ﺇﻫﻤﺎل ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﺇﺫﺍ ﻤﺎ ﻗﻭﺭﻨﺕ ﺒﻔﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ.‬ ‫- ٢٤ -‬
  ‫א‬ - ٤٣ -
‫ﻁﺭﻕ ﻨﻘل ﺍﻟﺒﺘﺭﻭل:‬ ‫ﻴﺘﻡ ﻨﻘل ﻤﺨﺘﻠﻑ ﺃﻨﻭﺍﻉ ﺍﻟﺒﺘﺭﻭل ﻭﻤﻨﺘﺠﺎﺘﻪ ﺇﻤﺎ ﻋﻥ ﻁﺭﻴـﻕ‬ ‫ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻭ ﺒﺈﺴﺘﺨﺩﺍﻡ ﺴﻴﺎﺭﺍﺕ ﺍﻟﺸﺤﻥ )ﺍﻟﻠـﻭﺍﺭﻯ( ﺃﻭ‬ ‫ﺒﺈﺴﺘﺨﺩﺍﻡ ﺼﻬﺎﺭﻴﺞ ﺍﻟﺴـﻜﺔ ﺍﻟﺤﺩﻴـﺩ ﺃﻭ ﺒﺈﺴـﺘﺨﺩﺍﻡ ﺍﻟﻨـﺎﻗﻼﺕ‬ ‫ﺍﻟﺒﺤﺭﻴﺔ )ﺍﻟﺴﻔﻥ( ﻭﻴﺘﻤﻴﺯ ﺍﻟﻨﻘل ﺒﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﺒﺈﺴـﺘﻤﺭﺍﺭ‬ ‫ﻋﻤﻠﻴﺔ ﺍﻟﻨﻘل ﺒﺼﺭﻑ ﺍﻟﻨﻅﺭ ﻋﻥ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺃﻯ ﻴـﺘﻡ‬ ‫ﻨﻘل ﻤﺨﺘﻠﻑ ﺃﻨﻭﺍﻉ ﺍﻟﺴﻭﺍﺌل ﺒﺎﻟﺘﻌﺎﻗﺏ ﺩﺍﺨل ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻟﻴﺱ‬ ‫ﻨﻘل ﻨﻭﻉ ﻭﺍﺤﺩ ﻤﻥ ﺍﻟﺴﻭﺍﺌل ﻜﻤﺎ ﻴﺘﻡ ﺒﺈﺴﺘﺨﺩﺍﻡ ﺴﻴﺎﺭﺍﺕ ﺍﻟﺸﺤﻥ‬ ‫)ﺍﻟﻠﻭﺍﺭﻯ( ﺃﻭ ﺼﻬﺎﺭﻴﺞ ﺍﻟﺴﻜﺔ ﺍﻟﺤﺩﻴﺩ ﺃﻭ ﺍﻟﻨـﺎﻗﻼﺕ ﺍﻟﺒﺤﺭﻴـﺔ‬ ‫)ﺍﻟﺴﻔﻥ(.‬ ‫- ٤٤ -‬
‫ﺘﺼﻨﻴﻑ ﺃﻨﻅﻤﺔ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﺘﺼﻨﻑ ﺃﻨﻅﻤﺔ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﺨﺎﺼﺔ ﺒﻨﻘل ﺍﻟﺒﺘﺭﻭل ﺇﻟـﻰ‬ ‫ﺜﻼﺜﺔ ﺃﻨﻭﺍﻉ :‬ ‫١- ﻨﻅﺎﻡ ﺍﻟﺘﺠﻤﻴﻊ ‪:Gathering System‬‬ ‫ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﺍﻟﻤﻌﺩﺍﺕ ﺍﻷﺨﺭﻯ ﺍﻟﻤﺴﺘﺨﺩﻤﺔ ﻟﻨﻘل ﺍﻟﺯﻴـﺕ‬ ‫ﺍﻟﺨﺎﻡ ﻭﻤﻨﺘﺠﺎﺘﻪ ﻤﻥ ﺍﻵﺒﺎﺭﺍﻟﻤﻨﻔﺭﺩﺓ ﻭﻤﻭﺍﻗﻊ ﺍﻹﻨﺘﺎﺝ ﺍﻷﺨﺭﻯ ﺇﻟﻰ‬ ‫ﻤﻭﻗﻊ ﺭﺌﻴﺴﻰ ﻴﺴﻤﻰ ﻨﻅﺎﻡ ﺘﺠﻤﻴﻊ، ﻭﺘﺘﻜﻭﻥ ﺃﻨﻅﻤـﺔ ﺍﻟﺘﺠﻤﻴـﻊ‬ ‫ﺃﺴﺎﺴﺎ ﻤﻥ ﻓﺭﻭﻉ ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺘﺴﺭﻯ ﺇﻟﻰ ﻤﺤﻁﺎﺕ ﺨﻁ ﺭﺌﻴﺴﻰ‬ ‫ﹰ‬ ‫ﺃﻭ ﻤﻭﺍﻗﻊ ﺃﺨﺭﻯ ﺤﻴﺙ ﻴﺘﻡ ﻨﻘل ﺍﻟﺯﻴﺕ ﻭﻤﻨﺘﺠﺎﺘﻪ ﺇﻟﻰ ﻨﻅﺎﻡ ﺨﻁ‬ ‫ﺭﺌﻴﺴﻰ، ﻭﺘﻜﻭﻥ ﻤﻌﻅـﻡ ﺍﻷﻗﻁﺎﺭﺍﻟﺸـﺎﺌﻌﺔ ﻟﻠﺨﻁـﻭﻁ ﺒﺘﻠـﻙ‬ ‫ﺍﻟﺘﻔﺭﻴﻌﺎﺕ ﻤﻥ ٤ ﺇﻟﻰ ٢١ ﺒﻭﺼﺔ ﻭﻴﺤﺘﻭﻯ ﻨﻅﺎﻡ ﺍﻟﺘﺠﻤﻴﻊ ﻋﺎﺩﺓ‬ ‫ﻋﻠﻰ ﻤﺤﻁﺎﺕ ﻀﺦ ﻟﺘﺠﻤﻴﻊ ﺍﻟﺯﻴﺕ ﻤﻥ ﺒﺌﺭ ﻤﻔﺭﺩ ﻭﻴﻜﻭﻥ ﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﻤﺴﺘﺨﺩﻡ ﺒﻨﻅﺎﻡ ﺍﻟﺘﺠﻤﻴﻊ ﻗﺼﻴﺭ ﺒﺎﻟﻤﻘﺎﺭﻨـﺔ ﺒﺨﻁـﻭﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﺭﺌﻴﺴﻴﺔ ﻭﻴﺘﺭﺍﻭﺡ ﻤﺩﻯ ﺍﻟﻁﻭل ﻤﻥ ﺃﻤﺘﺎﺭ ﻗﻠﻴﻠﺔ ﺇﻟـﻰ‬ ‫ﻋﺩﺓ ﻜﻴﻠﻭ ﻤﺘﺭﺍﺕ.‬ ‫- ٥٤ -‬
‫٢- ﻨﻅﺎﻡ ﺍﻟﺨﻁ ﺍﻟﺭﺌﻴﺴﻰ ‪:Trunk Line System‬‬ ‫ﻭﺘﻜﻭﻥ ﺍﻟﻤﺭﺤﻠﺔ ﺍﻟﺜﺎﻨﻴﺔ ﻫﻰ ﻨﻘل ﺍﻟﺯﻴﺕ ﺍﻟﺨﺎﻡ ﻭﻤﻨﺘﺠﺎﺘﻪ ﻋﻥ‬ ‫ﻁﺭﻴﻕ ﺨﻁـﻭﻁ ﺃﻨﺎﺒﻴـﺏ ﺭﺌﻴﺴـﻴﺔ ‪Trunk Pipe –Lines‬‬ ‫ﻭﻴﺴﺘﺨﺩﻡ ﻨﻅﺎﻡ ﺍﻟﺨﻁ ﺍﻟﺭﺌﻴﺴﻲ ﻟﻨﻘل ﺍﻟﺒﺘﺭﻭل ﻭﻤﻨﺘﺠﺎﺘـﻪ ﻤـﻥ‬ ‫ﺍﻵﺒﺎﺭ ﻭ ﻤﻭﺍﻗﻊ ﺍﻹﻨﺘﺎﺝ ﺍﻷﺨـﺭﻯ ﺇﻟـﻰ ﻤﻨـﺎﻁﻕ ﺍﻟﻤﻌﺎﻟﺠـﺔ‬ ‫ﺃﻭﺍﻟﺘﻜﺭﻴﺭ ﻭﺍﻟﺘﺴﻭﻴﻕ ﻭﺫﻟﻙ ﺒﻜﻤﻴﺎﺕ ﻜﺒﻴﺭﺓ ﻭﻟﻤﺴﺎﻓﺎﺕ ﻁﻭﻴﻠﺔ.‬ ‫٣- ﺃﻨﻅﻤﺔ ﺍﻟﺘﻭﺯﻴﻊ ‪:Distribution Systems‬‬ ‫ﻴﺘﻡ ﻨﻘل ﺍﻟﻤﻨﺘﺠﺎﺕ ﺍﻟﺒﺘﺭﻭﻟﻴﺔ ﻤﻥ ﻤﺼﺎﺩﺭ ﺍﻹﻤﺩﺍﺩ ﻤﺜل ﻤﻌﺎﻤل‬ ‫ﺍﻟﺘﻜﺭﻴﺭ ﻭﺍﻟﻤﻭﺍﻨﻰ ﺍﻟﺒﺤﺭﻴﺔ ﺇﻟﻰ ﻤﻨـﺎﻁﻕ ﺍﻹﺴـﺘﻬﻼﻙ ﺃﺴﺎﺴـﺎ‬ ‫ﹰ‬ ‫ﺒﻭﺍﺴﻁﺔ ﺃﻨﻅﻤﺔ ﺨﻁ ﺍﻟﺘﻭﺯﻴـﻊ ‪Pipe Line Distribution‬‬ ‫‪ ،Systems‬ﻭﺘﻜﻭﻥ ﻤﻌﻅﻡ ﺍﻟﻤﻨﺘﺠﺎﺕ ﺍﻟﺒﺘﺭﻭﻟﻴﺔ ﻫـﻰ ﺃﻨـﻭﺍﻉ‬ ‫ﺍﻟﺒﻨﺯﻴﻥ ﺍﻟﻤﺨﺘﻠﻔﺔ، ﻭﻗﻭﺩ ﺍﻟﻨﻔﺎﺜـﺎﺕ، ﺍﻟﻜﻴﺭﻭﺴـﻴﻥ، ﺍﻟﺴـﻭﻻﺭ،‬ ‫ﺍﻟﻤﺎﺯﻭﺕ ﻭﻜﺫﻟﻙ ﺍﻟﺒﻭﺘﺎﺠﺎﺱ ﺍﻟﻤﺴﺎل ﻭﺘﺨﺘﻠﻑ ﺨﻁﻭﻁ ﺃﻨﺎﺒﻴـﺏ‬ ‫ﺍﻟﺘﻭﺯﻴﻊ ﻟﻠﻤﻨﺘﺠﺎﺕ ﻋﻥ ﺨﻁﻭﻁ ﺃﻨﺎﺒﻴﺏ ﺍﻟﺯﻴﺕ ﺍﻟﺨﺎﻡ ﻓـﻲ ﺃﻨﻬـﺎ‬ ‫ﻋﺎﺩﺓ ﺘﺒﺩﺃ ﻜﺄﻨﻅﻤﺔ ﺫﺍﺕ ﺴﻌﺎﺕ ﻜﺒﻴﺭﺓ ﻭﺘﺘﻔﺭﻉ ﺇﻟﻰ ﺃﻨﻅﻤـﺔ ﺫﺍﺕ‬ ‫ﺴﻌﺎﺕ ﺃﺼﻐﺭ ﻜﺈﻤﺩﺍﺩﺍﺕ ﻟﻠﻤﻭﺍﻗﻊ ﺍﻟﻤﺨﺘﻠﻔﺔ.‬ ‫- ٦٤ -‬
‫ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻼﺯﻡ ﻟﻤﺸﺭﻭﻉ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﺴﺘﻬﻠﻙ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻼﺯﻡ ﻟﻠﻤﺸﺭﻭﻉ ﺃﺴﺎﺴﺎ ﻓـﻲ ﺘﻜـﺎﻟﻴﻑ‬ ‫ﹰ‬ ‫ﺇﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﺃﻴﻀﺎ ﺘﻜﺎﻟﻴﻑ ﺇﻨﺸﺎﺀ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ.‬ ‫ﹰ‬ ‫١- ﺘﻜﺎﻟﻴﻑ ﺇﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﻌﺘﺒﺭ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻓـﻲ ﺇﻨﺸـﺎﺀ ﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫)ﺩﻭﻻﺭ/ﻁﻥ ﺃﻭ ﺩﻭﻻﺭ/ ﻜﻴﻠﻭﻤﺘﺭ( ﻴﺘﻨﺎﺴﺏ ﻤﻊ ﻭﺯﻥ ﻤﻭﺍﺴـﻴﺭ‬ ‫ﺍﻟﺨﻁ ﻭﻫﻭ ﻴﺴﺎﻭﻯ ﺜﻤﻥ ﺍﻟﻤﻭﺍﺴﻴﺭ = ﺃ × ﻭﺯﻥ ﺍﻟﻤﻭﺍﺴﻴﺭ، ﺤﻴﺙ‬ ‫ﺃﻥ ﺃ ﻤﻌﺎﻤل ﻭﺃﻥ ﻭﺯﻥ ﺍﻟﻤﻭﺍﺴﻴﺭ ﻴﻌﺘﻤﺩ ﻋﻠـﻰ ﻗﻁـﺭ ﻭﺴـﻤﻙ‬ ‫ﻭﻁﻭل ﻫﺫﻩ ﺍﻟﻤﻭﺍﺴﻴﺭ.‬ ‫٢- ﺘﻜﺎﻟﻴﻑ ﺇﻨﺸﺎﺀ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ:‬ ‫ﻴﻌﺘﺒﺭ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻓﻲ ﺇﻨﺸـﺎﺀ ﻤﺤﻁـﺔ ﻟﻠﻀـﺦ‬ ‫)ﺩﻭﻻﺭ/ ﺤﺼﺎﻥ( ﻴﺘﻨﺎﺴﺏ ﻤﻊ ﻗﺩﺭﺓ ﻫﺫﻩ ﺍﻟﻤﺤﻁﺔ ﻭﻫﻭ ﻴﺴـﺎﻭﻯ‬ ‫ﺍﻟﺜﻤﻥ ﺍﻷﺴﺎﺴﻰ ﻟﻠﻤﻀﺨﺎﺕ.‬ ‫- ٧٤ -‬
‫ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻤﺸﺭﻭﻉ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ:‬ ‫ﺘﻨﻘﺴﻡ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ ﺇﻟﻰ ﺍﻟﺒﻨﻭﺩ ﺍﻵﺘﻴﺔ :‬ ‫ﻤﺼﺎﺭﻴﻑ ﺍﻟﺘﺸـﻐﻴل ﻭﺍﻟﺼـﻴﺎﻨﺔ ﻟﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫١-‬ ‫ﻭﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﻭﺘﺸﻤل ﺇﺴﺘﻬﻼﻙ ﺍﻟﺘﻴﺎﺭ ﺍﻟﻜﻬﺭﺒـﺎﺌﻲ‬ ‫ﻭﺍﻟﻤﻴﺎﻩ ﻭﻗﻁﻊ ﺍﻟﻐﻴﺎﺭ ﻭﺍﻟﻭﻗﻭﺩ ﻭﺍﻟﺯﻴﻭﺕ، ﻭﺘﻜـﺎﻟﻴﻑ‬ ‫ﺃﻋﻤﺎل ﺍﻟﺼﻴﺎﻨﺔ ﺍﻟﺘﻲ ﺘﺘﻡ ﻋﻥ ﻁﺭﻴﻕ ﺍﻟﻐﻴﺭ.‬ ‫ﺍﻟﻤﺭﺘﺒﺎﺕ ﻭﺍﻷﺠﻭﺭ.‬ ‫٢-‬ ‫ﺍﻟﻀﺭﺍﺌﺏ ﻭﺍﻟﺘﺄﻤﻴﻨﺎﺕ ﻭﻤﺎ ﺸﺎﺒﻪ ﺫﻟﻙ.‬ ‫٣-‬ ‫ﻤﺼﺎﺭﻴﻑ ﺍﻹﻫﻼﻙ ﺍﻟﺴﻨﻭﻴﺔ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻤﺤﻁـﺎﺕ‬ ‫٤-‬ ‫ﺍﻟﻀﺦ ﻭﺘﻌﺭﻑ ﺒﺄﻨﻬﺎ ﻨﺴﺒﺔ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻹﻨﺸﺎﺀ‬ ‫ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻭ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﺇﻟﻰ ﺍﻟﻌﻤﺭ ﺍﻹﻓﺘﺭﺍﻀﻰ‬ ‫ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻭ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﺤﻴﺙ ﻴـﺘﻡ ﺤﺴـﺎﺏ‬ ‫ﻤﺼﺎﺭﻴﻑ ﺍﻹﻫﻼﻙ ﺍﻟﺴﻨﻭﻴﺔ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺘﻘﺴﻴﻡ ﺭﺃﺱ‬ ‫ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻹﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﻋﻠـﻰ ﺍﻟﻌﻤـﺭ‬ ‫ﺍﻹﻓﺘﺭﺍﻀﻰ ﻟﻠﺨﻁ )ﺤﻭﺍﻟﻰ ٣٣ ﻋﺎﻤـﺎ( ﻭﻜـﺫﻟﻙ ﻴـﺘﻡ‬ ‫ﹰ‬ ‫ﺤﺴﺎﺏ ﻤﺼﺎﺭﻴﻑ ﺍﻹﻫﻼﻙ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻤﺤﻁﺎﺕ ﺍﻟﻀـﺦ‬ ‫ﺒﺘﻘﺴﻴﻡ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻹﻨﺸﺎﺀ ﻤﺤﻁﺎﺕ ﺍﻟﻀـﺦ‬ ‫ﻋﻠﻰ ﺍﻟﻌﻤﺭ ﺍﻹﻓﺘﺭﺍﻀﻰ ﻟﻠﻤﻀﺨﺎﺕ )ﺤﻭﺍﻟﻰ ٥٢ ﻋﺎﻤﺎ(.‬ ‫ﹰ‬ ‫ﺃﻯ ﻤﺼﺭﻭﻓﺎﺕ ﺃﺨﺭﻯ ﻤﺜل ﺍﻟﻔﺎﺌﺩﺓ ﻋﻠﻰ ﺭﺃﺱ ﺍﻟﻤﺎل‬ ‫٥-‬ ‫ﺍﻟﻤﻘﺘﺭﺽ.‬ ‫- ٨٤ -‬
‫ﻭﺒﺫﻟﻙ ﻴﻤﻜﻥ ﺤﺴﺎﺏ ﺘﻜﻠﻔﺔ ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﻭﻫﻰ ﺘﺴﺎﻭﻯ‬ ‫ﺇﺠﻤﺎﻟﻰ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ‬ ‫ﺘﻜﻠﻔﺔ ﺍﻟﻨﻘل )ﺩﻭﻻﺭ/ﻁﻥ(‬ ‫)ﺩﻭﻻﺭ(‬ ‫=‬ ‫ﻜﻤﻴﺔ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭﻟﺔ ﻓﻲ ﺍﻟﻌﺎﻡ )ﻁﻥ(‬ ‫ﻭﺒﻨﺎﺀ ﻋﻠﻰ ﻤﺎ ﺴﺒﻕ ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﺴﻌﺭ ﻨﻘل ﺍﻟﺒﺘـﺭﻭل ﺒﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﺒﻀﺭﺏ ﺘﻜﻠﻔﺔ ﺍﻟﻨﻘل ﻓﻲ ﻤﻌﺎﻤل ﺒﺤﻴﺙ ﻻ ﻴﺘﻌﺩﻯ ﺴﻌﺭ‬ ‫ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﺒﺎﻟﻁﺭﻕ ﺍﻷﺨﺭﻯ ﻭﺘﻌﺘﻤﺩ ﻗﻴﻤﺔ ﻫﺫﺍ ﺍﻟﻤﻌﺎﻤل ﻋﻠـﻰ‬ ‫ﺃﺴﻌﺎﺭ ﺍﻟﻨﻘل ﻟﻠﺸﺭﻜﺎﺕ ﺍﻷﺨﺭﻯ ﺍﻟﻤﻨﺎﻓﺴﺔ‬ ‫ﺃﺴﺱ ﺇﺨﺘﻴﺎﺭ ﻗﻁﺭ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ:‬ ‫ﻴﻌﺘﻤﺩ ﺇﺨﺘﻴﺎﺭ ﻗﻁﺭ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻋﻠﻰ ﻋﻤل ﺩﺭﺍﺴﺔ ﺘﺸـﻤل‬ ‫ﺍﻵﺘﻲ:‬ ‫١- ﺤﺴﺎﺏ ﺘﻜﺎﻟﻴﻑ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ، ﻭﻫﻰ ﻜﻤـﺎ ﺒﺎﻟﺸـﻜل‬ ‫)١١( ﻤﻨﺤﻨﻰ ١ ﺘﺯﺩﺍﺩ ﺒﺯﻴﺎﺩﺓ ﻗﻁﺭ ﺍﻟﺨﻁ.‬ ‫٢- ﺤﺴﺎﺏ ﺘﻜﺎﻟﻴﻑ ﻭﺤﺩﺍﺕ ﺍﻟﻀﺦ ﻭﻫﻰ ﻜﻤﺎ ﻨﺭﻯ ﻤﻨﺤﻨﻰ‬ ‫٢ ﺘﻘل ﺒﺯﻴﺎﺩﺓ ﻗﻁﺭ ﺍﻟﺨﻁ.‬ ‫- ٩٤ -‬
‫ﻭﺒﺠﻤﻊ ﺍﻟﻤﻨﺤﻨﻴﻴﻥ ١، ٢ ﻨﺤﺼل ﻋﻠـﻰ ﺍﻟﺘﻜـﺎﻟﻴﻑ ﺍﻟﻜﻠﻴـﺔ‬ ‫ﺍﻟﺴﻨﻭﻴﺔ ﻤﻨﺤﻨﻰ ٣ ﻭﺍﻟﻘﻁﺭ ﺍﻷﻤﺜل ﺇﻗﺘﺼﺎﺩﻴﺎ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻫـﻭ‬ ‫ﹰ‬ ‫ﺍﻟﻘﻁﺭ ﺍﻟﺫﻯ ﻟﻪ ﺃﻗل ﺘﻜﻠﻔﺔ ﻜﻠﻴﺔ ﻭﻗﺩ ﻭﺠﺩ ﺃﻥ ﺍﻟﺴﺭﻋﺔ ﺍﻟﻤﻨﺎﺴـﺒﺔ‬ ‫ﻟﻠﺴﻭﺍﺌل ﻓﻲ ﺍﻷﻨﺎﺒﻴﺏ ﻓﻲ ﻫـﺫﻩ ﺍﻟﺤﺎﻟـﺔ ﺘﺘـﺭﺍﻭﺡ ﺒـﻴﻥ ١:٣‬ ‫ﻤﺘﺭ/ﺜﺎﻨﻴﺔ.‬ ‫ﻭﻴﺘﻀﺢ ﻤﻥ ﺍﻟﺨﺒﺭﺓ ﺍﻟﻌﻤﻠﻴـﺔ ﺃﻥ ﺍﻟﺴـﺭﻋﺔ ﺘﻘﺘـﺭﺏ ﻤـﻥ‬ ‫١ﻤﺘﺭ/ﺜﺎﻨﻴﺔ ﻟﻠﺴﻭﺍﺌل ﻤﺭﺘﻔﻌﺔ ﺍﻟﻠﺯﻭﺠﺔ ﻭﺃﻴﻀـﺎ ﺘﻘﺘـﺭﺏ ﻤـﻥ‬ ‫ﹰ‬ ‫٣ﻤﺘﺭ/ﺜﺎﻨﻴﺔ ﻟﻠﺴﻭﺍﺌل ﻤﻨﺨﻔﻀﺔ ﺍﻟﻠﺯﻭﺠﺔ ﻭﻴﻌﺘﺒﺭ ﻫـﺫﺍ ﺍﻟﻤـﺩﻯ‬ ‫ﻟﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﺍﻟﺴﻭﺍﺌل ﺩﺍﺨل ﺍﻷﻨﺎﺒﻴﺏ ﻫﻭ ﺍﻟﻘﻴﺩ ﻟﺭﻓﻊ ﻜﻔـﺎﺀﺓ‬ ‫ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ.‬ ‫ﻭﻋﻨﺩ ﺇﺨﺘﻴﺎﺭ ﻗﻁﺭ ﺨﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﻴﺠـﺏ ﺃﻥ ﻴﺅﺨـﺫ ﻓـﻲ‬ ‫ﺍﻹﻋﺘﺒﺎﺭ ﻤﻌﺎﻤل ﺍﻟﺨﺩﻤـﺔ ‪ Service Factor‬ﻟﺨﻁـﺔ ﺍﻟﻨﻘـل‬ ‫ﺍﻟﺴﻨﻭﻴﺔ ﻭﻫﻭ ﻴﻜﻭﻥ ﻓﻲ ﺤﺩﻭﺩ ٢٨% ﺒﻤﻌﻨﻰ ﺃﻥ ﻴﺘﻡ ﻨﻘل ﺍﻟﻜﻤﻴﺔ‬ ‫ﺍﻟﻤﻁﻠﻭﺒﺔ ﺴﻨﻭﻴﺎ ﺨﻼل ٠٠٣ ﻴﻭﻡ ﻓﻘﻁ ﻭﺫﻟﻙ ﺤﺘـﻰ ﻻ ﻴـﺅﺜﺭ‬ ‫ﹰ‬ ‫ﺇﻴﻘﺎﻑ ﺍﻟﺨﻁ ﻷﻯ ﺴﺒﺏ ﻋﻠﻰ ﺘﺤﻘﻴﻕ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟـﺔ ﺴـﻨﻭﻴﺎ‬ ‫ﹰ‬ ‫ﻭﻟﺫﻟﻙ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺘﺴﺎﻭﻯ‬ ‫- ٠٥ -‬
‫ﺸﻜل )١١(‬ ‫6 01 × ) ‪(million ton / year‬‬ ‫=‪Q‬‬ ‫‪7200 × sp.gr‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ sp.gr‬ﻫﻰ ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ ﻟﻠﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺒﺎﻟﺨﻁ‬ ‫ﻭﺃﻴﻀﺎ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌـﺏ ﻓـﻲ ﺍﻟﺴـﺎﻋﺔ‬ ‫ﹰ‬ ‫ﺘﺴﺎﻭﻯ 2‪. Q = ١,٨٢٤ Di‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ V‬ﻫﻰ ﺴﺭﻋﺔ ﺍﻟﺴﺎﺌل ﺩﺍﺨل ﺍﻟﺨﻁ ﺒﺎﻟﻤﺘﺭ/ﺜﺎﻨﻴﺔ.‬ ‫- ١٥ -‬
‫‪ Di‬ﻫﻭ ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺒﻭﺼﺔ، ﻭﻤﻤﺎ ﺴﺒﻕ‬ ‫ﻴﺘﻀﺢ ﺃﻨﻪ ﻟﻜﻲ ﻴﺘﻡ ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﺒﺼﻭﺭﺓ ﺇﻗﺘﺼـﺎﺩﻴﺔ ﺒﻤﻌﻨـﻰ‬ ‫ﺘﺤﻘﻴﻕ ﺃﻗل ﺘﻜﻠﻔﺔ ﻜﻠﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ ﻴﻜﻭﻥ ﺍﻟﺤﺩ ﺍﻷﺩﻨـﻰ ﻟﻠﻜﻤﻴـﺔ‬ ‫ﺍﻟﻤﻨﻘﻭﻟﺔ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺘﺴـﺎﻭﻯ 2‪Qmin = 1.824 Di‬‬ ‫ﻭﺃﻴﻀﺎ ﺒﻬﺩﻑ ﺭﻓﻊ ﻜﻔﺎﺀﺓ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻴﻜﻭﻥ ﺍﻟﺤـﺩ ﺍﻷﻗﺼـﻰ‬ ‫ﹰ‬ ‫ﻟﻠﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺘﺴﺎﻭﻯ 2‪. Qmax = 5.472 Di‬‬ ‫ﺍﻟﻌﻭﺍﻤل ﺍﻟﻤﺅﺜﺭﺓ ﻋﻠﻰ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﻜﻠﻴﺔ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل‬ ‫ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﺘﻀﺢ ﻤﻤﺎ ﺴﺒﻕ ﺃﻥ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺘﻨﺨﻔﺽ ﺒﺯﻴﺎﺩﺓ‬ ‫ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺴﻨﻭﻴﺎ ﻭﺃﻥ ﻤﺴﺎﻓﺔ ﺍﻟﻨﻘل ﻟﻬﺎ ﺘﺄﺜﻴﺭ ﻗﻠﻴل ﺠـﺩﺍ،‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﻭﻗﺩ ﺘﺨﺘﻠﻑ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺒﺈﺨﺘﻼﻑ ﻤﻭﺍﺼﻔﺎﺕ ﺍﻟﺴﺎﺌل‬ ‫ﺍﻟﻤﻨﻘﻭل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻨﺫﻜﺭ ﻋﻠﻰ ﺴـﺒﻴل ﺍﻟﻤﺜـﺎل ﺍﻟﻌﻭﺍﻤـل‬ ‫ﺍﻵﺘﻴﺔ:‬ ‫١- ﺘﺼﺒﺢ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺃﻗل ﻤﺎ ﻴﻤﻜﻥ ﻋﻨﺩ ﻨﻘل‬ ‫ﺴﺎﺌل ﻭﺍﺤﺩ ﺫﻭ ﻟﺯﻭﺠﺔ ﻤﻨﺨﻔﻀﺔ ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ.‬ ‫- ٢٥ -‬
‫٢- ﺘﺯﺩﺍﺩ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﺍﻟـﺫﻯ‬ ‫ﻴﻨﻘل ﺴﻭﺍﺌل ﻤﺘﻌﺩﺩﺓ ﺒﺴـﺒﺏ ﺍﻟﺘﺭﻜﻴﺒـﺎﺕ ﺍﻹﻀـﺎﻓﻴﺔ‬ ‫ﻭﺍﻟﺨﻁﻭﻁ ﺍﻟﻔﺭﻋﻴﺔ.‬ ‫٣- ﺘﺯﺩﺍﺩ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﻤﻌﺯﻭل‬ ‫ﺤﺭﺍﺭﻴﺎ ﺒﺴﺒﺏ ﺃﻋﺒﺎﺀ ﺘﻜﺎﻟﻴﻑ ﺍﻟﻌﺯل ﺍﻟﺤﺭﺍﺭﻯ ﻟﻠﺨﻁ‬ ‫ﹰ‬ ‫ﻭﺘﻜﺎﻟﻴﻑ ﺯﻴﺎﺩﺓ ﻋﻤﻕ ﺍﻟﺨﻁ ﺘﺤﺕ ﺍﻷﺭﺽ ﻋﻥ ﺍﻟﻌﻤﻕ‬ ‫ﺍﻟﻁﺒﻴﻌﻰ ﻭﺘﻜﺎﻟﻴﻑ ﺘﺴﺨﻴﻥ ﺍﻟﺴﺎﺌل ﻭﺃﻴﻀـﺎ ﺇﺭﺘﻔـﺎﻉ‬ ‫ﹰ‬ ‫ﺍﻟﻘﺩﺭﺓ ﺍﻟﻼﺯﻤﺔ ﻟﻀﺦ ﺍﻟﺴﺎﺌل ﺍﻟﻠﺯﺝ.‬ ‫ﺘﺼﻤﻴﻡ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻟﺘﺼﻤﻴﻡ ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﻴﺠﺏ ﺃﻭﻻ ﺘﺤﺩﻴﺩ ﺍﻟﺒﻴﺎﻨﺎﺕ ﺍﻵﺘﻴﺔ :‬ ‫ﹰ‬ ‫١- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﻤﺩﻯ ﻟﻠﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﺃﻯ ﺍﻟﻜﻤﻴـﺔ‬ ‫ﺍﻟﻤﺒﺩﺌﻴ ـﺔ ﻭﺍﻟﻘﺼ ـﻭﻯ ‪Initial And Ultimate‬‬ ‫ـ‬ ‫ـ‬ ‫‪Throughput‬‬ ‫٢- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﺍﻟﻀﻐﻁ ﺍﻵﻤﻥ ﺍﻟﺫﻯ ﻴﺘﺤﻤﻠﻪ ﻤﻌـﺩﻥ ﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﻭﻓﻲ ﺃﻏﻠﺏ ﺍﻷﺤﻴﺎﻥ ﻴﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻀﻐﻁ ﻓـﻲ‬ ‫ﺤﺩﻭﺩ ٠٧ﻜﺠﻡ/ﺴﻡ٢.‬ ‫- ٣٥ -‬
‫٣- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﺍﻟﻀﻐﻁ ﻋﻨﺩ ﻨﻬﺎﻴـﺔ ﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﺃﻯ‬ ‫ﺍﻟﻀﻐﻁ ﻋﻨﺩ ﻤﺤﻁﺔ ﺍﻹﺴﺘﻼﻡ ﻭﻫﻭ ﻴﻜﻭﻥ ﻓﻲ ﺤـﺩﻭﺩ‬ ‫٢ﻜﺠﻡ/ﺴﻡ٢.‬ ‫٤- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﻁﻭل ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻯ ﺍﻟﻤﺴﺎﻓﺔ ﺒﻴﻥ ﻤﺤﻁﺔ‬ ‫ﺍﻟﺘﺩﻓﻴﻊ ﻭﻤﺤﻁﺔ ﺍﻹﺴﺘﻼﻡ.‬ ‫ﺨﻁﻭﺍﺕ ﺍﻟﺘﺼﻤﻴﻡ :‬ ‫١- ﻴﺘﻡ ﺤﺴﺎﺏ ﻤﺩﻯ ﻷﻗﻁﺎﺭ ﺍﻟﺨﻁﻭﻁ ﺍﻟﺘـﻲ ﺘﺴـﺘﻭﻋﺏ‬ ‫ﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬـﺎ ﺃﻯ ﺍﻟﺤـﺩ ﺍﻷﺩﻨـﻰ‬ ‫ﻭﺍﻷﻗﺼﻰ ﻷﻗﻁﺎﺭ ﺍﻟﺨﻁﻭﻁ، ﻭﺒﻤﺎ ﺃﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ‬ ‫ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺘﺴﺎﻭﻯ 2‪Q = 1.842V Di‬‬ ‫ﻓﻴﻜﻭﻥ ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺒﻭﺼﺔ ﻴﺴﺎﻭﻯ‬ ‫= ‪ Di‬ﺤﻴﺙ ﺃﻥ ‪ V‬ﻫﻰ ﺴﺭﻋﺔ ﺍﻟﺴـﺎﺌل‬ ‫‪Q‬‬ ‫‪1.824V‬‬ ‫ﺩﺍﺨل ﺍﻟﺨﻁ ﺒﺎﻟﻤﺘﺭ/ﺜﺎﻨﻴﺔ، ﻭﻹﻴﺠﺎﺩ ﺍﻟﺤﺩ ﺍﻷﺩﻨﻰ ﻟﻠﻘﻁﺭ‬ ‫ﺍﻟ ـﺩﺍﺨﻠﻰ ﻨﻀ ـﻊ ﺍﻟﻜﻤﻴ ـﺔ ﺍﻟﻘﺼ ـﻭﻯ ‪Ultimate‬‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫‪ Throughput‬ﻭﺃﻴﻀﺎ ‪ V=٣mt/sec‬ﻓﻲ ﺍﻟﻤﻌﺎﺩﻟﺔ‬ ‫ﹰ‬ ‫ﺍﻟﺴﺎﺒﻘﺔ‬ ‫‪Qult‬‬ ‫= ‪Minimum Di‬‬ ‫3 × 428.1‬ ‫- ٤٥ -‬
‫ﻭﻜﺫﻟﻙ ﻹﻴﺠﺎﺩ ﺍﻟﺤﺩ ﺍﻷﻗﺼﻰ ﻟﻠﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻨﻀﻊ ﺍﻟﻜﻤﻴـﺔ‬ ‫ـﺎ ٥,١=‪V‬‬ ‫ـﻭﻯ ‪ Ultimate Throughput‬ﻭﺃﻴﻀـ ﹰ‬ ‫ﺍﻟﻘﺼـ‬ ‫‪ mt/sec‬ﻓﻲ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺍﻟﺴﺎﺒﻘﺔ‬ ‫‪Qult‬‬ ‫= ‪Maximum Di‬‬ ‫5.1× 428.1‬ ‫٢- ﻴﺘﻡ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﺃﻯ ﺘﻘﺭﻴﺒﺎ ﻓﺎﻗـﺩ ﺍﻟﻀـﻐﻁ‬ ‫ﹰ‬ ‫ﺍﻟﻤﺭﺘﺒﻁ ﺒﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﻭﺫﻟﻙ ﻟﻤـﺩﻯ‬ ‫ﺍﻷﻗﻁﺎﺭ ﺍﻟﺘﻲ ﺘﻡ ﺇﺨﺘﻴﺎﺭﻫﺎ ﻓﻲ ﺍﻟﺨﻁﻭﺓ ﺍﻟﺴﺎﺒﻘﺔ ﻋـﻥ‬ ‫ﻁﺭﻴﻕ ﻤﻌﺎﺩﻟﺔ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜـﺎﻙ ﺁﺨـﺫﺍ ﻓـﻲ‬ ‫ﹰ‬ ‫ﺍﻹﻋﺘﺒﺎﺭ ﺍﻟﻤﻌﻁﻴﺎﺕ.‬ ‫- ٥٥ -‬
‫٣- ﻴﺘﻡ ﺘﺴﺠﻴل ﻨﺘﺎﺌﺞ ﺍﻟﺤﺴﺎﺒﺎﺕ ﻓﻲ ﺠﺩﻭل ﻜﺎﻵﺘﻲ :‬ ‫ﺭﺃﺱ‬ ‫ﺍﻟﻤﺎل‬ ‫ﻓﺎﻗﺩ‬ ‫ﺃﻗل‬ ‫ﺘﻜﺎﻟﻴﻑ‬ ‫ﺍﻟﻜﻤﻴﺔ‬ ‫ﺍﻟﻼﺯﻡ‬ ‫ﺘﻜﺎﻟﻴﻑ‬ ‫ﺇﺠﻬﺎﺩ ﺍﻟﻀﻐﻁ‬ ‫ﺇﻨﺸﺎﺀ‬ ‫ﺍﻟﻤﻨﻘﻭﻟﺔ‬ ‫ﺍﻟﻘﻁﺭ‬ ‫ﻹﻨﺸﺎﺀ‬ ‫ﺇﻨﺸﺎﺀ‬ ‫ﺨﻀﻭﻉ ﻋﻠﻰ‬ ‫ﻤﺤﻁﺎﺕ‬ ‫ﺒﺎﻟﻤﺘﺭ‬ ‫ﺴﻤﻙ ﺍﻟﺩﺍﺨﻠﻰ‬ ‫ﺨﻁ‬ ‫ﺨﻁ‬ ‫ﻟﻤﻌﺩﻥ ﻁﻭل‬ ‫ﻗﻁﺭ ﺍﻟﺨﻁ‬ ‫ﺍﻟﻀﺦ‬ ‫ﺍﻟﻤﻜﻌﺏ‬ ‫ﺍﻟﺨﻁ ﻟﻠﺨﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ‬ ‫ﺍﻟﻤﻭﺍﺴ ﺍﻟﺨﻁ‬ ‫-١‪α(P‬‬ ‫ﻓﻲ‬ ‫‪Di‬‬ ‫ﻭﻤﺤﻁﺎ‬ ‫‪α Di‬‬ ‫ﻴﺭ ‪(P١- min‬‬ ‫)٢‪P‬‬ ‫ﺍﻟﺴﺎﻋﺔ‬ ‫ﺕ‬ ‫)٢‪P‬‬ ‫‪σy‬‬ ‫ﺍﻟﻀﺦ‬ ‫- ٦٥ -‬
‫ﻭﻴﻤﻜﻥ ﺍﻟﺘﺤﻜﻡ ﻓﻲ ﺍﻟﻌﻭﺍﻤل ﺍﻟﻤﺘﻐﻴﺭﺓ ﻤﺜل ﻗﻁﺭ ﺍﻟﺨﻁ ﻭﻓﺎﻗﺩ‬ ‫ﺍﻟﻀﻐﻁ ﻋﻠﻰ ﻁﻭل ﺍﻟﺨﻁ ﺒﻬﺩﻑ ﺇﻴﺠﺎﺩ ﺃﻗل ﻗﻴﻤﺔ ﻤﻤﻜﻨﺔ ﻟـﺭﺃﺱ‬ ‫ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺨﺩﻡ ﻹﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﻋﻠﻤـﺎ‬ ‫ﹰ‬ ‫ﺒﺄﻥ ﻤﻌﻅﻡ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺨﺩﻡ ﻴﺴﺘﻬﻠﻙ ﻓـﻲ ﺇﻨﺸـﺎﺀ ﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﻨﻔﺴﻪ، ﻭﻗﺩ ﻴﺘﻀﺢ ﺃﻨﻪ ﻟﺘﺼﻤﻴﻡ ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺒﺄﻗل ﺭﺃﺱ‬ ‫ﻤﺎل ﻓﺈﻨﻪ ﻴﺠﺏ ﺇﺨﺘﻴﺎﺭ ﺍﻟﻤﻭﺍﺴﻴﺭ ﺫﺍﺕ ﺍﻷﻗﻁﺎﺭ ﺍﻟﺼﻐﻴﺭﺓ ﻭﻓـﻲ‬ ‫ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻓﺈﻥ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﻗﺩ ﺘﻜﻭﻥ ﻤﺘﻘﺎﺭﺒﺔ ﻭﻫﺫﺍ ﻴﺤﻘـﻕ‬ ‫ﺃﻋﻠﻰ ﺇﺴﺘﻔﺎﺩﺓ ﻤﻥ ﺍﻹﺴﺘﺜﻤﺎﺭﺍﺕ ﺍﻟﻤﺩﻓﻭﻋﺔ ﻓﻲ ﺃﻯ ﻭﻗـﺕ ﻓـﻭﺭ‬ ‫ﻀﺦ ﻫﺫﻩ ﺍﻹﺴﺘﺜﻤﺎﺭﺍﺕ ﻭﻴﺠﺏ ﺃﻥ ﻨﺘﻼﻗﻰ ﻀﺦ ﺃﻯ ﺇﺴﺘﺜﻤﺎﺭﺍﺕ‬ ‫ﻏﻴﺭ ﻀﺭﻭﺭﻴﺔ ﻤﺒﻜﺭﺍ ﺤﻴﺙ ﺃﻨﻪ ﻴﺘﺴﺒﺏ ﻓﻲ ﻋﺩﻡ ﺍﻹﺴﺘﻔﺎﺩﺓ ﻤﻥ‬ ‫ﹰ‬ ‫ﻫﺫﻩ ﺍﻹﺴﺘﺜﻤﺎﺭﺍﺕ ﻋﺩﺓ ﺴﻨﻭﺍﺕ.‬ ‫ﻤﺜﺎل ﻋﻠﻰ ﺘﺼﻤﻴﻡ ﺨﻁ ﺃﻨﺎﺒﻴﺏ :‬ ‫ﻤﻁﻠﻭﺏ ﻨﻘل ﺴﺎﺌل ﻟﻤﺴﺎﻓﺔ ﻗﺩﺭﻫﺎ ٠٩١ﻜﻴﻠﻭ ﻤﺘـﺭ ﻭﺒﻜﻤﻴـﺔ‬ ‫ﻗﺩﺭﻫﺎ ٢ ﻤﻠﻴﻭﻥ ﻁﻥ ﺴﻨﻭﻴﺎ ﺴﻭﻑ ﺘﺯﺩﺍﺩ ﻤﺴﺘﻘﺒﻼ ﺇﻟﻰ ٥ ﻤﻠﻴﻭﻥ‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﻁﻥ ﺴﻨﻭﻴﺎ.‬ ‫ﹰ‬ ‫- ٧٥ -‬
‫ﺍﻟﺤل : ﻨﺤﺴﺏ ﺃﻭﻻ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﺒﺩﺌﻴﺔ ﻭﺍﻟﻘﺼﻭﻯ ﺍﻟﻤﻁﻠـﻭﺏ‬ ‫ﹰ‬ ‫ﻨﻘﻠﻬﺎ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺒﻔﺭﺽ ﺃﻥ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻁﻠـﻭﺏ‬ ‫6 01 × 2‬ ‫‪Q Initial‬‬ ‫= ‪= 2 × 10 ton / year‬‬ ‫6‬ ‫ﻨﻘﻠﻪ ﻫﻭ ﺍﻟﻤﺎﺀ.‬ ‫‪7200sp.gr‬‬ ‫‪Qinitial= ٢٧٧,٧٧ mt٣/hr‬‬ ‫6 01 × 5‬ ‫= ‪QUltimate = 5 × 10 6 ton / year‬‬ ‫‪= 694.44mt 3 / hr‬‬ ‫‪7200sp.gr‬‬ ‫ﺜﻡ ﻨﺤﺴﺏ ﺍﻟﺤﺩ ﺍﻷﺩﻨﻰ ﻭﺍﻷﻗﺼﻰ ﻷﻗﻁﺎﺭ ﺍﻟﺨﻁﻭﻁ ﺍﻟﺘـﻲ‬ ‫ﺘﺴﺘﻭﻋﺏ ﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ‬ ‫44. 496‬ ‫= ‪min .D i‬‬ ‫‪= 11 .265 inch‬‬ ‫274. 5‬ ‫44. 496‬ ‫= ‪max .D i‬‬ ‫‪= 15 .93 inch‬‬ ‫637. 2‬ ‫ﻭﻤﻤﺎ ﺴﺒﻕ ﻨﺴﺘﻨﺘﺞ ﺃﻥ ﺃﺩﻨﻰ ﻭﺃﻗﺼﻰ ﻗﻁﺭ ﻟﻨﻘل ﻫﺫﺍ ﺍﻟﻤـﺩﻯ‬ ‫ﻤﻥ ﺍﻟﻜﻤﻴﺎﺕ ﻴﺴﺎﻭﻯ٢١، ٦١ ﺒﻭﺼﺔ ﻋﻠﻰ ﺍﻟﺘـﻭﺍﻟﻰ، ﻭﺒـﺫﻟﻙ‬ ‫ﻴﻤﻜﻥ ﺇﺨﺘﻴﺎﺭ ٣ ﺃﻗﻁﺎﺭ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﻼﺯﻡ ﻟﻨﻘل ﻫﺫﺍ ﺍﻟﻤـﺩﻯ‬ ‫ﻤﻥ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﻭﻫﺫﻩ ﺍﻷﻗﻁﺎﺭ ﻫﻰ ٢١ ﺒﻭﺼـﺔ،‬ ‫٤١ ﺒﻭﺼﺔ ﻭ٦١ ﺒﻭﺼﺔ.‬ ‫- ٨٥ -‬
‫: ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺒﻘﻁﺭ ٢١ ﺒﻭﺼﺔ ﺒﻤﺤﻁﺔ ﻀﺦ ﻭﺍﺤﺩﺓ‬ ‫ﺃﻭﻻ‬ ‫ﹰ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ ﻭﻴـﺘﻡ ﺇﻀـﺎﻓﺔ ﻤﺤﻁـﺔ ﻀـﺦ‬ ‫ﻤﺴﺎﻋﺩﺓ ﻓﻲ ﻤﻨﺘﺼﻑ ﺍﻟﻁﻭل ﺘﻘﺭﻴﺒﺎ ﻓﻴﻤﺎ ﺒﻌﺩ ﺜﻡ ﺒﻌـﺩ‬ ‫ﹰ‬ ‫ﺫﻟﻙ ﻴﺘﻡ ﺇﻀﺎﻓﺔ ﻋﺩﺩ ٢ ﻤﺤﻁﺔ ﻀﺦ ﻤﺴﺎﻋﺩﺓ ﻋﻠـﻰ‬ ‫ﻤﺴﺎﻓﺔ ﺭﺒﻊ ﻁﻭل ﺍﻟﺨﻁ ﺘﻘﺭﻴﺒﺎ ﻤﻥ ﺒﺩﺍﻴﺘـﻪ ﻭﻨﻬﺎﻴﺘـﻪ‬ ‫ﹰ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ‬ ‫ﻭﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻴﺘﻡ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﺃﻯ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ‬ ‫ﺍﻟﻤﺭﺘﺒﻁ ﺒﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﻜﺎﻵﺘﻲ :‬ ‫ﻟﻠﺨﻁ ٢١ ﺒﻭﺼﺔ ‪ Standard weight‬ﺴـﻤﻙ ﺍﻟﺨـﻁ =‬ ‫٥٧٣,٠ ﺒﻭﺼﺔ‬ ‫‪Di=١٢,٧٥ – ٢ (٠,٣٧٥) = ١٢// and L = ١٩٠ kmt‬‬ ‫١( ﻟﻠﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ ‪QI=٢٧٧,٧٧ m٣/hr‬‬ ‫77.772‬ ‫=‪V‬‬ ‫‪= 1.057mt / sec‬‬ ‫2 )21(428.1‬ ‫ﺒﺘﻁﺒﻴﻕ ﻤﻌﺎﺩﻟﺔ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻟﻠﺴﺭﻴﺎﻥ ﺍﻟﻤﻀﻁﺭﺏ‬ ‫ﺩﺍﺨل ﺍﻷﻨﺎﺒﻴﺏ‬ ‫57.1 77.772)091( 52.01‬ ‫× 5245.71 = ‪h f‬‬ ‫‪= 471.2mt‬‬ ‫57.4 21‬ ‫- ٩٥ -‬
‫ﻭﺒﺫﻟﻙ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓﻲ ﺼـﻭﺭﺓ ﻀـﻐﻁ ﻴﺴـﺎﻭﻯ‬ ‫‪sp.gr‬‬ ‫× 2.174‬ ‫2 ‪= 47.12kg / cm‬‬ ‫01‬ ‫ﻭﻴﺘﻀﺢ ﻤﻤﺎ ﺴﺒﻕ ﺃﻨﻪ ﻴﻜﻔﻲ ﺘﺭﻜﻴﺏ ﻤﺤﻁﺔ ﻀﺦ ﻭﺍﺤﺩﺓ ﻓﻲ‬ ‫ﺒﺩﺍﻴﺔ ﺍﻟﺨﻁ ﻭﺫﻟﻙ ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ.‬ ‫٢( ﻟﻠﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ ‪Qu = ٦٩٤,٤٤ m٣/hr‬‬ ‫ﻨﻜﺭﺭ ﻨﻔﺱ ﺍﻟﺨﻁﻭﺍﺕ ﺍﻟﺴﺎﺒﻘﺔ:‬ ‫‪V = ٢,٦٤ mt/sec‬‬ ‫٢‪hf = ٢٣٤,٢ kg/cm‬‬ ‫ﻭﺤﻴﺙ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ ﻴﺘﻌﺩﻯ ﺍﻟﻀﻐﻁ ﺍﻵﻤﻥ ﺍﻟﺫﻯ ﻴﺘﺤﻤﻠﻪ‬ ‫ﻤﻌﺩﻥ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ، ﻟﺫﻟﻙ ﻴﻜﻭﻥ ﻋﺩﺩ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﺍﻟﻤﻁﻠﻭﺒﺔ‬ ‫ﻭﻤﻤـﺎ ﺴـﺒﻕ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ ﻴﺴﺎﻭﻯ 643.3 =‬ ‫2.432‬ ‫07‬ ‫ﻴﺘﻀﺢ ﺃﻨﻪ ﻴﺠﺏ ﺘﺭﻜﻴﺏ ٤ ﻤﺤﻁﺎﺕ ﻀﺦ ﻋﻠﻰ ﻁـﻭل ﺍﻟﺨـﻁ‬ ‫ﻭﺫﻟﻙ ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ.‬ ‫: ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺒﻘﻁﺭ ٤١ ﺒﻭﺼﺔ ﺒﻤﺤﻁﺔ ﻀﺦ ﻭﺍﺤﺩﺓ‬ ‫ﺜﺎﻨﻴﺎ‬ ‫ﹰ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ ﺜﻡ ﺒﻌﺩ ﺫﻟﻙ ﻴﺘﻡ ﺇﻀﺎﻓﺔ ﻤﺤﻁـﺔ‬ ‫ﻀﺦ ﻤﺴﺎﻋﺩﺓ ﻓﻲ ﻤﻨﺘﺼﻑ ﻁﻭل ﺍﻟﺨﻁ ﺘﻘﺭﻴﺒﺎ ﻟﻨﻘـل‬ ‫ﹰ‬ ‫ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ.‬ ‫- ٠٦ -‬
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  • 1.
  • 3. ‫ﻃﺒﻘﺎ ﻟﻘﻮﺍﻧﲔ ﺍﳌﻠﻜﻴﺔ ﺍﻟﻔﻜﺮﻳﺔ‬ ‫א‬ ‫א‬ ‫א‬ ‫.‬ ‫אא‬ ‫א‬ ‫)ﻋـﱪ ﺍﻻﻧﱰﻧـﺖ ﺃﻭ‬ ‫א‬ ‫אא‬ ‫ﻟﻠﻤﻜﺘﺒــﺎﺕ ﺍﻻﻟﻜﱰﻭﻧﻴــﺔ ﺃﻭ ﺍﻷﻗــﺮﺍﺹ ﺍﳌﺪﳎــﺔ ﺃﻭ ﺍﻯ‬ ‫א‬ ‫ﻭﺳﻴﻠﺔ ﺃﺧﺮﻯ (‬ ‫א‬ ‫א‬ ‫.‬ ‫.‬ ‫א א‬
  • 4. ‫‪‬‬ ‫:ﺍﻟﻨﻅﺭﻴﺎﺕ ﺍﻷﺴﺎﺴﻴﺔ ﻓﻲ ﺍﻟﺘﺼﻤﻴﻤﺎﺕ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴﺔ - ٦ -‬ ‫ﺍﻟﺒﺎﺏ ﺍﻷﻭل‬ ‫: ﺘﺼﻤﻴﻡ ﺨﻁﻭﻁ ﺃﻨﺎﺒﻴﺏ ﻨﻘل ﺍﻟﺒﺘﺭﻭل .......... - ٣٤ -‬ ‫ﺍﻟﺒﺎﺏ ﺍﻟﺜﺎﻨﻲ‬ ‫ﺍﻟﺒﺎﺏ ﺍﻟﺜﺎﻟﺙ : ﺘﻁﺒﻴﻘﺎﺕ ﻋﻠﻰ ﺍﻟﺘﺼﻤﻴﻤﺎﺕ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴﺔ ...... - ٧٧ -‬ ‫ﺍﻟﺒﺎﺏ ﺍﻟﺭﺍﺒﻊ : ﺘﺼﻤﻴﻡ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ ................... - ٢١١ -‬ ‫-٣-‬
  • 6. ‫‪‬‬ ‫ﻤﻨﺫ ﻋﺩﺓ ﺴﻨﻭﺍﺕ ﻭﺍﻟﺤﺎﺠﺔ ﻤﺎﺴﺔ ﺇﻟـﻰ ﺒﺤـﺙ ﻤﺘﺨﺼـﺹ‬ ‫ﻴﺘﻨﺎﻭل ﻤﻭﻀﻭﻉ ﺍﻟﺘﺼﻤﻴﻤﺎﺕ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴﺔ ﻟﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫ﻭﺘﻁﺒﻴﻘﺎﺘﻬﺎ ﻓﻲ ﻤﺠﺎل ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﻭﻗﺩ ﺃﻋﺩﺩﺕ ﻫﺫﺍ ﺍﻟﺒﺤﺙ ﺁﻤﻼ‬ ‫ﹰ‬ ‫ﺃﻥ ﻴﻭﻀﺢ ﺍﻟﻤﻭﻀﻭﻋﺎﺕ ﺍﻟﺘﻲ ﻗﺩ ﺘﻜﻭﻥ ﻤﺒﻬﻤﺔ ﻓﻲ ﻫﺫﺍ ﺍﻟﻤﺠﺎل‬ ‫ﻜﻤﺎ ﺃﻥ ﺇﺤﺘﻭﺍﺀ ﻫﺫﺍ ﺍﻟﺒﺤﺙ ﻋﻠﻰ ﺒﻌﺽ ﺍﻟﻤﻌﺎﺩﻻﺕ ﻭﺍﻟﺠـﺩﺍﻭل‬ ‫ﻭﺍﻟﻘﻭﺍﻋ ـﺩ ﺍﻟﻬﻴﺩﺭﻭﻟﻴﻜﻴ ـﺔ ﺍﻟﻤﺴ ـﺘﻨﺘﺠﺔ ﺒﻤﻌﺭﻓﺘ ـﻰ ﻭﺍﻷﻤﺜﻠ ـﺔ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ﻭﺍﻟﺭﺴﻭﻤﺎﺕ ﺍﻟﺘﻭﻀﻴﺤﻴﺔ ﻭﺍﻟﺘﻲ ﺤﺎﻭﻟـﺕ ﺠﺎﻫـﺩﺍ ﺃﻥ ﺃﺠﻌﻠﻬـﺎ‬ ‫ﹰ‬ ‫ﻤﺒﺴﻁﺔ ﺤﺘﻰ ﻴﺘﺴﻨﻰ ﻟﻜل ﺩﺍﺭﺱ ﺃﻭ ﻤﺘﺨﺼﺹ ﻓﻲ ﻫﺫﺍ ﺍﻟﻤﺠﺎل‬ ‫ﺃﻥ ﻴﺘﻨﺎﻭﻟﻬﺎ ﺒﻜل ﺴﻼﺴﺔ ﻭﻴﺴﺭ ﺁﻤﻼ ﻤﻥ ﺍﷲ ﻋﺯ ﻭﺠل ﺃﻥ ﻴﻌﻭﺩ‬ ‫ﹰ‬ ‫ﻫﺫﺍ ﺍﻟﺒﺤﺙ ﺒﺎﻟﻨﻔﻊ ﻋﻠﻰ ﺠﻤﻴﻊ ﺍﻟﻤﻬﺘﻤﻴﻥ ﺒﻬﺫﺍ ﺍﻟﻤﺠﺎل.‬ ‫-٥-‬
  • 7.   ‫א‬ ‫א‬ ‫א‬ ‫א‬ ‫א‬ ‫א‬ -٦-
  • 8. ‫ﺍﻟﻜﺜﺎﻓﺔ )‪:(Density‬‬ ‫ﻭﻫﻰ ﺘﻌﺒﺭ ﻋﻥ ﻜﺘﻠﺔ ﻭﺤﺩﺓ ﺍﻟﺤﺠﻭﻡ ﻤﻥ ﺍﻟﻤﺎﺩﺓ ﻭﻴﺭﻤﺯ ﻟﻬـﺎ‬ ‫ﺒﺎﻟﺭﻤﺯ ‪ ρ‬ﻭﻭﺤﺩﺘﻬﺎ ﻫﻰ ﻜﺘﻠﺔ ﺍﻟﺠﺭﺍﻡ ﻟﻜل ﺴـﻨﺘﻴﻤﺘﺭ ﻤﻜﻌـﺏ‬ ‫)ﺠﻡ/ﺴﻡ٣( ﻭﺘﻌﺘﻤﺩ ﻜﺜﺎﻓﺔ ﺍﻟﺴﺎﺌل ﻋﻠﻰ ﻨﻭﻋﻪ ﻭﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ،‬ ‫ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺀ ﺘﺴﺎﻭﻯ ١ﺠﻡ/ﺴﻡ٣ ﻋﻨﺩ ٦,٥١‪º‬ﻡ.‬ ‫ﺍﻟﻭﺯﻥ ﺍﻟﻨﻭﻋﻰ )‪:(Specific weight‬‬ ‫ﻭﻫﻭ ﻴﻌﺒﺭ ﻋﻥ ﻭﺯﻥ ﻭﺤﺩﺓ ﺍﻟﺤﺠﻭﻡ ﻤﻥ ﺍﻟﻤﺎﺩﺓ ﻭﻴﺭﻤﺯ ﻟـﻪ‬ ‫ﺒﺎﻟﺭﻤﺯ ‪ w‬ﻭﻭﺤﺩﺘﻪ ﻫﻰ ﻗﻭﺓ ﺍﻟﺠﺭﺍﻡ ﻟﻜـل ﺴـﻨﺘﻴﻤﺘﺭ ﻤﻜﻌـﺏ‬ ‫)ﺠﻡ/ﺴﻡ٣( ﻤﻊ ﻤﻼﺤﻅﺔ ﺃﻥ ‪ w = ρg‬ﺤﻴﺙ ﺃﻥ ‪ g‬ﻫﻰ ﻋﺠﻠـﺔ‬ ‫ﺍﻟﺠﺎﺫﺒﻴﺔ ﺍﻷﺭﻀﻴﺔ ﻭﺘﺴﺎﻭﻯ ٧٦٠٨,٩ ﻤﺘﺭ/ﺜﺎﻨﻴﺔ٢.‬ ‫-٧-‬
  • 9. ‫ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ )‪:(Specific Gravity‬‬ ‫ﻭﺘﻌﺭﻑ ﺒﺄﻨﻬﺎ ﺍﻟﻨﺴﺒﺔ ﺒﻴﻥ ﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺩﺓ ﺃﻭ ﻭﺯﻨﻬـﺎ ﺍﻟﻨـﻭﻋﻰ‬ ‫ﻭﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺀ ﺃﻭ ﻭﺯﻨﻪ ﺍﻟﻨﻭﻋﻰ ﻭﻴﺭﻤﺯ ﻟﻬﺎ ﺒﺎﻟﺭﻤﺯ ‪ sp.gr‬ﻭﻫﻰ‬ ‫ﻨﺴﺒﺔ ﺒﺩﻭﻥ ﻭﺤﺩﺍﺕ، ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ ﻟﻠﻤـﺎﺀ‬ ‫ﺘﺴﺎﻭﻯ ١ ﻭﻟﻠﺯﺌﺒﻕ ﺘﺴـﺎﻭﻯ ٦,٣١ ﻭﻓـﻲ ﺍﻟﻨﻅـﺎﻡ ﺍﻟﻤﺘـﺭﻯ‬ ‫ﻟﻠﻭﺤﺩﺍﺕ )ﺴﻨﺘﻴﻤﺘﺭ – ﺠﺭﺍﻡ – ﺜﺎﻨﻴﺔ( ﺘﻜﻭﻥ ﺍﻟﻜﺜﺎﻓـﺔ ﺍﻟﻨﺴـﺒﻴﺔ‬ ‫ﺘﺴﺎﻭﻯ ﺍﻟﻜﺜﺎﻓﺔ ﻋﺩﺩﻴﺎ.‬ ‫ﹰ‬ ‫ﺍﻟﻀﻐﻁ )‪:(Pressure‬‬ ‫ﻴﻌﺭﻑ ﺍﻟﻀﻐﻁ ﺒﺄﻨﻪ ﺍﻟﻘﻭﺓ ﺍﻟﻤﺅﺜﺭﺓ ﻋﻠﻰ ﻭﺤـﺩﺓ ﺍﻟﻤﺴـﺎﺤﺔ‬ ‫ﻭﺘﻜﻭﻥ ﺍﻟﻘﻭﺓ ﻤﺘﻌﺎﻤﺩﺓ ﻋﻠﻰ ﺍﻟﻤﺴﺎﺤﺔ ﻭﻭﺤﺩﺘﻪ ﻫـﻰ ﻜﻴﻠـﻭﺠﺭﺍﻡ‬ ‫ﻟﻜل ﺴﻨﺘﻴﻤﺘﺭ ﻤﺭﺒﻊ )ﻜﺠﻡ/ﺴﻡ٢( ﻭﻓﻲ ﺤﺎﻟﺔ ﻭﺠﻭﺩ ﺴﺎﺌﻠﻴﻥ ﻟﻬـﻡ‬ ‫ﻜﺜﺎﻓﺔ ١، ٥,٠ ﻜﻤﺎ ﺒﺎﻟﺸﻜل )١( ﻓﺈﻥ ﺍﻟﺴﺎﺌل ﺫﻭ ﺍﻟﻜﺜﺎﻓﺔ ﺍﻷﻗـل‬ ‫ﻻﺒﺩ ﺃﻥ ﻴﺼﻌﺩ ﺇﻟﻰ ﺇﺭﺘﻔﺎﻉ ﻋﻤﻭﺩ ﺃﻋﻠﻰ ﻟﻜﻲ ﻴﻭﻟﺩ ﻨﻔﺱ ﺍﻟﻀﻐﻁ‬ ‫ﻋﻨﺩ ﻨﻔﺱ ﺍﻟﻤﺴﺘﻭﻯ ﻤﺜل ﺍﻟﺴﺎﺌل ﺍﻷﺜﻘل ﻭﻴﻜﻭﻥ ﺍﻟﻀـﻐﻁ ﻋﻨـﺩ‬ ‫ﺃﺴﻔل ﺍﻟﻌﻤﻭﺩ ‪ H‬ﻟﻜل ﺴﺎﺌل ﻴﺴﺎﻭﻯ ﻭﺯﻥ ﺍﻟﺴﺎﺌل ﻓـﻭﻕ ﻨﻘﻁـﺔ‬ ‫ﻗﻴﺎﺱ ﺍﻟﻀﻐﻁ ﻤﻘﺴﻭﻤﺎ ﻋﻠﻰ ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁـﻊ ‪ A‬ﻋﻨـﺩ ﻨﻔـﺱ‬ ‫ﹰ‬ ‫ﺃﻯ ﻴﺴﺎﻭﻯ ‪ WH‬ﻭﺒﺫﻟﻙ ﻴﻤﻜﻨﻨﺎ ﺍﻟﺘﻌﺒﻴﺭ ﻋـﻥ‬ ‫ﺍﻟﻨﻘﻁﺔ‬ ‫‪AHW‬‬ ‫‪A‬‬ ‫-٨-‬
  • 10. ‫ﺍﻟﻀﻐﻁ ﺒﺩﻻﻟﺔ ﺇﺭﺘﻔﺎﻉ ﻋﻤﻭﺩ ﺴﺎﺌل ﻤﻌﻴﻥ ﻭﻫـﻭ ﻤـﺎ ﻴﺴـﻤﻰ‬ ‫‪ Head‬ﺃﻭ ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ‪ Pressure Energy‬ﻭﻭﺤﺩﺘﻪ ﻫـﻰ‬ ‫ﻜﺠﻡ.ﻤﺘﺭ/ﻜﺠﻡ ﺃﻯ ﺍﻟﻤﺘﺭ ﻤﻊ ﻤﻼﺤﻅﺔ ﺃﻥ )‪ (Head‬ﺒـﺎﻟﻤﺘﺭ =‬ ‫ﺍﻟﻀﻐﻁ ﺒﺎﻟﻜﺠﻡ/ﺴﻡ٢×٠١/ ‪Sp.gr‬‬ ‫ﺸﻜل )١(‬ ‫-٩-‬
  • 11. ‫ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ ﻴﺴﺎﻭﻯ ٣٠,١ﻜﺠﻡ/ﺴﻡ٢‬ ‫ﻋﻨﺩ ﻤﺴﺘﻭﻯ ﺴﻁﺢ ﺍﻟﺒﺤﺭ ﻭﻫﻭ ﻴﺴﺎﻭﻯ ﺍﻟﻀﻐﻁ ﺍﻟﻨﺎﺘﺞ ﻤﻥ ﻭﺯﻥ‬ ‫01 × 30.1‬ ‫ﺃﻯ ٣,٠١ ﻤﺘﺭ ﻭﻴﺴﺎﻭﻯ ﺃﻴﻀﺎ‬ ‫ﹰ‬ ‫ﻋﻤﻭﺩ ﻤﺎﺀ ﺇﺭﺘﻔﺎﻋﻪ‬ ‫1‬ ‫ـﻪ‬ ‫ـﻕ ﺇﺭﺘﻔﺎﻋـ‬ ‫ـﻭﺩ ﺯﺌﺒـ‬ ‫ـﻐﻁ ﺍ ـﺎﺘﺞ ـﻥ ﻭﺯﻥ ﻋﻤـ‬ ‫ﻤـ‬ ‫ﻟﻨـ‬ ‫ﺍﻟﻀـ‬ ‫01 × 30.1‬ ‫ﺃﻯ ٦٧ﺴﻡ.‬ ‫‪= 0.76 mt‬‬ ‫6.31‬ ‫ﺍﻟﻀﻐﻭﻁ ﺍﻟﻌﻴﺎﺭﻴﺔ ﻭﺍﻟﻤﻁﻠﻘﺔ:‬ ‫ﺸﻜل )٢(‬ ‫- ٠١ -‬
  • 12. ‫ﻜﻤﺎ ﻴﺘﻀﺢ ﻤﻥ ﺸﻜل )٢( ﺃﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻌﻴـﺎﺭﻯ ) ‪Gage‬‬ ‫‪ (pressure‬ﻫﻭ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻨﺴـﻭﺏ ﺇﻟـﻰ ﺍﻟﻀـﻐﻁ ﺍﻟﺠـﻭﻯ‬ ‫)‪ (Atmospheric pressure‬ﺒﺈﻋﺘﺒﺎﺭ ﺃﻥ ﺍﻟﻀـﻐﻁ ﺍﻟﺠـﻭﻯ‬ ‫ﻴﺴﺎﻭﻯ ﺼﻔﺭ ﻓﻬﻭ ﺇﻤﺎ ﺃﻋﻠﻰ ﻤﻥ ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ ﻓﻴﺴﻤﻰ ﻀﻐﻁ‬ ‫)‪ (pressure‬ﺃﻭ ﺃﻗل ﻤﻥ ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ ﻓﻴﺴـﻤﻰ ﺘﻔﺭﻴـﻎ ﺃﻭ‬ ‫ﺨﻠﺨﻠﺔ )‪ (vacuum‬ﻭﻴﻘﺎﺱ ﻫﺫﺍ ﺍﻟﻀﻐﻁ ﺒﻭﺍﺴﻁﺔ ﺃﺠﻬﺯﺓ ﻤﺜـل‬ ‫ﺍﻟﻤ ـﺎﻨﻭﻤﺘﺭﺍﺕ ﻭﺃﻨﺒﻭﺒ ـﺔ ﺒ ـﻭﺭﺩﻭﻥ ﺃﻤ ـﺎ ﺍﻟﻀ ـﻐﻁ ﺍﻟﻤﻁﻠ ـﻕ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ ـ‬ ‫ـ‬ ‫)‪ (Absolute pressure‬ﻓﻬﻭ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻨﺴﻭﺏ ﺇﻟﻰ ﺍﻟﺼـﻔﺭ‬ ‫ﺍﻟﻤﻁﻠﻕ ﺤﻴﺙ ﺃﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻁﻠـﻕ = ﺍﻟﻀـﻐﻁ ﺍﻟﻌﻴـﺎﺭﻯ +‬ ‫ﺍﻟﻀﻐﻁ ﺍﻟﺠﻭﻯ.‬ ‫ﻀﻐﻁ ﺍﻟﺒﺨﺎﺭ )‪:(Vapor pressure‬‬ ‫ﻭﻴﻌﺭﻑ ﺒﺄﻨﻪ ﺍﻟﻀﻐﻁ ﺍﻟﺫﻯ ﻋﻨﺩﻩ ﻴﺘﺤﻭل ﺍﻟﺴﺎﺌل ﺇﻟﻰ ﺒﺨـﺎﺭ‬ ‫ﻭﻴﻌﺘﻤﺩ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﻭﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ ﻭﻴﺘﻡ ﺍﻟﺘﻌﺒﻴﺭ ﻋﻨـﻪ‬ ‫ﺒﺎﻟﻘﻴﻡ ﺍﻟﻤﻁﻠﻘﺔ ﻟﻠﻀﻐﻭﻁ، ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻀﻐﻁ ﺍﻟﺒﺨﺎﺭ ﻟﻠﻤﺎﺀ‬ ‫ـﺔ )٦,٣٢‪º‬ﻡ( ـﺎﻭﻯ‬ ‫ﻴﺴـ‬ ‫ـﺭﺍﺭﺓ ﺍﻟﻌﺎﺩﻴـ‬ ‫ـﺎﺕ ﺍﻟﺤـ‬ ‫ـﺩ ﺩﺭﺠـ‬ ‫ﻋﻨـ‬ ‫٣٠,٠ﻜﺠﻡ/ﺴﻡ٢ ﻤﻁﻠﻕ ﻤﻌﻨﻰ ﺫﻟﻙ ﺃﻨﻪ ﻟﻭ ﺘﻡ ﺨﻠﺨﻠﺔ ﺍﻟﻔﺭﺍﻍ ﻓﻭﻕ‬ ‫ﺴﻁﺢ ﺍﻟﻤﺎﺀ ﺤﺘﻰ ﻴﺼل ﺍﻟﻀﻐﻁ ﺇﻟﻰ ﻫﺫﻩ ﺍﻟﻘﻴﻤﺔ ﻓـﺈﻥ ﺍﻟﻤـﺎﺀ‬ ‫ﻴﺘﺒﺨﺭ ﻋﻨﺩ ﺩﺭﺠﺎﺕ ﺍﻟﺤﺭﺍﺭﺓ ﺍﻟﻌﺎﺩﻴﺔ.‬ ‫- ١١ -‬
  • 13. ‫ﺸﻜل )٣(‬ ‫ﺃﻗﺼﻰ ﻀﻐﻁ ﺴﺎﻟﺏ:‬ ‫ﻜﻤﺎ ﻴﺘﻀﺢ ﻤﻥ ﺸﻜل )٣( ﺃﻨﻪ ﺇﺫﺍ ﺘﻡ ﻋﻤـل ﺨﻠﺨﻠـﺔ ﻓـﻲ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﺍﻟﺭﺃﺴﻴﺔ ﻓﺈﻥ ﺍﻟﻤﺎﺀ ﻴﺼﻌﺩ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﺒﺘﺄﺜﻴﺭ ﺍﻟﻀـﻐﻁ‬ ‫ﺍﻟﺠﻭﻯ ﺤﺘﻰ ﻴﺼل ﺇﻟﻰ ﺤﺩ ﻤﻌﻴﻥ ﻴﻜﻭﻥ ﺍﻟﻀﻐﻁ ﻋﻨﺩﻩ ﻴﺴـﺎﻭﻯ‬ ‫ﻀﻐﻁ ﺍﻟﺒﺨﺎﺭ ﻭﻴﻁﻠﻕ ﻋﻠﻰ ﺍﻹﺭﺘﻔﺎﻉ ﻤﻥ ﺴﻁﺢ ﺍﻟﺴﺎﺌل ﺒﺎﻹﻨـﺎﺀ‬ ‫ﺤﺘﻰ ﻫﺫﺍ ﺍﻟﺤﺩ ﺒﺄﻗﺼﻰ ﻀﻐﻁ ﺴﺎﻟﺏ )ﻓﻲ ﺼﻭﺭﺓ ‪ (Head‬ﻭﻫﻭ‬ ‫]30.0 − 30.1[ × 01‬ ‫ﻟﻠﻤـﺎﺀ ﻋﻨـﺩ ﺩﺭﺠـﺎﺕ‬ ‫ﻴﺴﺎﻭﻯ ‪= 10 mt‬‬ ‫1‬ ‫ﺍﻟﺤﺭﺍﺭﺓ ﺍﻟﻌﺎﺩﻴﺔ.‬ ‫- ٢١ -‬
  • 14. ‫ﺍﻟﻠﺯﻭﺠﺔ )‪:(Viscosity‬‬ ‫ﻴﻁﻠﻕ ﺇﺴﻡ ﺍﻟﻤﻭﺍﺌﻊ ﻋﻠﻰ ﺍﻟﺴﻭﺍﺌل ﻭﺍﻟﻐﺎﺯﺍﺕ ﻭﺘﺴﻤﻰ ﺨﺎﺼﻴﺔ‬ ‫ﺍﻟﺴﺎﺌل ﺍﻟﺘﻲ ﺘﻭﻟﺩ ﻤﻘﺎﻭﻤﺔ ﻟﻘﻭﻯ ﺍﻟﻘﺹ ﻓﻲ ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻠﺯﻭﺠـﺔ‬ ‫ﻭﺇﺫﺍ ﺘﻡ ﻤلﺀ ﺍﻟﻔﺭﺍﻍ ﺒﻴﻥ ﺴﻁﺤﻴﻥ ﻤﺴﺘﻭﻴﻴﻥ ﺒﺴﺎﺌل ﻓﻴﻠﺯﻡ ﻗـﻭﺓ‬ ‫ﻟﻜﻲ ﻴﺘﺤﺭﻙ ﺇﺤﺩﻯ ﺍﻟﺴﻁﺤﻴﻥ ﺒﺴﺭﻋﺔ ﺜﺎﺒﺘﺔ ﺒﺎﻟﻨﺴـﺒﺔ ﻟﻶﺨـﺭ‬ ‫ﻭﺘﺘﻐﻴﺭ ﺴﺭﻋﺔ ﺍﻟﺴﺎﺌل ﺨﻁﻴﺎ ﺒﻴﻥ ﺍﻟﺴﻁﺤﻴﻥ ﻭﺍﻟﻨﺴﺒﺔ ﺒﻴﻥ ﺍﻟﻘـﻭﺓ‬ ‫ﹰ‬ ‫ﻟﻜل ﻭﺤﺩﺓ ﻤﺴﺎﺤﺔ )ﺇﺠﻬﺎﺩ ﺍﻟﻘﺹ( ﺇﻟﻰ ﺍﻟﺴﺭﻋﺔ ﻟﻜـل ﻭﺤـﺩﺓ‬ ‫ﻤﺴﺎﻓﺔ ﺒﻴﻥ ﺍﻟﺴﻁﺤﻴﻥ )ﻤﻌﺩل ﺍﻟﻘﺹ( ﺘﻜﻭﻥ ﻤﻘﻴـﺎﺱ ﻟﺯﻭﺠـﺔ‬ ‫ﺍﻟﺴﺎﺌل ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﺃﻭ ﺍﻟﻤﻁﻠﻘﺔ ﻭﺍﻟﺴﻭﺍﺌل ﺍﻟﺘﻲ ﺘﺘﻨﺎﺴـﺏ ﻓﻴﻬـﺎ‬ ‫ﺇﺠﻬﺎﺩﺍﺕ ﺍﻟﻘﺹ ﻤﻊ ﻤﻌﺩﻻﺕ ﺍﻟﻘﺹ ﺘﻜﻭﻥ ﻟﻬﺎ ﻤﻌﺎﻤﻼﺕ ﻟﺯﻭﺠﺔ‬ ‫ﺜﺎﺒﺘﺔ ﻋﻨﺩ ﻀﻐﻁ ﻭﺩﺭﺠﺔ ﺤﺭﺍﺭﺓ ﻤﺤﺩﺩﻴﻥ ﻭﻴﻁﻠﻕ ﻋﻠﻴﻬﺎ ﺇﺴـﻡ‬ ‫ﺍﻟﺴـﻭﺍﺌل ﺍﻟﺤﻘﻴﻘﻴـﺔ ‪ Newtonian Liquids‬ﻭﻓﻴﻬـﺎ ﺘﺯﻴـﺩ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﻭﻤﻘﺎﻭﻤﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻤﻊ ﻨﻘﺹ ﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ.‬ ‫ﻭﺘﻜﻭﻥ ﻭﺤـﺩﺓ ﺍﻟﻠﺯﻭﺠـﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴـﺔ ﺃﻭ ﺍﻟﻤﻁﻠﻘـﺔ ﻫـﻰ‬ ‫ﺩﺍﻴﻥ.ﺜﺎﻨﻴﺔ/ﺴﻡ٢ ﻭﺘﺴـﻤﻰ ﺒـﻭﻴﺯ )‪ (poise‬ﻭﺘﺴـﺎﻭﻯ ﻋـﺩﺩﻴﺎ‬ ‫ﹰ‬ ‫ﺠﻡ/ﺴﻡ.ﺜﺎﻨﻴﺔ ﻭﺍﻟﻘﻴﺎﺱ ﺍﻟﺸﺎﺌﻊ ﻟﻠﺯﻭﺠﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﺃﻭ ﺍﻟﻤﻁﻠﻘـﺔ‬ ‫× ‪Centipoise‬‬ ‫ﻴﻜﻭﻥ ﺴﻨﺘﻰ ﺒﻭﻴﺯ )١/٠٠١ﺒﻭﻴﺯ( ﺤﻴﺙ ﺃﻥ‬ ‫‪.١٠-٣ = N.sec/m٢ = Pa.sec‬‬ ‫- ٣١ -‬
  • 15. ‫‪N – Newton‬‬ ‫٢‪Pa – Pascal = N/m‬‬ ‫ﻭﺃﺤﻴﺎﻨﺎ ﻴﻌﺒﺭ ﻋﻥ ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺒﺎﻟﻠﺯﻭﺠـﺔ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴـﺔ‬ ‫ﹰ‬ ‫ﻭﻫﻰ ﺘﺴﺎﻭﻯ ﺍﻟﻠﺯﻭﺠﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﻤﻘﺴﻭﻤﺔ ﻋﻠﻰ ﺍﻟﻜﺜﺎﻓﺔ )‪(w/g‬‬ ‫ﻭﻭﺤ ـﺩﺘﻬﺎ ﺍﻟﻤﺘﺭﻴ ـﺔ ﻫ ـﻰ ﺴ ـﻡ٢/ﺜﺎﻨﻴ ـﺔ ﻭﺘﺴ ـﻤﻰ ﺴ ـﺘﻭﻙ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ ـ ـ‬ ‫ـ‬ ‫)‪ (stoke‬ﻭﺍﻟﻘﻴﺎﺱ ﺍﻟﺸﺎﺌﻊ ﻟﻠﺯﻭﺠﺔ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴﺔ ﻴﻜـﻭﻥ ﺴـﻨﺘﻰ‬ ‫ﺴﺘﻭﻙ )١/٠٠١ ﺴﺘﻭﻙ( ﺤﻴﺙ ﺃﻥ‬ ‫‪Centistoke = mm٢/sec‬‬ ‫‪Centistoke × ١٠-٦ = m٢/sec‬‬ ‫ﻭﺘﻌﺘﻤﺩ ﺍﻟﻠﺯﻭﺠﺔ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﻭﺩﺭﺠﺔ ﺍﻟﺤﺭﺍﺭﺓ، ﻋﻠـﻰ‬ ‫ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻟﺯﻭﺠﺔ ﺍﻟﻤـﺎﺀ ﺘﺴـﺎﻭﻯ ٣١١٠,٠ ﺒـﻭﻴﺯ ﻋﻨـﺩ‬ ‫٦,٥١‪º‬ﻡ ﻭﻓﻲ ﺍﻟﻨﻅﺎﻡ ﺍﻟﻤﺘﺭﻯ ﻟﻠﻭﺤﺩﺍﺕ )ﺴﻡ.ﺠﻡ.ﺜﺎﻨﻴﺔ( ﺘﻜـﻭﻥ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴﺔ ﺒﺎﻟﺴﻨﺘﻰ ﺴﺘﻭﻙ = ﺍﻟﻠﺯﻭﺠﺔ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ ﺃﻭ‬ ‫ﺍﻟﻤﻁﻠﻘﺔ ﺒﺎﻟﺴﻨﺘﻰ ﺒﻭﻴﺯ/‪ Sp.gr‬ﻭﺍﻟﺘﺤﻭﻴل ﻤﻥ ﺍﻟﻭﺤﺩﺍﺕ ﺍﻟﻤﺘﺭﻴﺔ‬ ‫ﺇﻟﻰ ﺍﻟﻭﺤﺩﺍﺕ ﺍﻹﻨﺠﻠﻴﺯﻴﺔ )ﻗـﺩﻡ – ﺭﻁـل – ﺜﺎﻨﻴـﺔ( ﻴﻜـﻭﻥ‬ ‫ﺭﻁل.ﺜﺎﻨﻴﺔ/ﻗﺩﻡ٢ = ٥٥٨٨٠٢٠٠٠٠,٠ ﺴﻨﺘﻰ ﺒﻭﻴﺯ.‬ ‫ﻗﺩﻡ٢/ﺜﺎﻨﻴﺔ = ٩٣٦٧٠١,٠ ﺴﻨﺘﻰ ﺴﺘﻭﻙ.‬ ‫- ٤١ -‬
  • 16. ‫ﻭﺍﻟﻤﺎﺌﻊ ﺍﻟﻤﺜﺎﻟﻰ ﻫﻭ ﺍﻟﻤﺎﺌﻊ ﺍﻟﺫﻯ ﻨﻌﺘﺒﺭﻩ ﺨﺎل ﻤﻥ ﺍﻟﻠﺯﻭﺠـﺔ‬ ‫ﻭﺘﺴﻬﻴﻼ ﻟﺩﺭﺍﺴﺔ ﺍﻟﻤﻌﺎﺩﻻﺕ ﻨﻌﺘﺒﺭ ﺍﻟﻤﺎﺌﻊ ﻤﺜﺎﻟﻴﺎ ﺒﺈﻫﻤﺎل ﺘـﺄﺜﻴﺭ‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﺜﻡ ﺇﺩﺨﺎل ﻤﻌﺎﻤﻼﺕ ﺍﻟﺘﺼﺤﻴﺢ ﺍﻟﺘﻲ ﻴـﺘﻡ ﺍﻟﺤﺼـﻭل‬ ‫ﻋﻠﻴﻬﺎ ﻤﻥ ﺍﻟﺘﺠﺎﺭﺏ ﺍﻟﻤﻌﻤﻠﻴﺔ.‬ ‫ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ )‪:(Continuity Equation‬‬ ‫ﺸﻜل )٤(‬ ‫- ٥١ -‬
  • 17. ‫ﺘﺭﺒﻁ ﻫﺫﻩ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺒﻴﻥ ﺍﻟﺴﺭﻋﺔ ﺍﻟﻤﺘﻭﺴـﻁﺔ ‪ V‬ﺍﻟﻌﻤﻭﺩﻴـﺔ‬ ‫ﻋﺒﺭ ﻤﻘﻁﻊ ﻓﻲ ﺃﻨﺒﻭﺒﺔ ﻭﺒﻴﻥ ﺍﻟﻤﺴﺎﺤﺔ ‪ A‬ﻟﻬﺫﺍ ﺍﻟﻤﻘﻁـﻊ ﻭﻜﻤـﺎ‬ ‫ﻴﺘﻀﺢ ﻤﻥ ﺸﻜل )٤( ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )١( ﺇﺫﺍ ﻜﺎﻨﺕ ﺍﻟﻤﺴﺎﺤﺔ ١‪A‬‬ ‫ﻭﺍﻟﺴﺭﻋﺔ ١‪ V‬ﻭﻜﺜﺎﻓﺔ ﺍﻟﻤﺎﺌﻊ ١‪ ρ‬ﺘﻜﻭﻥ ﻜﺘﻠﺔ ﺍﻟﻤﺎﺌﻊ ﺍﻟﻤﺎﺭ ﻓـﻲ‬ ‫ﺍﻟﺜﺎﻨﻴﺔ ﺍﻟﻭﺍﺤﺩﺓ ﺨﻼل ﻫﺫﺍ ﺍﻟﻤﻘﻁﻊ ﻫﻰ ١‪ ρ١A١V‬ﻓﻠـﻭ ﺘﻐﻴـﺭ‬ ‫ﺍﻟﻤﻘﻁﻊ ﺇﻟﻰ )٢( ﻭﻜﺎﻨﺕ ﻤﺴﺎﺤﺘﻪ ٢‪ A‬ﻓﻼﺒﺩ ﺃﻥ ﻴﺤﺩﺙ ﺘﻐﻴﺭ ﻓﻲ‬ ‫ﻗﻴﻡ ٢‪ ρ٢,V‬ﻟﺘﻅل ﺍﻟﻜﺘﻠﺔ ﺜﺎﺒﺘﺔ ﻭﻓﻲ ﺤﺎﻟﺔ ﺍﻟﻤﻭﺍﺌﻊ ﺍﻟﻐﻴﺭ ﻗﺎﺒﻠـﺔ‬ ‫ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل ﻟﻡ ﺘﺘﻐﻴﺭ ﺍﻟﻜﺜﺎﻓﺔ ﺃﻯ ﺘﻅل ﺜﺎﺒﺘﺔ ﺃﻯ ﺃﻥ‬ ‫ﻤﻘﺩﺍﺭ ﺜﺎﺒﺕ = ٢‪A١V١=A٢V‬‬ ‫ﻭﻴﻁﻠﻕ ﻋﻠﻰ ﻫﺫﺍ ﺍﻟﻤﻘﺩﺍﺭ ﺍﻟﺜﺎﺒﺕ ﺇﺴﻡ ﻤﻌـﺩل ﺍﻟﺴـﺭﻴﺎﻥ ﺃﻭ‬ ‫ﺍﻟﻜﻤﻴﺔ )‪ (Flow Rate‬ﻭﻴﺭﻤﺯ ﻟﻪ ﺒﺎﻟﺭﻤﺯ ‪ Q‬ﻭﻴﻌـﺭﻑ ﺒﺄﻨـﻪ‬ ‫ﺤﺠﻡ ﺍﻟﺴﺎﺌل ﺍﻟﻤﺎﺭ ﻓﻲ ﻭﺤﺩﺓ ﺍﻟﺯﻤﻥ ﻭﻭﺤﺩﺘﻪ ﻫﻰ ﻤﺘﺭ٣/ﺴﺎﻋﺔ.‬ ‫ﺍﻟﻁﺎﻗﺔ )‪:(Energy‬‬ ‫ﺘﻜﻭﻥ ﻁﺎﻗﺔ ﺍﻟﻤﻭﺍﺌﻊ ﺍﻟﻐﻴﺭ ﻗﺎﺒﻠﺔ ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل ﻓﻲ‬ ‫ﺜﻼﺙ ﺼﻭﺭ ﻫﻰ ﺴﺭﻋﺔ، ﻀﻐﻁ ﻭﺇﺭﺘﻔﺎﻉ ﻭﻴﺘﻡ ﺍﻟﺘﻌﺒﻴﺭ ﻋﻨﻬﺎ ﻓﻲ‬ ‫ﺼﻭﺭﺓ ﻁﺎﻗﺔ ﻟﻭﺤﺩﺓ ﺍﻷﻭﺯﺍﻥ ﻭﻭﺤﺩﺘﻬﺎ ﻫﻰ ﻜﺠﻡ.ﻤﺘﺭ/ﻜﺠـﻡ ﺃﻭ‬ ‫ﺍﻟﻤﺘﺭ ﻋﻴﺎﺭﻯ ﺃﻭ ﻤﻁﻠﻕ.‬ ‫- ٦١ -‬
  • 18. ‫ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ )‪:(Velocity Head‬‬ ‫2‪V‬‬ ‫( ﻭﻭﺤـﺩﺘﻬﺎ ﻫـﻰ‬ ‫ﻭﻴﻌﺒﺭ ﻋﻨﻬﺎ ﻓﻲ ﺼﻭﺭﺓ ﺴـﺭﻋﺔ )‬ ‫‪2g‬‬ ‫ﻜﺠﻡ.ﻤﺘﺭ/ﻜﺠﻡ ﺃﻯ ﺍﻟﻤﺘﺭ ﻭﺴـﺭﻋﺔ ﺍﻟﺴـﻭﺍﺌل ﻓـﻲ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫ﻭﺍﻟﻘﻨﻭﺍﺕ ﺍﻟﻤﻔﺘﻭﺤﺔ ﺘﺘﻐﻴﺭ ﻋﺒﺭ ﺃﻯ ﻤﻘﻁﻊ ﻭﺍﺤﺩ ﻤﻥ ﺍﻟﻤﺠـﺭﻯ‬ ‫ﻭﻟﺫﻟﻙ ﻓﺈﻨﻪ ﻤﻥ ﺍﻟﺩﻗﺔ ﺍﻟﻜﺎﻓﻴﺔ ﺃﻥ ﻨﺴﺘﺨﺩﻡ ﺍﻟﺴﺭﻋﺔ ﺍﻟﻤﺘﻭﺴﻁﺔ ‪V‬‬ ‫ﺍﻟﻤﺤﺴﻭﺒﺔ ﺒﻘﺴﻤﺔ ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ ﻋﻠﻰ ﻤﺴﺎﺤﺔ ﻤﻘﻁﻊ ﺍﻟﻤﺠﺭﻯ.‬ ‫ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ )‪:(Pressure Head‬‬ ‫‪10 4 P‬‬ ‫ﻭﻭﺤﺩﺘﻬﺎ‬ ‫ﻭﻴﻌﺒﺭ ﻋﻨﻬﺎ ﻓﻲ ﺼﻭﺭﺓ ‪ Head‬ﻭﺘﺴﺎﻭﻯ‬ ‫‪w‬‬ ‫ﺍﻟﻤﺘﺭ ﺤﻴﺙ ﺃﻥ ‪ P‬ﺍﻟﻀﻐﻁ ﺒﺎﻟﻜﺠﻡ/ﺴﻡ٢، ‪ w‬ﺍﻟـﻭﺯﻥ ﺍﻟﻨـﻭﻋﻰ‬ ‫ﻟﻠﺴﺎﺌل ﺒﺎﻟﻜﺠﻡ/ﻤﺘﺭ٣.‬ ‫ﻁﺎﻗﺔ ﺍﻟﻭﻀﻊ )‪:(Elevation Head‬‬ ‫ﻭﻴﻌﺒﺭ ﻋﻨﻬﺎ ﺒﺎﻹﺭﺘﻔﺎﻉ ‪ Z‬ﻋـﻥ ﻤﺴـﺘﻭﻯ ﻗﻴﺎﺴـﻲ ﻤﻌـﻴﻥ‬ ‫‪ Datum Plane‬ﻭﻋﺎﺩﺓ ﻴﻜﻭﻥ ﻤﺴﺘﻭﻯ ﺴﻁﺢ ﺍﻟﺒﺤﺭ ﻭﻭﺤﺩﺘﻬﺎ‬ ‫ﺍﻟﻤﺘﺭ.‬ ‫- ٧١ -‬
  • 19. ‫ﻨﻅﺭﻴﺔ ﺒﺭﻨﻭﻟﻠﻰ )‪:(Bernoulli's Equation‬‬ ‫ﻨﻅﺭﻴﺔ ﺒﺭﻨﻭﻟﻠﻰ ﻟﻠﻤﻭﺍﺌﻊ ﺍﻟﻐﻴﺭ ﻗﺎﺒﻠﺔ ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل‬ ‫ﺘﻨﺹ ﻋﻠﻰ ﺃﻨﻪ ﻓﻲ ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻤﺴﺘﻘﺭ ‪ Steady Flow‬ﺒـﺩﻭﻥ‬ ‫ﻓﻭﺍﻗﺩ )ﻤﺎﺌﻊ ﻤﺜﺎﻟﻰ( "ﺍﻟﻁﺎﻗﺔ ﻋﻨﺩ ﺃﻯ ﻨﻘﻁﺔ ﺘﺴـﺎﻭﻯ ﻤﺠﻤـﻭﻉ‬ ‫ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ ﻭﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ﻭﻁﺎﻗﺔ ﺍﻟﻭﻀـﻊ ﻭﻴﻜـﻭﻥ ﻫـﺫﺍ‬ ‫ﺍﻟﻤﺠﻤﻭﻉ ﺜﺎﺒﺕ ﻋﻠﻰ ﻁﻭل ﺨﻁ ﺍﻟﺴﺭﻴﺎﻥ ﻓﻲ ﺍﻟﻤﺠﺭﻯ" ﻭﻫـﺫﻩ‬ ‫ﺍﻟﻁﺎﻗﺔ ﺘﺴﺎﻭﻯ‬ ‫4‬ ‫2‬ ‫‪10 P V‬‬ ‫=‪H‬‬ ‫+‬ ‫‪+z‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﻭﻋﻨﺩ ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻤﺴﺘﻘﺭ ﻟﻠﻤﺎﺌﻊ ﺍﻟﻤﺜﺎﻟﻰ ﻴﻤﻜـﻥ ﻟﻠﻁﺎﻗـﺔ ﺃﻥ‬ ‫ﺘﺘﻐﻴﺭ ﻤﻥ ﺼﻭﺭﺓ ﻷﺨﺭﻯ ﻓﺈﺫﺍ ﺯﺍﺩﺕ ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ ﺇﻨﺨﻔﻀـﺕ‬ ‫ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ﺃﻭ ﻁﺎﻗﺔ ﺍﻟﻭﻀﻊ ﻭﺴﻭﻑ ﻨﻭﻀﺢ ﺘﻁﺒﻴﻘﺎﺕ ﻨﻅﺭﻴﺔ‬ ‫ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺒﻌﺽ ﺤﺎﻻﺕ ﺍﻟﺴﺭﻴﺎﻥ ﻓﻲ ﺃﺠﻬﺯﺓ ﻗﻴﺎﺱ ﻤﻌـﺩل‬ ‫ﺍﻟﺴﺭﻴﺎﻥ )ﺍﻟﻜﻤﻴﺔ(.‬ ‫- ٨١ -‬
  • 20. ‫١- ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ )‪:(Orifice Meter‬‬ ‫ﺸﻜل )٥(‬ ‫- ٩١ -‬
  • 21. ‫ﻴﺘﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻤﻘﻴﺎﺱ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ D‬ﻴﻜـﻭﻥ‬ ‫ﺃﻜﺒﺭ ﻤﻥ ٥ﺴﻡ ﻭﻤﺭﻜﺏ ﺒﻬﺎ ﻗﺭﺹ ﺒﻪ ﻓﺘﺤﺔ ﻗﻁﺭﻫﺎ ‪ d‬ﺃﺼـﻐﺭ‬ ‫ﻤﻥ ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒﺔ ﻭﻻ ﻴﻘل ﻋﻥ ٦ﻤﻡ ﻜﻤﺎ ﺒﺎﻟﺸﻜل )٥( ﺒﺤﻴـﺙ‬ ‫ﻓﻲ ﺤـﺩﻭﺩ ٢,٠ – ٨,٠ ﻭﻻ ﺘﺯﻴـﺩ‬ ‫ﺘﻜﻭﻥ ﻨﺴﺒﺔ ﺍﻷﻗﻁﺎﺭ‬ ‫‪d‬‬ ‫‪D‬‬ ‫2‬ ‫ﻨﺴﺒﺔ ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁﻊ ⎞ ⎛ ﻋـﻥ ٧,٠، ﺒﺘﻁﺒﻴـﻕ ﻤﻌﺎﺩﻟـﺔ‬ ‫‪d‬‬ ‫⎟ ⎜‬ ‫⎠‪⎝D‬‬ ‫ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺍﻟﻨﻘﻁﺘﻴﻥ )١(، )٢( ﻭﺇﻋﺘﺒﺎﺭ ﺍﻟﻤﺎﺌﻊ ﻤﺜﺎﻟﻴﺎ‬ ‫ﹰ‬ ‫ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ)١(= ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ)٢(= ﺜﺎﺒﺕ‬ ‫2‪10 4 P‬‬ ‫22‪V‬‬ ‫21‪10 4 P1 V‬‬ ‫+‬ ‫= 2‪+ Z‬‬ ‫+‬ ‫1‪+ Z‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﻤﻊ ﺃﺨﺫ ﺍﻟﻤﺴﺘﻭﻯ ﺍﻟﻘﻴﺎﺴﻰ ﻫﻭ ﻤﺤـﻭﺭ ﺍﻷﻨﺒﻭﺒـﺔ ﻭﺇﻫﻤـﺎل‬ ‫ﺍﻟﺴﺭﻋﺔ ١‪ V‬ﺒﺈﻋﺘﺒﺎﺭﻫﺎ ﺃﻗل ﺒﻜﺜﻴﺭ ﻤﻥ ٢‪V‬‬ ‫) 2 ‪V22 10 4 ( p1 − p‬‬ ‫=‬ ‫‪= H1 − H 2 = h‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪V 2 = 2 gh‬‬ ‫ﻭﺇﺫﺍ ﺘﻜﻠﻤﻨﺎ ﻋﻥ ﺘﺄﺜﻴﺭ ﺍﻟﻠﺯﻭﺠﺔ ﻴﺘﺒﻴﻥ ﺃﻨﻪ ﻋﻨﺩ ﺴﺭﻴﺎﻥ ﺍﻟﻤﺎﺌﻊ‬ ‫ﻴﻀﻴﻊ ﺠﺯﺀ ﻤﻥ ﺍﻟﻁﺎﻗﺔ ﻋﻥ ﻁﺭﻴﻕ ﺍﻹﺤﺘﻜـﺎﻙ ﺍﻟﻨﺎﺸـﺊ ﻤـﻥ‬ ‫ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺃﻯ ﺃﻨﻪ ﺇﺫﺍ ﺘﻡ ﻗﻴﺎﺱ ﺍﻟﺴﺭﻋﺔ ٢‪ V‬ﻟﻭﺠﺩﻨﺎ ﺃﻨﻬـﺎ‬ ‫ﻷﻥ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ )٢( ﺘﻜﻭﻥ ﺃﻗـل‬ ‫ﺃﻗل ﻤﻥ ‪2 gh‬‬ ‫- ٠٢ -‬
  • 22. ‫ﻤﻥ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ )١( ﻨﺘﻴﺠﺔ ﻓﻘﺩ ﺠﺯﺀ ﻤﻨﻬﺎ ﺒﺈﺤﺘﻜﺎﻙ‬ ‫ﺍﻟﻤﺎﺌﻊ ﻤﻊ ﺠﺩﺭﺍﻥ ﺍﻟﻤﻘﻴﺎﺱ ﻋﻨﺩ ﺨﺭﻭﺠﻪ ﻤﻥ ﺍﻟﻔﺘﺤـﺔ، ﺤﻴـﺙ‬ ‫ﻴﻨﺘﻘل ﺍﻟﺴﺎﺌل ﻤﻥ ﻨﻘﻁﺔ ﺇﻟﻰ ﺃﺨﺭﻯ ﻨﺘﻴﺠﺔ ﻓﺭﻕ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴـﺔ‬ ‫ﺒﻴﻥ ﺍﻟﻨﻘﻁﺘﻴﻥ‬ ‫ﻭﺒﺫﻟﻙ ﺘﻜﻭﻥ ﺍﻟﺴﺭﻋﺔ ٢‪ V‬ﺘﺴﺎﻭﻯ ‪ K V 2 gh‬ﺤﻴـﺙ ‪Kv‬‬ ‫ﻴﺴﻤﻰ ﻤﻌﺎﻤل ﺍﻟﺴﺭﻋﺔ ﻭﻫﻭ ﺃﻗل ﻤﻥ ١ ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻤﻌـﺩل‬ ‫ﺍﻟﺴﺭﻴﺎﻥ )ﺍﻟﻜﻤﻴﺔ( ‪ Q‬ﺍﻟﻤﺎﺭ ﺨﻼل ﺍﻟﻔﺘﺤﺔ ﻤﻥ ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ‬ ‫٢‪ Q = A٢V‬ﺤﻴﺙ ﺃﻥ ﺍﻟﺴﺭﻋﺔ ﺘﻜﻭﻥ ﻋﻤﻭﺩﻴﺔ ﻋﻠﻰ ﺍﻟﻤﺴـﺎﺤﺔ‬ ‫ﻋﻨﺩ ﺍﻹﻨﻜﻤﺎﺵ ﺃﻯ ﻋﻨﺩ ﺍﻟﻨﻘﻁـﺔ )٢( ﻭﻟـﻴﺱ ﻋﻨـﺩ ﺍﻟﻔﺘﺤـﺔ‬ ‫‪ Orifice‬ﺫﺍﺘﻬﺎ ﻭﺒﺫﻟﻙ ﺘﻜﻭﻥ ﻤﺴﺎﺤﺔ ﻤﻘﻁﻊ ﺍﻹﻨﻜﻤﺎﺵ ٢‪ A‬ﺃﻗل‬ ‫‪π‬‬ ‫ﻤﻥ ﻤﺴﺎﺤﺔ ﻤﻘﻁﻊ ﺍﻟﻔﺘﺤﺔ ﻨﻔﺴﻬﺎ 2 ‪d‬‬ ‫4‬ ‫‪π‬‬ ‫‪A2 = K C‬‬ ‫2‪d‬‬ ‫4‬ ‫ﺤﻴﺙ ﺃﻥ ‪ Kc‬ﻴﺴﻤﻰ ﻤﻌﺎﻤل ﺇﻨﻜﻤﺎﺵ ﻤﻘﻁﻊ ﺍﻟﺴﺭﻴﺎﻥ ﻭﻫـﻭ‬ ‫ﺃﻗل ﻤﻥ ١ ﻭﺒﺫﻟﻙ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ ﺨﻼل ﺍﻟﻔﺘﺤﺔ ﺘﺴﺎﻭﻯ‬ ‫‪π‬‬ ‫‪π‬‬ ‫‪Q = KC‬‬ ‫‪d 2 K V 2 gh = K d‬‬ ‫‪d 2 2 gh‬‬ ‫4‬ ‫4‬ ‫)١(‬ ‫- ١٢ -‬
  • 23. ‫ﺤﻴﺙ ﺃﻥ ‪ Kd‬ﻫﻭ ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ﻭﻴﺴﺎﻭﻯ ‪ KvKc‬ﻭﻴﻜﻭﻥ‬ ‫ﺃﻗل ﻤﻥ ١ ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻗﻴﻤﺔ ﻫﺫﺍ ﺍﻟﻤﻌﺎﻤل ﻤـﻥ ﺍﻟﺘﺠـﺎﺭﺏ‬ ‫ﺍﻟﻤﻌﻤﻠﻴﺔ ﻭﻟﺘﺴﻬﻴل ﺍﻟﺤﺴﺎﺒﺎﺕ ﻴﻤﻜﻥ ﺇﻋﺘﺒﺎﺭ ﺍﻟﻘﻴﻤﺔ ﺍﻟﺘﻘﺭﻴﺒﻴﺔ ﻟﻬﺫﺍ‬ ‫ﺍﻟﻤﻌﺎﻤل ﺘﺴﺎﻭﻯ ٦٩٥,٠، ﻭﺒﻬﺫﻩ ﺍﻟﻁﺭﻴﻘﺔ ﻴﺘﻡ ﻗﻴـﺎﺱ ﺍﻟﻜﻤﻴـﺔ‬ ‫ﺒﻤﻌﺭﻓﺔ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺒﻴﻥ ﻗﺒل ﻭﺒﻌﺩ ﺍﻟﻔﺘﺤﺔ ﻭﻴﺘـﺭﺍﻭﺡ ﻀـﻐﻁ‬ ‫ﺍﻟﻨﻔﺙ ‪ Jet‬ﺍﻟﺨﺎﺭﺝ ﻤﻥ ﺍﻟﻔﺘﺤﺔ ﺒﻴﻥ ﺃﻗل ﻗﻴﻤﺔ ﻟﻪ ﻋﻨﺩ ﺍﻹﻨﻜﻤﺎﺵ‬ ‫ﻭﺃﻗﺼﻰ ﻗﻴﻤﺔ ﻟﻪ ﺒﻌﺩ ﺤﻭﺍﻟﻰ ٤ ﺃﻭ ٥ ﺃﻤﺜﺎل ﺍﻟﻘﻁـﺭ ‪ D‬ﺒﻌـﺩ‬ ‫ﺍﻟﻔﺘﺤﺔ ﻓﻲ ﺇﺘﺠﺎﻩ ﺍﻟﺴﺭﻴﺎﻥ.‬ ‫ﻭﺍﻟﻌﻴﺏ ﺍﻷﺴﺎﺴﻰ ﻟﻠﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ ﺒﺎﻟﻤﻘﺎﺭﻨﺔ ﺒﺎﻟﻤﻘﻴﺎﺱ ﺫﻭ‬ ‫ﺍﻟﻔﻭﻫﺔ ﺃﻭ ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﻫﻭ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ ﻜﺒﻴـﺭ ﻭﻤـﻥ‬ ‫ﻨﺎﺤﻴﺔ ﺃﺨﺭﻯ ﻓﺈﻨﻪ ﻏﻴﺭ ﻤﺭﺘﻔﻊ ﺍﻟﺜﻤﻥ ﻭﺒﺈﻤﻜﺎﻨﻪ ﻗﻴـﺎﺱ ﺍﻟﻜﻤﻴـﺔ‬ ‫ﺒﺩﻗﺔ، ﻋﻠﻰ ﺴﺒﻴل ﺍﻟﻤﺜﺎل ﻟﺤﺴﺎﺏ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘـﺎﺱ ﻋﺒـﺭ‬ ‫ﺍﻟﻔﺘﺤﺔ ‪ Orifice‬ﻟﺨﻁ ﺃﻨﺎﺒﻴﺏ ﻗﻁﺭﻩ ٢١ ﺒﻭﺼﺔ ﻭﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ‬ ‫ﺤﻭﺍﻟﻰ ٠٠٤ ﻤﺘﺭ ﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ :‬ ‫ﻨﻔﺘﺭﺽ ﺃﻥ ﻗﻁﺭ ﺍﻟﻔﺘﺤﺔ ﻴﺴﺎﻭﻯ ٥٧٦,٠ ﻗﻁـﺭ ﺍﻟﺨـﻁ ﺃﻯ‬ ‫ﻴﺴﺎﻭﻯ ٨ ﺒﻭﺼﺔ، ﺒﺘﻁﺒﻴﻕ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺭﻗﻡ )١( ﻭﺇﻋﺘﺒـﺎﺭ = ‪Kd‬‬ ‫‪π‬‬ ‫‪Q = Kd‬‬ ‫‪d 2 2 gh‬‬ ‫٦٩٥,٠‬ ‫4‬ ‫- ٢٢ -‬
  • 24. ‫⎞ 45.2 × 8 ⎛ ‪π‬‬ ‫2‬ ‫٦٨٦,١ = ‪2 × 9.8h , h‬‬ ‫004‬ ‫⎜ 695.0 =‬ ‫⎟‬ ‫0063‬ ‫⎠ 001 ⎝ 4‬ ‫‪mt‬‬ ‫ﻭﺒﻔﺭﺽ ﺃﻥ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺯﻴﺕ ﻜﺜﺎﻓﺘﻪ ٢٨٨,٠ ﺠﻡ/ ﺴﻡ٣‬ ‫ﻴﻜﻭﻥ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘﺎﺱ ﻋﺒﺭ ﺍﻟﻔﺘﺤﺔ ﻴﺴﺎﻭﻯ‬ ‫288.0‬ ‫× 686.1 = ‪∆P‬‬ ‫2 ‪= 0.148 kg / cm‬‬ ‫01‬ ‫ﻭﻋﻨﺩ ﺇﺨﺘﻴﺎﺭ ﻤﻘﻴﺎﺱ ﺍﻟﻔﺘﺤﺔ ﻴﺠﺏ ﻤﺭﺍﻋﺎﺓ ﺍﻟﺤـﺩ ﺍﻷﻗﺼـﻰ‬ ‫ﻟﻠﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻟﻠﻀﻐﻁ ﻋﺒﺭ ﺍﻟﻤﻘﻴﺎﺱ ‪ Head loss‬ﺤﻴﺙ ﻴﺠﺏ ﺃﻥ‬ ‫ﻴﻜﻭﻥ ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻟﻠﻀﻐﻁ ﺃﻗل ﻤﺎ ﻴﻤﻜﻥ ﻭﻴﻨﺒﻐﻰ ﺃﻻ ﺘﺼل ﻗﻴﻤﺔ‬ ‫ﻫﺫﺍ ﺍﻟﻔﺎﻗﺩ ﺇﻟﻰ ٥٢,٠ ﻜﺠﻡ/ﺴﻡ٢ ﺒﺄﻯ ﺤﺎل ﻤـﻥ ﺍﻷﺤـﻭﺍل ﻷﻥ‬ ‫ﻫﺫﺍ ﻤﻌﻨﺎﻩ ﺤﺩﻭﺙ ﻓﻘﺩ ﻜﺒﻴﺭ ﻨﺴﺒﻴﺎ ﻓﻲ ﻁﺎﻗﺔ ﺍﻟﺴﺎﺌل ﻤﻘﺎﺒل ﻗﻴﺎﺱ‬ ‫ﹰ‬ ‫ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ.‬ ‫ﻤﻠﺤﻭﻅﺔ: ﻴﻤﻜﻥ ﺘﻁﺒﻴﻕ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺭﻗﻡ )١( ﻓﻲ ﺤﺎﻟﺔ ﻗﻴـﺎﺱ‬ ‫ﺍﻟﻜﻤﻴﺔ ﻟﻠﻤﻭﺍﺌﻊ ﺍﻟﻘﺎﺒﻠﺔ ﻟﻼﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﻐﺎﺯﺍﺕ ﺒﺸﺭﻁ ﺃﻻ ﺘﺯﻴﺩ‬ ‫ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﺍﻟﻐﺎﺯ ﻋﻥ ٠٠١ ﻤﺘﺭ ﻓﻲ ﺍﻟﺜﺎﻨﻴﺔ ﺤﻴﺙ ﺃﻨﻪ ﻋﻨـﺩ‬ ‫ﻫﺫﻩ ﺍﻟﺴﺭﻋﺔ ﺘﺘﻐﻴﺭ ﻜﺜﺎﻓﺔ ﺍﻟﻐﺎﺯ ﺘﻐﻴﺭ ﻁﻔﻴﻑ ﺠﺩﺍ ﺃﻯ ﺃﻨﻪ ﻴﻤﻜﻥ‬ ‫ﹰ‬ ‫ﺇﻫﻤﺎل ﺘﺄﺜﻴﺭ ﺇﻨﻀﻐﺎﻁﻴﺔ ﺍﻟﻐﺎﺯ ﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻭﺇﻋﺘﺒﺎﺭ ﺍﻟﻐـﺎﺯ‬ ‫ﻜﻤﺎﺌﻊ ﻏﻴﺭ ﻗﺎﺒل ﻟﻺﻨﻀﻐﺎﻁ ﻤﺜل ﺍﻟﺴﻭﺍﺌل.‬ ‫- ٣٢ -‬
  • 26. ‫٢- ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﻭﻫﺔ)‪:(Flow-Nozzle Meter‬‬ ‫ﻴﺘﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻤﻘﻴﺎﺱ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ D‬ﻴﻜـﻭﻥ‬ ‫ﺃﻜﺒﺭ ﻤﻥ ٥ﺴﻡ ﻭﻤﺭﻜﺏ ﺩﺍﺨﻠﻬﺎ ﺃﻨﺒﻭﺒﺔ ﻗﺼﻴﺭﺓ ﻤﺘﻐﻴﺭﺓ ﺍﻟﻤﻘﻁـﻊ‬ ‫ﺒﺈﻨﺘﻅﺎﻡ ﻭﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ d‬ﻜﻤﺎ ﺒﺎﻟﺸﻜل )٦( ﺒﺤﻴﺙ ﺘﻜﻭﻥ ﻨﺴﺒﺔ‬ ‫2‬ ‫⎞ ⎛ ﻓﻲ ﺤﺩﻭﺩ ٢,٠ ﺇﻟﻰ ٥٥,٠، ﺒﺘﻁﺒﻴـﻕ‬ ‫ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁﻊ‬ ‫‪d‬‬ ‫⎟ ⎜‬ ‫⎠‪⎝D‬‬ ‫ﻤﻌﺎﺩﻟﺔ ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺍﻟﻨﻘﻁﺘﻴﻥ )١(، )٢( ﻤﻊ ﻭﻀـﻊ ﺘـﺄﺜﻴﺭ‬ ‫ﺍﻟﻠﺯﻭﺠﺔ ﻓﻲ ﺍﻹﻋﺘﺒﺎﺭ.‬ ‫21‪10 4 P1 V‬‬ ‫22‪10 4 P2 V‬‬ ‫+‬ ‫= 1‪+ Z‬‬ ‫+‬ ‫‪+ Z2 + hf‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ hf‬ﻫﻭ ﺍﻟﻔﺎﻗﺩ ﺒﺎﻹﺤﺘﻜﺎﻙ ﺒﻴﻥ ﺍﻟﻨﻘﻁﺘـﻴﻥ )١(، )٢(‬ ‫ﻤـﻊ ﺇﻋﺘﺒـﺎﺭ ﺍﻟﻤﺴـﺘﻭﻯ ﺍﻟﻘﻴﺎﺴـﻰ ﻫـﻭ ﻤﺤـﻭﺭ ﺍﻷﻨﺒﻭﺒـﺔ‬ ‫ـ‬ ‫ـ‬ ‫ـ ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫22‪10 4 P1 V12 10 4 P2 V‬‬ ‫+‬ ‫=‬ ‫+‬ ‫‪+ hf‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫‪w‬‬ ‫‪2g‬‬ ‫ﺒﺈﺴﺘﺨﺩﺍﻡ ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ ٢‪ A١V١=A٢V‬ﻭﺇﺩﺨﺎل ﻤﻌﺎﻤل‬ ‫ﺍﻟﺴﺭﻋﺔ ‪ KV‬ﻟﻴﺤل ﻤﺤل ﺍﻟﻔﺎﻗﺩ ﺒﺎﻻﺤﺘﻜﺎﻙ ‪hf‬‬ ‫) ‪10 4 P1 (V2 / K V‬‬ ‫) ‪10 4 P2 (V2 / K V‬‬ ‫2‬ ‫2‪⎛ A‬‬ ‫⎞‬ ‫2‬ ‫2‬ ‫+‬ ‫⎜‬ ‫‪⎜A‬‬ ‫= ⎟‬ ‫⎟‬ ‫+‬ ‫‪w‬‬ ‫‪2g‬‬ ‫1 ⎝‬ ‫⎠‬ ‫‪w‬‬ ‫‪2g‬‬ ‫- ٥٢ -‬
  • 27. ‫) 2‪10 4 (P1 − P‬‬ ‫⎤ ⎞ 2‪V22 ⎡ ⎛ A‬‬ ‫2‬ ‫=‬ ‫‪⎢1 − ⎜ ⎟ ⎥ = H 1 − H 2 = h‬‬ ‫⎥ ⎠ 1‪2 gK v2 ⎢ ⎜ A‬‬ ‫⎟‬ ‫⎝ ⎣‬ ‫‪w‬‬ ‫⎦‬ ‫‪2 gh‬‬ ‫‪V2 = K v‬‬ ‫‪⎡ ⎛A‬‬ ‫⎞‬ ‫2‬ ‫⎤‬ ‫2 ⎜ − 1⎢‬ ‫⎜‬ ‫⎟‬ ‫⎟‬ ‫⎥‬ ‫1‪⎢ ⎝ A‬‬ ‫⎣‬ ‫⎠‬ ‫⎥‬ ‫⎦‬ ‫ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ )ﺍﻟﻜﻤﻴﺔ( ‪ Q‬ﺍﻟﻤـﺎﺭ ﺨـﻼل‬ ‫ﺍﻟﻔﻭﻫﺔ ﻤﻥ ﻤﻌﺎﺩﻟﺔ ﺍﻹﺴﺘﻤﺭﺍﺭ‬ ‫‪π‬‬ ‫= 2‪Q = A2V‬‬ ‫2 ‪d 2V‬‬ ‫4‬ ‫‪π‬‬ ‫‪2 gh‬‬ ‫. ‪= Kd‬‬ ‫2‪d‬‬ ‫4‬ ‫⎤ 4⎞ ‪⎡ ⎛ d‬‬ ‫⎥ ⎟ ⎜ − 1⎢‬ ‫⎥ ⎠‪⎢ ⎝D‬‬ ‫⎣‬ ‫⎦‬ ‫ﺤﻴﺙ ﺃﻥ ‪ Kd=KV‬ﻭﻫﻭ ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ﻭﻴﻜﻭﻥ ﺃﻗل ﻤﻥ‬ ‫١ ﻭﻴﻤﻜﻥ ﺤﺴﺎﺏ ﻗﻴﻤﺔ ﻫﺫﺍ ﺍﻟﻤﻌﺎﻤل ﻤﻥ ﺍﻟﺘﺠﺎﺭﺏ ﺍﻟﻤﻌﻤﻠﻴﺔ ﻭﻓﻲ‬ ‫ﻤﻌﻅﻡ ﺍﻷﺤﻴﺎﻥ ﻟﺘﺴﻬﻴل ﺍﻟﺤﺴﺎﺒﺎﺕ ﻴﻤﻜﻥ ﺇﻋﺘﺒﺎﺭ ﺍﻟﻘﻴﻤﺔ ﺍﻟﺘﻘﺭﻴﺒﻴﺔ‬ ‫ﻟﻬﺫﺍ ﺍﻟﻤﻌﺎﻤل ﺘﺘـﺭﺍﻭﺡ ﺒـﻴﻥ ٥٣٩,٠ ﻟﻸﻗﻁـﺎﺭ ﻭﺍﻟﺴـﺭﻋﺎﺕ‬ ‫ﺍﻟﺼﻐﻴﺭﺓ ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )٢( ﺇﻟﻰ ٨٨٩,٠ ﻟﻸﻗﻁﺎﺭ ﻭﺍﻟﺴـﺭﻋﺎﺕ‬ ‫ﺍﻟﻜﺒﻴﺭﺓ ﻨﺴﺒﻴﺎ ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )٢( ﻭﺒﻬﺫﻩ ﺍﻟﻁﺭﻴﻘﺔ ﻴﻤﻜـﻥ ﻗﻴـﺎﺱ‬ ‫ﹰ‬ ‫ﺍﻟﻜﻤﻴﺔ ﺒﻤﻌﺭﻓﺔ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺒﻴﻥ ﻗﺒل ﻤﺩﺨل ﺍﻟﻔﻭﻫـﺔ ﻭﻋﻨـﺩ‬ ‫ﻤﺨﺭﺠﻬﺎ.‬ ‫- ٦٢ -‬
  • 28. ‫ﻭﺍﻟﺭﺴﻡ ﺒﺎﻟﺸﻜل )٦( ﻴﻭﻀﺢ ﺘﻐﻴﺭ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻤﻊ ﺍﻟﻁﻭل‬ ‫ﻟﻜﻤﻴﺔ ﻤﻌﻴﻨﺔ ﺨﻼل ﺍﻟﻔﻭﻫﺔ ﺒﺈﻋﺘﺒـﺎﺭ ﺃﻥ ﺍﻟﻤﺴـﺘﻭﻯ ﺍﻟﻘﻴﺎﺴـﻰ‬ ‫ﺍﻟﻤﻨﺎﺴﺏ ﻫﻭ ﻤﺤﻭﺭ ﺍﻟﻔﻭﻫﺔ ﻭﻨﺤﺩﺩ ﺍﻷﻁﻭﺍل ﻋﻠﻴﻪ ﺃﻤﺎ ﺍﻟﻤﺤـﻭﺭ‬ ‫ﺍﻟﺭﺃﺴﻰ ﻓﻴﻤﺜل ﺼﻭﺭ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻤﺨﺘﻠﻔﺔ ﻓﻌﻨﺩ ﺍﻟﻨﻘﻁـﺔ )١( ﻨﺒـﺩﺃ‬ ‫1‪10 4 P‬‬ ‫ﻭﻨﻀـﻴﻑ‬ ‫ﺒﺘﻭﻗﻴﻊ ﻤﺴﺎﻓﺔ ﺭﺃﺴﻴﺔ ﺘﻤﺜل ﻁﺎﻗﺔ ﺍﻟﻀـﻐﻁ‬ ‫‪w‬‬ ‫2‪V‬‬ ‫ﺇﻟﻴﻬﺎ ﻤﺴﺎﻓﺔ ﺃﺨﺭﻯ ﺘﻤﺜل ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ 1 ﻓﻨﺤﺼـل ﻋﻠـﻰ‬ ‫‪2g‬‬ ‫ﻨﻘﻁﺔ ﺘﻤﺜل ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻨﻘﻁﺔ )١( ﻭﻨﻜـﺭﺭ ﺫﻟـﻙ ﻋﻨـﺩ‬ ‫ﺍﻟﻨﻘﻁﺔ )٢( ﻓﻨﺤﺼل ﻋﻠﻰ ﻨﻘﻁﺔ ﺃﺨﺭﻯ ﺘﻤﺜل ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ‬ ‫ﻨﻘﻁﺔ )٢( ﻭﻨﻜﺭﺭ ﻫﺫﻩ ﺍﻟﻌﻤﻠﻴﺔ ﻋﻨﺩ ﺃﻭﻀﺎﻉ ﻤﺨﺘﻠﻔﺔ ﻋﻠﻰ ﻁﻭل‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﻭﺫﻟﻙ ﺒﻤﻘﻴﺎﺱ ﺭﺴﻡ ﻤﻌﻴﻥ ﻭﺒﺘﻭﺼـﻴل ﻫـﺫﻩ ﺍﻟـﻨﻘﻁ‬ ‫ﻨﺤﺼل ﻋﻠﻰ ﺨﻁ ﻴﻤﺜل ﺘﻐﻴﺭ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴـﺔ ﺨـﻼل ﺍﻟﻔﻭﻫـﺔ‬ ‫ﻭﻴﻁﻠﻕ ﻋﻠﻴﻪ ﺇﻨﺤـﺩﺍﺭ ﺍﻟﻁﺎﻗـﺔ ‪(E.G) Energy Gradient‬‬ ‫ﻭﺘﻜﻭﻥ ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ ﻋﻨﺩ ﻤﺨﺭﺝ ﺍﻟﻔﻭﻫﺔ ﺃﻗل ﻤﻨﻬﺎ ﻋﻨﺩ ﻤﺩﺨﻠﻬﺎ‬ ‫ﺒﻤﻘﺩﺍﺭ ‪ hf‬ﻭﺇﺫﺍ ﺘﻡ ﺘﻭﺼﻴل ﻨﻘﻁ ﺘﻭﻗﻴﻊ ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ ﻨﺤﺼـل‬ ‫ﻋﻠﻰ ﺨﻁ ﻴﻤﺜل ﺘﻐﻴﺭ ﺍﻟﻀﻐﻁ ﺨﻼل ﺍﻟﻔﻭﻫـﺔ ﻭﻴﻁﻠـﻕ ﻋﻠﻴـﻪ‬ ‫ﺇﻨﺤﺩﺍﺭ ﺍﻟﻀﻐﻁ ‪ (H.G) Hydraulic Gradient‬ﻭﻴﺘﻀﺢ ﺃﻥ‬ ‫ﺇﻨﺤﺩﺍﺭ ﺍﻟﻀﻐﻁ ﻴﻨﺨﻔﺽ ﻋﻥ ﺇﻨﺤﺩﺍﺭ ﺍﻟﻁﺎﻗﺔ ﺒﻘﺩﺭ ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ‬ ‫- ٧٢ -‬
  • 29. ‫2‪V‬‬ ‫ﻋﻨﺩ ﻫﺫﻩ ﺍﻟﻨﻘﻁﺔ ﻭﻨﻼﺤﻅ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ﻋﺒﺭ ﺍﻟﻤﻘﻴـﺎﺱ‬ ‫‪2g‬‬ ‫ﻴﺴﺎﻭﻯ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ ﻋﺒﺭ ﺍﻟﻤﻘﻴﺎﺱ ﻭﺫﻟﻙ ﻟﺘﺴـﺎﻭﻯ ﺍﻟﺴـﺭﻋﺔ‬ ‫ﻭﻜﺫﻟﻙ ﻁﺎﻗﺔ ﺍﻟﻭﻀﻊ ﻋﻨﺩ ﻤﺩﺨل ﻭﻤﺨﺭﺝ ﺍﻟﻤﻘﻴـﺎﺱ ﻭﻴﺴـﺒﺏ‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﻭﻫﺔ ﻓﺎﻗﺩ ﻀﻐﻁ ﺃﻜﺒﺭ ﻤﻥ ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﻭﺃﻗل‬ ‫ﻤﻥ ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ.‬ ‫٣- ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ‪:Venturi Meter‬‬ ‫ﺸﻜل )٧(‬ ‫- ٨٢ -‬
  • 30. ‫ﻴﺘﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻤﻘﻴﺎﺱ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻗﻁﺭﻫﺎ ﺍﻟﺩﺍﺨﻠﻰ ‪ D‬ﻴﻜـﻭﻥ‬ ‫ﺃﻜﺒﺭ ﻤﻥ ٥ ﺴﻡ ﻭﻴﻅل ﻴﺼﻐﺭ ﺤﺘﻰ ﻴﺼل ﺇﻟﻰ ﺍﻟﻘﻁـﺭ ‪ d‬ﺜـﻡ‬ ‫ﻴﻜﺒﺭ ﺍﻟﻘﻁﺭ ﺘﺩﺭﻴﺠﻴﺎ ﻟﻴﺼل ﺇﻟﻰ ﻗﻴﻤﺘﻪ ﺍﻷﺼﻠﻴﺔ ﻜﻤـﺎ ﺒﺎﻟﺸـﻜل‬ ‫ﹰ‬ ‫2‬ ‫)٧( ﺒﺤﻴﺙ ﺘﻜﻭﻥ ﻨﺴﺒﺔ ﻤﺴﺎﺤﺔ ﺍﻟﻤﻘﻁـﻊ ⎞ ⎛ ﻓـﻲ ﺤـﺩﻭﺩ‬ ‫‪d‬‬ ‫⎟ ⎜‬ ‫⎠‪⎝D‬‬ ‫٥٠,٠ ﺇﻟﻰ ٥٥,٠.‬ ‫ﺒﺘﻁﺒﻴﻕ ﻤﻌﺎﺩﻟﺔ ﺒﺭﻨﻭﻟﻠﻰ ﻋﻠﻰ ﺍﻟﻨﻘﻁﺘﻴﻥ )١(، )٢( ﻤﻊ ﻭﻀﻊ‬ ‫ﺘﺄﺜﻴﺭ ﺍﻟﻠﺯﻭﺠﺔ ﻓﻲ ﺍﻹﻋﺘﺒﺎﺭ ﻭﺇﺴـﺘﺨﺩﺍﻡ ﻤﻌﺎﺩﻟـﺔ ﺍﻹﺴـﺘﻤﺭﺍﺭ‬ ‫ﻭﺇﺩﺨﺎل ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ‪ Kd‬ﻟﻴﺤل ﻤﺤل ﺍﻟﻔﺎﻗﺩ ﺒﺎﻹﺤﺘﻜﺎﻙ ‪hf‬‬ ‫ﻜﻤﺎ ﺘﻡ ﻟﻠﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﻭﻫﺔ ﻴﻤﻜﻥ ﺤﺴﺎﺏ ﺍﻟﻜﻤﻴـﺔ ‪ Q‬ﺍﻟﻤـﺎﺭﺓ‬ ‫ﺨﻼل ﺍﻟﻔﻨﺸﻭﺭﻯ‬ ‫‪π‬‬ ‫‪2 gh‬‬ ‫‪Q = Kd‬‬ ‫2‪d‬‬ ‫4‬ ‫⎤ 4⎞ ‪⎡ ⎛ d‬‬ ‫⎥ ⎟ ⎜ − 1⎢‬ ‫⎥ ⎠‪⎢ ⎝D‬‬ ‫⎣‬ ‫⎦‬ ‫ﻭﺒﻬﺫﻩ ﺍﻟﻁﺭﻴﻘﺔ ﻴﺘﻡ ﻗﻴﺎﺱ ﺍﻟﻜﻤﻴﺔ ﺒﻤﻌﺭﻓﺔ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺒـﻴﻥ‬ ‫ﻗﺒل ﺒﺩﺍﻴﺔ ﺘﺼﻐﻴﺭ ﺍﻟﻘﻁﺭ ﻭﻋﻨﺩ ﺃﻗل ﻗﻁﺭ ﻭﻴﻤﻜﻥ ﺭﺴﻡ ﺇﻨﺤـﺩﺍﺭ‬ ‫ﺍﻟﻁﺎﻗﺔ ﻭﺍﻟﻀﻐﻁ ﻭﻴﺘﻀﺢ ﻤﻨﻪ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ‪ hf‬ﺘﻘﺎﺒل ﺇﺴﺘﺨﺩﺍﻡ‬ ‫ﺍﻟﻤﻌﺎﻤل ‪ ،kd‬ﻭﻴﺴﺒﺏ ﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﻓﺎﻗﺩ ﻀﻐﻁ ﺼﻐﻴﺭ ﺠﺩﺍ‬ ‫ﹰ‬ ‫ﻭﻴﺘﺭﺍﻭﺡ ﻤﻌﺎﻤل ﺍﻟﺘﺼﺭﻴﻑ ﻟﻤﻘﻴﺎﺱ ﻓﻨﺸﻭﺭﻯ ﺒﻴﻥ ﻗﻴﻤﺔ ﺘﻘﺭﻴﺒﻴﺔ‬ ‫ﻗﺩﺭﻫﺎ ٥٣٩,٠ ﻟﻸﻗﻁﺎﺭ ﻭﺍﻟﺴﺭﻋﺎﺕ ﺍﻟﺼﻐﻴﺭﺓ ﻋﻨﺩ ﺍﻟﻤﻘﻁﻊ )٢(‬ ‫- ٩٢ -‬
  • 31. ‫ﺇﻟﻰ ٨٨٩,٠ ﻟﻸﻗﻁﺎﺭ ﻭﺍﻟﺴﺭﻋﺎﺕ ﺍﻟﻜﺒﻴﺭﺓ ﻨﺴﺒﻴﺎ ﻋﻨﺩ ﺍﻟﻤﻘﻁـﻊ‬ ‫ﹰ‬ ‫)٢( ﻭﻟﺘﺴﻬﻴل ﺍﻟﺤﺴﺎﺒﺎﺕ ﻴﻤﻜﻥ ﺇﻋﺘﺒﺎﺭ ﺍﻟﻘﻴﻤﺔ ﺍﻟﺘﻘﺭﻴﺒﻴـﺔ ﻟﻬـﺫﺍ‬ ‫ﺍﻟﻤﻌﺎﻤـل ﺘﺴـﺎﻭﻯ ٨٩,٠ – ٩٩,٠ ﻭﺘﻜـﻭﻥ ﻗﻴﻤـﺔ ﻤﻌﺎﻤـل‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ﺍﻟﺘﺼﺭﻴﻑ ﻟﻠﻬﻭﺍﺀ ﺤﻭﺍﻟﻰ ٩٩,٠‬ ‫ﻭﺍﻟﺠﺩﻭل ﺭﻗﻡ )١( ﻴﻭﻀﺢ ﻤﻘﺎﺭﻨﺔ ﻟﻘﻴﻤـﺔ ﺍﻟﻔﺎﻗـﺩ ﺍﻟﻜﻠـﻰ‬ ‫ﻟﻠﻀﻐﻁ ﻋﺒﺭ ﺍﻟﻤﻘﻴﺎﺱ ﻭﺫﻟﻙ ﻟﻸﻨﻭﺍﻉ ﺍﻟﺜﻼﺜﺔ ﺍﻟﺴﺎﺒﻘﺔ ﻷﺠﻬـﺯﺓ‬ ‫ﻗﻴﺎﺱ ﺍﻟﻜﻤﻴﺔ ﻭﺫﻟﻙ ﺒﺈﻋﺘﺒﺎﺭ ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘﺎﺱ ﻤﻘﺩﺍﺭ ﺜﺎﺒـﺕ‬ ‫ﻭﻴﺴﺎﻭﻯ ٠٣ﺴﻡ ﺯﺌﺒﻕ )٤,٠ﻜﺠﻡ/ﺴﻡ٢(.‬ ‫ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ‬ ‫ﻓﺭﻕ ﺍﻟﻀﻐﻁ‬ ‫ﻨﺴﺒﺔ‬ ‫ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻟﻠﻀﻐﻁ ﻋﺒﺭ‬ ‫ﻟﻠﻀﻐﻁ ﻋﺒﺭ‬ ‫ﺍﻟﻤﻘﺎﺱ ﻋﻨﺩ‬ ‫ﺍﻷﻗﻁﺎﺭ‬ ‫ﻨﻭﻉ‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﻜﻨﺴﺒﺔ ﻤﺌﻭﻴﺔ ﻤﻥ‬ ‫ﺍﻟﻤﻘﻴﺎﺱ‬ ‫ﺍﻟﻤﺂﺨﺫ ﺍﻟﻤﻼﺌﻤﺔ‬ ‫‪d‬‬ ‫ﺍﻟﻤﻘﻴﺎﺱ‬ ‫ﻓﺭﻕ ﺍﻟﻀﻐﻁ ﺍﻟﻤﻘﺎﺱ‬ ‫) (‬ ‫)٢‪(kg/cm‬‬ ‫)٢‪(kg/cm‬‬ ‫‪D‬‬ ‫٦١٢,٠‬ ‫٤٥%‬ ‫٤,٠‬ ‫٥٧٦,٠‬ ‫ﺫﻭ ﺍﻟﻔﺘﺤﺔ‬ ‫‪orifice‬‬ ‫٨١,٠‬ ‫٥٤%‬ ‫٤,٠‬ ‫٢٥٦,٠‬ ‫ﺫﻭ ﺍﻟﻔﻭﻫﺔ‬ ‫-‪Flow‬‬ ‫‪Nozzle‬‬ ‫٤٠,٠‬ ‫٠١%‬ ‫٤,٠‬ ‫٥,٠-‬ ‫ـﻭﺭﻯ‬‫ﻓﻨﺸـ‬ ‫٥٧٦,٠‬ ‫‪Venturi‬‬ ‫ﺠﺩﻭل )١(‬ ‫- ٠٣ -‬
  • 32. ‫ﺃﻁﻭﺍل ﺍﻷﻨﺎﺒﻴﺏ ﻗﺒل ﺃﺠﻬﺯﺓ ﺍﻟﻘﻴﺎﺱ ﻭﺒﻌﺩﻫﺎ:‬ ‫ﻋﻨﺩ ﺇﺴﺘﺨﺩﺍﻡ ﺃﺠﻬﺯﺓ ﻟﻘﻴﺎﺱ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺎﺭﺓ ﻓﻲ ﺍﻷﻨﺎﺒﻴﺏ ﻴﺠﺏ‬ ‫ﺃﻥ ﻴﺴﺒﻕ ﺍﻟﺠﻬﺎﺯ ﻁﻭل ﻤﺴﺘﻘﻴﻡ ﻤﻥ ﺍﻷﻨﺒﻭﺒـﺔ ‪Straight Run‬‬ ‫ﻟﻀﻤﺎﻥ ﺇﻨﺘﻅﺎﻡ ﺍﻟﺴﺭﻴﺎﻥ ﻗﺒل ﺍﻟﺠﻬـﺎﺯ ﻭﺨﺎﺼـﺔ ﺇﺫﺍ ﺇﺤﺘـﻭﺕ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﻋﻠﻰ ﺘﺭﻜﻴﺒﺎﺕ ﻤﺜل ﺍﻷﻜـﻭﺍﻉ، ﺍﻟﺘﻴﻬـﺎﺕ ﻭﺍﻟﻤﺤـﺎﺒﺱ‬ ‫ﻭﻜﺫﻟﻙ ﻴﺠﺏ ﺃﻥ ﻴﻠﻰ ﺍﻟﺠﻬﺎﺯ ﻁﻭل ﻤﺴﺘﻘﻴﻡ ﻤﻥ ﺍﻷﻨﺒﻭﺒﺔ ﻭﺫﻟـﻙ‬ ‫ﺤﺘﻰ ﻻ ﺘﺅﺜﺭ ﺍﻟﻀﻐﻭﻁ ﺍﻟﺨﻠﻔﻴﺔ ‪ Back pressure‬ﻋﻠﻰ ﺩﻗـﺔ‬ ‫ﺘﺘﺭﺍﻭﺡ ﺒـﻴﻥ‬ ‫ﺍﻟﺠﻬﺎﺯ ﻭﺇﺫﺍ ﻜﺎﻨﺕ ﺍﻟﻨﺴﺒﺔ ﺍﻟﺘﻘﺭﻴﺒﻴﺔ ﻟﻸﻗﻁﺎﺭ‬ ‫‪d‬‬ ‫‪D‬‬ ‫٢٥٦,٠ – ٥٧٦,٠ ﻴﻜﻭﻥ ﺍﻟﻁﻭل ﺍﻟﻤﺴـﺘﻘﻴﻡ ﺍﻟﺘﻘﺭﻴﺒـﻰ ﻗﺒـل‬ ‫ﺍﻟﻤﻘﻴﺎﺱ ﺫﻭ ﺍﻟﻔﺘﺤﺔ ‪ orifice‬ﻴﺴﺎﻭﻯ ٠٢ ﻤﺜل ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒـﺔ‬ ‫)‪ (٢٠ D‬ﻭﻴﻜﻭﻥ ﺍﻟﻁﻭل ﺍﻟﻤﺴﺘﻘﻴﻡ ﺍﻟﺘﻘﺭﻴﺒﻰ ﻗﺒـل ﺍﻟﻤﻘﻴـﺎﺱ ﺫﻭ‬ ‫ﺍﻟﻔﻭﻫﺔ ‪ Flow-Nozzle‬ﻭﻗﺒل ﻤﻘﻴـﺎﺱ ﻓﻨﺸـﻭﺭﻯ ‪Venturi‬‬ ‫ﻴﺴﺎﻭﻯ ٠٣ ﻤﺜل ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒﺔ )‪ (٣٠D‬ﻭﺫﻟﻙ ﻓﻲ ﺃﺴﻭﺃ ﺤﺎﻟـﺔ‬ ‫‪ Worst Case‬ﻤﻥ ﺃﻨﻭﺍﻉ ﺍﻟﺘﺭﻜﻴﺒﺎﺕ ﻭﻓﻲ ﺃﻏﻠﺏ ﺍﻷﺤﻴﺎﻥ ﻴﻜﻭﻥ‬ ‫ﺍﻟﻁﻭل ﺍﻟﻤﺴﺘﻘﻴﻡ ﺍﻟﺘﻘﺭﻴﺒﻰ ﺒﻌﺩ ﺍﻟﺠﻬﺎﺯ ﻴﺴﺎﻭﻯ ﺨﻤﺴـﺔ ﺃﻤﺜـﺎل‬ ‫ﻗﻁﺭ ﺍﻷﻨﺒﻭﺒﺔ )‪ (٥D‬ﻭﺫﻟﻙ ﻟﻜل ﺃﺠﻬﺯﺓ ﺍﻟﻘﻴﺎﺱ ﺍﻟﺴﺎﺒﻘﺔ.‬ ‫- ١٣ -‬
  • 33. ‫٤- ﺃﻨﺒﻭﺒﺔ ‪:Pitot‬‬ ‫ﺸﻜل )٨(‬ ‫ﺸﻜل )٩(‬ ‫- ٢٣ -‬
  • 34. ‫ﺘﺘﻜﻭﻥ ﺃﻨﺒﻭﺒﺔ ‪ Pitot‬ﻤﻥ ﺃﻨﺒﻭﺒﺔ ﻋﻠﻰ ﻫﻴﺌﺔ ﺯﺍﻭﻴـﺔ ﻗﺎﺌﻤـﺔ‬ ‫ﻭﻋﻨﺩﻤﺎ ﻴﻐﻤﺭ ﺍﻟﺠﺯﺀ ﺍﻟﻤﺜﻨﻰ ﺠﺯﺌﻴﺎ ﺘﺤﺕ ﺍﻟﻤﺎﺀ ﻭﻴﻭﺠﻪ ﻤﺒﺎﺸﺭﺓ‬ ‫ﹰ‬ ‫ﻹﺘﺠﺎﻩ ﺍﻟﺴﺭﻴﺎﻥ ‪ Flow‬ﻓﺈﻨﻪ ﻴﺒﻴﻥ ﺴﺭﻋﺔ ﺍﻟﺴـﺭﻴﺎﻥ ﺒﺎﻟﻤﺴـﺎﻓﺔ‬ ‫ﺍﻟﺘﻲ ﻴﺭﺘﻔﻌﻬﺎ ﺍﻟﻤﺎﺀ ﻓﻲ ﺍﻟﺠﺯﺀ ﺍﻟﺭﺃﺴﻰ ﻤﻥ ﺍﻷﻨﺒﻭﺒﺔ ﻋﻥ ﺴﻁﺢ‬ ‫2‪V‬‬ ‫ﻜﻤﺎ ﻫﻭ‬ ‫ﺍﻟﻤﺎﺀ ﺤﻴﺙ ﺃﻥ ﻫﺫﻩ ﺍﻟﻤﺴﺎﻓﺔ ﺘﺴﺎﻭﻯ ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ‬ ‫‪2g‬‬ ‫ﺒﺎﻟﺸﻜل )٨(.‬ ‫ﻭﺍﻟﺸﻜل ﺍﻟﻤﺘﻜﺎﻤل ﻟﻬﺫﻩ ﺍﻷﻨﺒﻭﺒﺔ ﻴﻌﺭﻑ ﺒﺈﺴﻡ ‪Pitot-Static‬‬ ‫ﻜﻤﺎ ﺒﺎﻟﺸﻜل )٩( ﻭﻫﻰ ﺘﺘﻜﻭﻥ ﻤﻥ ﺠﺯﺌﻴﻥ ﺃﺴﺎﺴﻴﻴﻥ ﻤﻨﻔﺼـﻠﻴﻥ‬ ‫ﻭﻤﺘﻭﺍﺯﻴﻴﻥ ﺃﺤﺩﻫﻡ ﻴﺒﻴﻥ ﻤﺠﻤﻭﻉ ﺍﻟﻀﻐﻁ ﺍﻟﻜﻠﻰ )ﺍﻟﻁﺎﻗﺔ ﺍﻟﻜﻠﻴﺔ(‬ ‫ﻭﺍﻵﺨﺭ ﻴﺒﻴﻥ ﺍﻟﻀﻐﻁ ﺍﻹﺴﺘﺎﺘﻴﻜﻰ )ﻁﺎﻗﺔ ﺍﻟﻀﻐﻁ( ﻓﻘـﻁ ﻭﻴـﺘﻡ‬ ‫ﺍﻟﺤﺼﻭل ﻋﻠﻰ ﺍﻟﻀﻐﻁ ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻰ )ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜـﺔ( ﺒﻁـﺭﺡ‬ ‫ﺍﻟﻀﻐﻁ ﺍﻹﺴﺘﺎﺘﻴﻜﻰ ﻤﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻜﻠﻰ ﺤﻴﺙ ﺃﻥ ﺃﻨﺒﻭﺒﺔ -‪Pitot‬‬ ‫‪ static‬ﺘﻘﻴﺱ ﺍﻟﻔﺭﻕ ﺒﻴﻥ ﺍﻟﻀﻐﻁ ﺍﻟﻜﻠﻰ ﻭﺍﻟﻀﻐﻁ ﺍﻹﺴـﺘﺎﺘﻴﻜﻰ‬ ‫ﻋﻨﺩ ﻨﻘﻁﺔ ﻭﺤﻴﺩﺓ ﻭﺘﺴﺘﺨﺩﻡ ﺍﻟﻤﺎﻨﻭﻤﺘﺭﺍﺕ ﺒﺼﻭﺭﺓ ﺸﺎﺌﻌﺔ ﻟﻘﻴﺎﺱ‬ ‫ﻫﺫﻩ ﺍﻟﻀﻐﻭﻁ.‬ ‫- ٣٣ -‬
  • 35. ‫ﻭﻴﻭﻀﺢ ﺸﻜل )٠١( ﺇﺴﺘﺨﺩﺍﻡ ﺃﻨﺒﻭﺒﺔ ‪ Pitot-Static‬ﻟﻘﻴﺎﺱ‬ ‫ﺍﻟﻜﻤﻴﺔ )ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ( ﻓـﻲ ﺍﻟﻘﻨـﻭﺍﺕ ﺍﻟﻤﻔﺘﻭﺤـﺔ ﻟﻠﺴـﺭﻴﺎﻥ‬ ‫ﺍﻟﻤﻨﺨﻔﺽ ﺍﻟﺴﺭﻋﺔ ﺤﻴﺙ ﺃﻨﻪ ﻴﺼﻌﺏ ﻗﻴﺎﺱ ﺇﺭﺘﻔﺎﻉ ﺍﻟﻤﺎﺀ ﻓـﻲ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﻓﻭﻕ ﺴﻁﺢ ﺍﻟﻤﺎﺀ ﺍﻟﻤﺘﺩﻓﻕ ﻭﻴﺘﻡ ﺫﻟﻙ ﺒﺘﻭﺼﻴل ﻁﺭﻓﻲ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﺒﺒﻌﺽ ﻤﻥ ﺃﻋﻠﻰ ﺒﻭﺍﺴﻁﺔ ﻭﺼﻠﺔ ﻋﻠﻰ ﺸﻜل ﺤـﺭﻑ‬ ‫‪ T‬ﻭﻴﻭﺼل ﺍﻟﻁﺭﻑ ﺍﻟﺜﺎﻟﺙ ﻟﻬﺎ ﺒﺨﻁ ﻴﻤﻜﻥ ﺘﻭﻟﻴﺩ ﺨﻠﺨﻠﺔ ﺠﺯﺌﻴﺔ‬ ‫ﺒﻪ ﻭﺒﻌﺩ ﺃﺨﺫ ﺍﻟﻬﻭﺍﺀ ﻤﻥ ﺃﻨﺒﻭﺒﺔ ‪ Pitot‬ﻴﺭﺘﻔﻊ ﺍﻟﻤﺎﺀ ﻷﻋﻠﻰ ﺇﻟﻰ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﺤﺘﻰ ﺍﻹﺭﺘﻔﺎﻉ ﺍﻟﻤﻘﺘﺭﺡ ﻟﺘﺴﻬﻴل ﺍﻟﻘﺭﺍﺀﺓ ﺜﻡ ﻴﻐﻠﻕ ﺨﻁ‬ ‫ﺍﻟﺨﻠﺨﻠﺔ ﻭﺘﺅﺜﺭ ﺍﻟﺨﻠﺨﻠﺔ ﺍﻟﺠﺯﺌﻴـﺔ ﺒﺎﻟﺘﺴـﺎﻭﻯ ﻋﻠـﻰ ﻁﺭﻓـﻲ‬ ‫ﺍﻟﻤﺎﻨﻭﻤﺘﺭ ﻭﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻟﻡ ﻴﺘﻐﻴﺭ ﻓﺭﻕ ﺍﻟـ ‪.Head‬‬ ‫ﺸﻜل )٠١(‬ ‫- ٤٣ -‬
  • 36. ‫ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ﻓﻲ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﻨﻘﺴﻡ ﻓﺎﻗﺩ ﺍﻟﻁﺎﻗﺔ ﻓﻲ ﺍﻷﻨﺎﺒﻴﺏ ﺇﻟﻰ ﻨﻭﻋﻴﻥ ﻫﻤﺎ :‬ ‫١- ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻨﺘﻴﺠﺔ ﺇﺠﻬﺎﺩﺍﺕ ﺍﻟﻘﺹ ﺍﻟﻠﺯﺝ ﺩﺍﺨـل‬ ‫ﺍﻟﺴﺎﺌل ﻭﺍﻹﻀﻁﺭﺍﺏ ﻋﻨﺩ ﺠﺩﺍﺭ ﺍﻷﻨﺒﻭﺒﺔ.‬ ‫٢- ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻨﺘﻴﺠﺔ ﻭﺠﻭﺩ ﺘﻐﻴﺭ ﻓـﻲ ﺴـﺭﻋﺔ ﺃﻭ‬ ‫ﺇﺘﺠﺎﻩ ﺍﻟﺴﺭﻴﺎﻥ ﻭﻨﻼﺤﻅ ﺃﻥ ﺘﻘﻠﻴل ﺍﻟﺴﺭﻋﺔ ﻴﺘﺴﺒﺏ ﻓﻲ‬ ‫ﻓﺎﻗﺩ ﻀﻐﻁ ﺃﻋﻠﻰ ﻤﻥ ﺯﻴﺎﺩﺓ ﺍﻟﺴﺭﻋﺔ.‬ ‫١- ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ‪:Friction Head Loss‬‬ ‫ﻴﻌﺘﻤﺩ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﺍﻟﻤـﺎﺭ‬ ‫ﻭﺴﺭﻋﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻭﺃﺒﻌﺎﺩ ﺍﻷﻨﺒﻭﺒﺔ ﻭﺍﻟﻤـﺎﺩﺓ ﺍﻟﻤﺼـﻨﻭﻉ ﻤﻨﻬـﺎ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﻭﻫﻭ ﻴﺴﺎﻭﻯ.‬ ‫‪l‬‬ ‫2 ‪⎛ V 2 ⎞ 0.81057 flQ‬‬ ‫‪hf = f‬‬ ‫⎜‬ ‫= ⎟ ‪⎜ 2g‬‬ ‫⎟‬ ‫‪d‬‬ ‫⎝‬ ‫⎠‬ ‫5 ‪gd‬‬ ‫2‪V‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ l‬ﻁﻭل ﺍﻷﻨﺒﻭﺒﺔ، ‪ d‬ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﻸﻨﺒﻭﺒﺔ،‬ ‫‪2g‬‬ ‫ﻁﺎﻗﺔ ﺍﻟﺤﺭﻜﺔ، ‪ Q‬ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ ﺃﻭ ﺍﻟﻜﻤﻴﺔ‬ ‫- ٥٣ -‬
  • 37. ‫‪ f‬ﻤﻌﺎﻤل ﺍﻹﺤﺘﻜﺎﻙ ﻭﺘﻌﺘﻤﺩ ﻗﻴﻤﺘﻪ ﻋﻠﻰ ﻨﻭﻉ ﺍﻟﺴـﺭﻴﺎﻥ ﻓـﻲ‬ ‫ﺍﻷﻨﺒﻭﺒﺔ ﺤﻴﺙ ﻴﻭﺠﺩ ﻨﻭﻋﺎﻥ ﻤﻥ ﺍﻟﺴﺭﻴﺎﻥ ﻓﻲ ﺍﻷﻨﺎﺒﻴـﺏ ﻫﻤـﺎ‬ ‫ﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﺭﻗﺎﺌﻘﻰ ‪ Laminar Flow‬ﻭﺍﻟﺴﺭﻴﺎﻥ ﺍﻟﻤﻀـﻁﺭﺏ‬ ‫‪ Turbulent Flow‬ﻭﻟﻜﻲ ﻴﺘﻡ ﻨﻘل ﺍﻟﺴﻭﺍﺌل ﺒﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ‬ ‫ﺒﺼﻭﺭﺓ ﺇﻗﺘﺼﺎﺩﻴﺔ ﺒﻤﻌﻨﻰ ﺘﺤﻘﻴﻕ ﺃﻗل ﺘﻜﻠﻔﺔ ﻜﻠﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ ﻓﺈﻥ‬ ‫ﺫﻟﻙ ﻴﺴﺘﻭﺠﺏ ﺃﻥ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴـﺎﺕ ﺍﻟﻤﻨﻘﻭﻟـﺔ ﺒـﺎﻟﺨﻁ ﻜﺒﻴـﺭﺓ‬ ‫ﻭﺒﺎﻟﺘﺎﻟﻰ ﻴﻜـﻭﻥ ﺍﻟﺴـﺭﻴﺎﻥ ﻤﻀـﻁﺭﺏ ‪Turbuleut FLow‬‬ ‫ﻭﻴﺘﺤﺩﺩ ﻨﻭﻉ ﺍﻟﺴﺭﻴﺎﻥ ﻋﻥ ﻁﺭﻴﻕ ﺭﻗﻡ ﺒﺩﻭﻥ ﻭﺤـﺩﺍﺕ ﻴﺴـﻤﻰ‬ ‫ﺭﻗﻡ ﺭﻴﻨﻭﻟﺩ ‪ Reynold's Number‬ﻭﻴﺭﻤﺯ ﻟﻪ ﺒـﺎﻟﺭﻤﺯ ‪RN‬‬ ‫ﻭﻫﻭ ﻴﺴﺎﻭﻯ‬ ‫)‪sp.gr × V (cm / sec) × d (cm‬‬ ‫= ‪RN‬‬ ‫)‪µ ( poise‬‬ ‫)‪25400 × V (mt / sec) × d (inch‬‬ ‫=‬ ‫) ‪γ (cst‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ sp.gr‬ﻫﻰ ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ ﻟﻠﺴﺎﺌل ﻭﻫﻰ ﺭﻗﻡ ﺒﺩﻭﻥ‬ ‫ﻭﺤﺩﺍﺕ ﻭﺘﺴﺎﻭﻯ ﻋﺩﺩﻴﺎ ﻜﺜﺎﻓﺔ ﺍﻟﺴﺎﺌل ﺒﺎﻟﺠﺭﺍﻡ/ ﺴﻨﺘﻴﻤﺘﺭ ﻤﻜﻌﺏ‬ ‫ﹰ‬ ‫‪ V‬ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﺍﻟﺴﺎﺌل ﺩﺍﺨل ﺍﻷﻨﺒﻭﺒﺔ‬ ‫‪ d‬ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﻸﻨﺒﻭﺒﺔ‬ ‫- ٦٣ -‬
  • 38. ‫‪ µ‬ﺃﻭ ‪ γ‬ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺍﻟﺩﻴﻨﺎﻤﻴﻜﻴﺔ )ﺍﻟﻤﻁﻠﻘﺔ( ﺃﻭ ﺍﻟﻜﻴﻨﻤﺎﺘﻴﻜﻴﺔ‬ ‫ﻭﻗﺩ ﻭﺠﺩ ﺃﻨﻪ ﺇﺫﺍ ﻜﺎﻥ ﺭﻗﻡ ﺭﻴﻨﻭﻟﺩ ﺃﻗل ﻤـﻥ ٠٠٠٢ ﻜـﺎﻥ‬ ‫ﺍﻟﺴﺭﻴﺎﻥ ﺭﻗﺎﺌﻘﻰ )ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﻤﻨﺨﻔﻀﺔ ﻨﺴﺒﻴﺎ( ﻭﻓـﻲ ﻫـﺫﻩ‬ ‫ﹰ‬ ‫ﺍﻟﺤﺎﻟﺔ ﺘﻜﻭﻥ ﺍﻟﻠﺯﻭﺠﺔ ﻫﻰ ﺍﻟﺴﺒﺏ ﺍﻷﻜﺒﺭ ﻟﻤﻘﺎﻭﻤﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻭﻓﻘﺩ‬ ‫ﺍﻟﻀﻐﻁ، ﻭﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻴﻜﻭﻥ‬ ‫) ‪γ (Cst‬‬ ‫7870.0 < ) ‪V (mt / sec‬‬ ‫)‪d (inch‬‬ ‫)‪Q(mt٣/hr) < ٠,١٤٣٦γ (cst). d(inch‬‬ ‫ﻭﺃﻴﻀﺎ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻴﺴﺎﻭﻯ‬ ‫ﹰ‬ ‫‪γlQ‬‬ ‫7177.2 = ‪h f‬‬ ‫4‪d‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ hf‬ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﺒﺎﻟﻤﺘﺭ‬ ‫‪l‬‬ ‫‪ γ‬ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺒﺎﻟﺴﻨﺘﻰ ﺴﺘﻭﻜﺱ‬ ‫ﻁﻭل ﺍﻷﻨﺒﻭﺒﺔ ﺒﺎﻟﻜﻴﻠﻭﻤﺘﺭ‬ ‫‪ Q‬ﻤﻌﺩل ﺍﻟﺴﺭﻴﺎﻥ ﺃﻭ ﺍﻟﻜﻤﻴﺔ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴـﺎﻋﺔ،‬ ‫‪ d‬ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﻸﻨﺒﻭﺒﺔ ﺒﺎﻟﺒﻭﺼﺔ‬ ‫- ٧٣ -‬
  • 39. ‫ﻭﺇﺫﺍ ﻜﺎﻥ ﺭﻗﻡ ﺭﻴﻨﻭﻟﺩ ﺃﻜﺒﺭ ﻤـﻥ ٠٠٠٤ ﻜـﺎﻥ ﺍﻟﺴـﺭﻴﺎﻥ‬ ‫ﻤﻀﻁﺭﺏ )ﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﻋﺎﻟﻴﺔ ﻨﺴﺒﻴﺎ ﻭﺃﻜﺜﺭ ﺇﻨﺘﻅﺎﻤﺎ(، ﻭﻓـﻲ‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻴﻜﻭﻥ ﺍﻟﺴﺒﺏ ﺍﻟﻤﻠﺤﻭﻅ ﺃﻜﺜﺭ ﻟﻤﻘﺎﻭﻤﺔ ﺍﻟﺴﺭﻴﺎﻥ ﻫـﻭ‬ ‫ﻨﺘﻴﺠﺔ ﺨﺸﻭﻨﺔ ﺠﺩﺍﺭ ﺍﻷﻨﺒﻭﺒﺔ ﻭﺍﻹﻀﻁﺭﺍﺏ ﻭﻓﻲ ﻫـﺫﻩ ﺍﻟﺤﺎﻟـﺔ‬ ‫ﻴﻜﻭﻥ‬ ‫) ‪γ (Cst‬‬ ‫84751.0 > )‪V (mt / sec‬‬ ‫)‪d (inch‬‬ ‫)‪Q(mt / hr ) > 0.287 γ (cst ). d (inch‬‬ ‫3‬ ‫ﻭﺃﻴﻀﺎ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻴﺴﺎﻭﻯ‬ ‫ﹰ‬ ‫57.1 ‪γ 0.25 l Q‬‬ ‫5245.71 = ‪h f‬‬ ‫57.4 ‪d‬‬ ‫ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓـﻲ ﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫‪hf‬‬ ‫ﺤﻴﺙ ﺃﻥ‬ ‫ﺒﺎﻟﻤﺘﺭ‬ ‫ﻟﺯﻭﺠﺔ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺴﻨﺘﻰ‬ ‫‪γ‬‬ ‫ﺴﺘﻭﻜﺱ‬ ‫ﻁﻭل ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﻜﻴﻠﻭﻤﺘﺭ‬ ‫‪l‬‬ ‫ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ‬ ‫‪Q‬‬ ‫ﻓﻲ ﺍﻟﺴﺎﻋﺔ‬ ‫- ٨٣ -‬
  • 40. ‫ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺒﻭﺼﺔ‬ ‫‪d‬‬ ‫٢- ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ‪:Minor losses‬‬ ‫⎞ 2 ‪⎛V‬‬ ‫⎞ 2 ‪⎛V‬‬ ‫ﻭﻫﻰ ﺘﺴﺎﻭﻯ ⎟ ⎜ ‪ hs = K‬ﺤﻴﺙ ﺃﻥ ⎟ ⎜ ﻫﻰ ﻁﺎﻗـﺔ‬ ‫⎟ ‪⎜ 2g‬‬ ‫⎟ ‪⎜ 2g‬‬ ‫⎝‬ ‫⎠‬ ‫⎝‬ ‫⎠‬ ‫ﺍﻟﺤﺭﻜﺔ، ‪ K‬ﻤﻌﺎﻤل ﻴﻌﺘﻤﺩ ﻋﻠﻰ ﻤﺼﺩﺭ ﺍﻟﻔﺎﻗﺩ ﻭﻴﻤﻜـﻥ ﺇﻴﺠـﺎﺯ‬ ‫ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻜﻤﺎ ﻓﻲ ﺍﻟﺠﺩﻭل )٢(.‬ ‫ﻤﻌﺎﻤل ﺍﻟﻔﺎﻗﺩ ‪K‬‬ ‫ﺍﻟﻔـــــﺎﻗﺩ‬ ‫٥,٠‬ ‫ﻓﻲ ﻤﺩﺨل ﺍﻷﻨﺒﻭﺒﺔ‬ ‫١‬ ‫ﻋﻨﺩ ﻤﺨﺭﺝ ﺍﻷﻨﺒﻭﺒﺔ‬ ‫٥,٠‬ ‫ﻋﻨﺩ ﺘﻘﻠﻴل ﻤﻘﻁﻊ ﺍﻷﻨﺒﻭﺒﺔ ﻓﺠﺄﺓ‬ ‫٥٠,٠‬ ‫ﻋﻨﺩ ﺘﻘﻠﻴل ﻤﻘﻁﻊ ﺍﻷﻨﺒﻭﺒﺔ ﺘﺩﺭﻴﺠﻴﺎ‬ ‫ﹰ‬ ‫١‬ ‫ﻓﻲ ﺍﻟﻜﻭﻉ ٠٩‪º‬‬ ‫٥,٠‬ ‫ﻓﻲ ﺍﻟﻜﻭﻉ ٥٤‪º‬‬ ‫٩,٠‬ ‫ﻓﻲ ﺍﻟﻭﺼﻠﺔ ﺘﻴﻪ‬ ‫٢,٠‬ ‫ﻓﻲ ﺍﻟﻤﺤﺒﺱ ﺍﻟﻤﻔﺘﻭﺡ ﺘﻤﺎﻤﺎ‬ ‫ﹰ‬ ‫ﺠﺩﻭل )٢(‬ ‫- ٩٣ -‬
  • 41. ‫ﻭﺘﻭﺠﺩ ﻁﺭﻴﻘﺔ ﺃﺨﺭﻯ ﻟﺤﺴﺎﺏ ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻫﻰ ﻁﺭﻴﻘـﺔ‬ ‫ﺍﻷﻁـﻭﺍل ﺍﻟﻤﻜﺎﻓﺌـﺔ ‪ Equivalent Length‬ﺒﻤﻌﻨـﻰ ﺃﻥ ﺃﻯ‬ ‫ﻤﺼﺩﺭ ﻤﻥ ﻤﺼﺎﺩﺭ ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﻴﻌﻁﻰ ﻓﻲ ﺼﻭﺭﺓ ﻁـﻭل‬ ‫ﻤﺴﺘﻘﻴﻡ ﻤﻥ ﺍﻷﻨﺒﻭﺒﺔ ﺒﺸﺭﻁ ﺃﻥ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓـﻲ ﻫـﺫﺍ‬ ‫ﺍﻟﻁﻭل ﻴﺴﺎﻭﻯ ﺍﻟﻔﺎﻗﺩ ﺍﻟﺜﺎﻨﻭﻯ ﻭﻫﻭ ﻴﺴﺎﻭﻯ‬ ‫2 ‪leq ⎛ V 2 ⎞ 0.81057 f leq Q‬‬ ‫‪hs = f‬‬ ‫⎜‬ ‫=⎟‬ ‫⎟ ‪d ⎜ 2g‬‬ ‫⎝‬ ‫⎠‬ ‫5 ‪gd‬‬ ‫- ٠٤ -‬
  • 42. (٣) ‫ ﻟﻤﺼﺎﺩﺭ ﺍﻟﻔﺎﻗﺩ ﺒﺎﻟﻤﺘﺭ ﻜﻤﺎ ﺒﺎﻟﺠﺩﻭل‬leq ‫ﻭﺘﻌﻁﻰ ﻗﻴﻡ‬ Welding Bends Valves Elbows Ratio Of Pipe Bend Long Short Welding Size Radius Radius Radius Tee Swing (Inch) To Pipe Gate Globe Angle Check Size ٥=‫ﻨﻕ=٦ ﻨﻕ‬ = ‫ﻨﻕ‬ ‫ﻨﻕ=٥,١ﺍﻟﻘﻁﺭ‬ ‫ﺍﻟﻘﻁﺭ ﺍﻟﻘﻁﺭ‬ ‫ﺍﻟﻘﻁﺭ‬ ١ ٠,١٥٠,١٨ ٠,٣٣ ٠,٤٣ ١,١٩ ٠,١٨ ٨,٨٤ ٤,٥٧ ٢,٢٢ ١,٢٥ ٠,١٨٠,٢٤ ٠,٤٣ ٠,٥٥ ١,٥٨ ٠,٢٤ ١١,٥٨ ٥,٧٩ ٢,٩٣ ١,٥ ٠,٢٤٠,٢٧ ٠,٤٩ ٠,٦٤ ١,٨٣ ٠,٢٧ ١٣,٧٢ ٦,٧ ٣,٣٥ ٢ ٠,٣٠٠,٣٣ ٠,٦٤ ٠,٨٥ ٢,٣٨ ٠,٣٦ ١٧,٣٧ ٨,٨٤ ٤,٢٧ ٢,٥ ٠,٣٦٠,٤٠ ٠,٧٦ ١ ٢,٨٣ ٠,٤٣ ٢١,٠٣ ١٠,٣٦ ٥,١٨ ٣ ٠,٤٦٠,٥٢ ٠,٩٤ ١,٢٥ ٣,٣٥ ٠,٥٥ ٢٥,٩١ ١٣,١١ ٦,٤ ٤ ٠,٦١٠,٦٧ ١,٢٢ ١,٦٤ ٤,٥٧ ٠,٧٣ ٣٤,١٤ ١٧,٠٧ ٨,٥٣ ٥ ٠,٧٦٠,٨٥ ١,٥٥ ٢,٠٤ ٥,٧٩ ٠,٨٨ ٤٢,٦٧ ٢١,٣٤١٠,٦٧ ٦ ٠,٩١ ١ ١,٨٦ ٢,٤٧ ٧ ١,٠٧ ٥١,٢١ ٢٥,٦ ١٢,٨ ٨ ١,١٩١,٣١ ٢,٤٤ ٣,٣٥ ٩,١٤ ١,٤٣ ٦٧,٦٧ ٣٣,٨٣١٧,٠٧ ١٠ ١,٤٩١,٦٨ ٣,٠٥ ٣,٩٦ ١١,٥٨ ١,٨ ٨٤,٧٣ ٤٢,٣٧٢١,٣٤ ١٢ ١,٧٧١,٩٥ ٣,٦٦ ٤,٨٨ ١٣,٧٢ ٢,١٣١٠١,١٩ ٥٠,٦ ٢٥,٣ ١٤ ١,٨٩٢,٠٧ ٣,٩٦ ٥,٤٩ ١٤,٩٣ ٢,٣٥١١٠,٩٥٥٥,٤٧٢٧,٧٤ ١٦ ٢,١٦٢,٣٨ ٤,٥٧ ٦,١ ١٧,٠٧ ٢,٦٨ ١٢٧,١ ٦٣,٤ ٣١,٧ - ٤١ -
  • 43. ‫٨١,٥ ٨٦,٢٤٤,٢ ٨١‬ ‫٧‬ ‫٦٦,٥٣٢٣,١٧٥٩,٢٤١٢٠,٣ ٢,٩١‬ ‫٩٧,٥ ٩٩,٢٤٧,٢ ٠٢‬ ‫٢٦,٧‬ ‫٣٩,٩٣٥٥,٩٧ ١,٩٥١ ٥٣,٣ ٤٦,١٢‬ ‫٦٦,٣٥٣,٣ ٤٢‬ ‫٧‬ ‫٤١,٩‬ ‫٥٨,٧٤١٧,٥٩٢٧,١٩١٦٩,٣ ١٩,٥٢‬ ‫ﺠﺩﻭل )٣(‬ ‫ﻭﻗﺩ ﻴﺘﻀﺢ ﻤﻥ ﺍﻟﺨﺒﺭﺓ ﺍﻟﻌﻤﻠﻴﺔ ﺃﻥ ﺍﻟﺒﻠﻭﻑ ﻤﻥ ﻨﻭﻉ ,‪Gate‬‬ ‫‪ Ball, Plug And Butterfly‬ﻟﻬﺎ ﻤﻘﺎﻭﻤﺔ ﻤﻨﺨﻔﻀﺔ ﻟﻠﺴﺭﻴﺎﻥ‬ ‫ﺃﻤﺎ ﺍﻟﺒﻠﻭﻑ ﺍﻷﺨﺭﻯ ﻤـﻥ ﻨـﻭﻉ ‪ Globe And Angle‬ﻟﻬـﺎ‬ ‫ﻤﻘﺎﻭﻤﺔ ﻤﺭﺘﻔﻌﺔ ﻟﻠﺴﺭﻴﺎﻥ.‬ ‫ﻭﻴﻁﻠﻕ ﻋﻠﻰ ﻤﺠﻤﻭﻉ ﻜﻼ ﻤﻥ ﻓﺎﻗـﺩ ﺍﻹﺤﺘﻜـﺎﻙ ﻭﺍﻟﻔﻭﺍﻗـﺩ‬ ‫ﹰ‬ ‫ﺍﻟﺜﺎﻨﻭﻴﺔ ﺍﻟﻔﺎﻗﺩ ﺍﻟﻜﻠﻰ ﻓﻲ ﺍﻷﻨﺒﻭﺒﺔ ﻭﻫﻭ ﻴﺴﺎﻭﻯ‬ ‫2 ‪l + leq ⎛ V 2 ⎞ 0.81057 f (l + leq)Q‬‬ ‫‪ht = h f + hs = f‬‬ ‫⎜‬ ‫=⎟‬ ‫⎟ ‪d ⎜ 2g‬‬ ‫⎝‬ ‫⎠‬ ‫5 ‪gd‬‬ ‫ﻭﻓﻲ ﺤﺎﻟﺔ ﺍﻟﺨﻁﻭﻁ ﺍﻟﻁﻭﻴﻠﺔ ﺘﻜﻭﻥ ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﺼـﻐﻴﺭﺓ‬ ‫ﺠﺩﺍ ﺒﺎﻟﻨﺴﺒﺔ ﻟﻔﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻭﺒﺎﻟﺘﺎﻟﻰ ﻴﻤﻜﻥ ﺇﻫﻤﺎﻟﻬﺎ ﺃﻤﺎ ﻓﻲ ﺤﺎﻟﺔ‬ ‫ﹰ‬ ‫ﺍﻟﺨﻁﻭﻁ ﺍﻟﻘﺼﻴﺭﺓ ﻤﺜل ﺸﺒﻜﺎﺕ ﺍﻟﺨﻁﻭﻁ ﺍﻟﺩﺍﺨﻠﻴﺔ ﻓﺈﻨﻪ ﻻ ﻴﻤﻜﻥ‬ ‫ﺇﻫﻤﺎل ﺍﻟﻔﻭﺍﻗﺩ ﺍﻟﺜﺎﻨﻭﻴﺔ ﺇﺫﺍ ﻤﺎ ﻗﻭﺭﻨﺕ ﺒﻔﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ.‬ ‫- ٢٤ -‬
  • 45. ‫ﻁﺭﻕ ﻨﻘل ﺍﻟﺒﺘﺭﻭل:‬ ‫ﻴﺘﻡ ﻨﻘل ﻤﺨﺘﻠﻑ ﺃﻨﻭﺍﻉ ﺍﻟﺒﺘﺭﻭل ﻭﻤﻨﺘﺠﺎﺘﻪ ﺇﻤﺎ ﻋﻥ ﻁﺭﻴـﻕ‬ ‫ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻭ ﺒﺈﺴﺘﺨﺩﺍﻡ ﺴﻴﺎﺭﺍﺕ ﺍﻟﺸﺤﻥ )ﺍﻟﻠـﻭﺍﺭﻯ( ﺃﻭ‬ ‫ﺒﺈﺴﺘﺨﺩﺍﻡ ﺼﻬﺎﺭﻴﺞ ﺍﻟﺴـﻜﺔ ﺍﻟﺤﺩﻴـﺩ ﺃﻭ ﺒﺈﺴـﺘﺨﺩﺍﻡ ﺍﻟﻨـﺎﻗﻼﺕ‬ ‫ﺍﻟﺒﺤﺭﻴﺔ )ﺍﻟﺴﻔﻥ( ﻭﻴﺘﻤﻴﺯ ﺍﻟﻨﻘل ﺒﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﺒﺈﺴـﺘﻤﺭﺍﺭ‬ ‫ﻋﻤﻠﻴﺔ ﺍﻟﻨﻘل ﺒﺼﺭﻑ ﺍﻟﻨﻅﺭ ﻋﻥ ﻨﻭﻉ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺃﻯ ﻴـﺘﻡ‬ ‫ﻨﻘل ﻤﺨﺘﻠﻑ ﺃﻨﻭﺍﻉ ﺍﻟﺴﻭﺍﺌل ﺒﺎﻟﺘﻌﺎﻗﺏ ﺩﺍﺨل ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻟﻴﺱ‬ ‫ﻨﻘل ﻨﻭﻉ ﻭﺍﺤﺩ ﻤﻥ ﺍﻟﺴﻭﺍﺌل ﻜﻤﺎ ﻴﺘﻡ ﺒﺈﺴﺘﺨﺩﺍﻡ ﺴﻴﺎﺭﺍﺕ ﺍﻟﺸﺤﻥ‬ ‫)ﺍﻟﻠﻭﺍﺭﻯ( ﺃﻭ ﺼﻬﺎﺭﻴﺞ ﺍﻟﺴﻜﺔ ﺍﻟﺤﺩﻴﺩ ﺃﻭ ﺍﻟﻨـﺎﻗﻼﺕ ﺍﻟﺒﺤﺭﻴـﺔ‬ ‫)ﺍﻟﺴﻔﻥ(.‬ ‫- ٤٤ -‬
  • 46. ‫ﺘﺼﻨﻴﻑ ﺃﻨﻅﻤﺔ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﺘﺼﻨﻑ ﺃﻨﻅﻤﺔ ﺨﻁﻭﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﺨﺎﺼﺔ ﺒﻨﻘل ﺍﻟﺒﺘﺭﻭل ﺇﻟـﻰ‬ ‫ﺜﻼﺜﺔ ﺃﻨﻭﺍﻉ :‬ ‫١- ﻨﻅﺎﻡ ﺍﻟﺘﺠﻤﻴﻊ ‪:Gathering System‬‬ ‫ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﺍﻟﻤﻌﺩﺍﺕ ﺍﻷﺨﺭﻯ ﺍﻟﻤﺴﺘﺨﺩﻤﺔ ﻟﻨﻘل ﺍﻟﺯﻴـﺕ‬ ‫ﺍﻟﺨﺎﻡ ﻭﻤﻨﺘﺠﺎﺘﻪ ﻤﻥ ﺍﻵﺒﺎﺭﺍﻟﻤﻨﻔﺭﺩﺓ ﻭﻤﻭﺍﻗﻊ ﺍﻹﻨﺘﺎﺝ ﺍﻷﺨﺭﻯ ﺇﻟﻰ‬ ‫ﻤﻭﻗﻊ ﺭﺌﻴﺴﻰ ﻴﺴﻤﻰ ﻨﻅﺎﻡ ﺘﺠﻤﻴﻊ، ﻭﺘﺘﻜﻭﻥ ﺃﻨﻅﻤـﺔ ﺍﻟﺘﺠﻤﻴـﻊ‬ ‫ﺃﺴﺎﺴﺎ ﻤﻥ ﻓﺭﻭﻉ ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺘﺴﺭﻯ ﺇﻟﻰ ﻤﺤﻁﺎﺕ ﺨﻁ ﺭﺌﻴﺴﻰ‬ ‫ﹰ‬ ‫ﺃﻭ ﻤﻭﺍﻗﻊ ﺃﺨﺭﻯ ﺤﻴﺙ ﻴﺘﻡ ﻨﻘل ﺍﻟﺯﻴﺕ ﻭﻤﻨﺘﺠﺎﺘﻪ ﺇﻟﻰ ﻨﻅﺎﻡ ﺨﻁ‬ ‫ﺭﺌﻴﺴﻰ، ﻭﺘﻜﻭﻥ ﻤﻌﻅـﻡ ﺍﻷﻗﻁﺎﺭﺍﻟﺸـﺎﺌﻌﺔ ﻟﻠﺨﻁـﻭﻁ ﺒﺘﻠـﻙ‬ ‫ﺍﻟﺘﻔﺭﻴﻌﺎﺕ ﻤﻥ ٤ ﺇﻟﻰ ٢١ ﺒﻭﺼﺔ ﻭﻴﺤﺘﻭﻯ ﻨﻅﺎﻡ ﺍﻟﺘﺠﻤﻴﻊ ﻋﺎﺩﺓ‬ ‫ﻋﻠﻰ ﻤﺤﻁﺎﺕ ﻀﺦ ﻟﺘﺠﻤﻴﻊ ﺍﻟﺯﻴﺕ ﻤﻥ ﺒﺌﺭ ﻤﻔﺭﺩ ﻭﻴﻜﻭﻥ ﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﻤﺴﺘﺨﺩﻡ ﺒﻨﻅﺎﻡ ﺍﻟﺘﺠﻤﻴﻊ ﻗﺼﻴﺭ ﺒﺎﻟﻤﻘﺎﺭﻨـﺔ ﺒﺨﻁـﻭﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﺭﺌﻴﺴﻴﺔ ﻭﻴﺘﺭﺍﻭﺡ ﻤﺩﻯ ﺍﻟﻁﻭل ﻤﻥ ﺃﻤﺘﺎﺭ ﻗﻠﻴﻠﺔ ﺇﻟـﻰ‬ ‫ﻋﺩﺓ ﻜﻴﻠﻭ ﻤﺘﺭﺍﺕ.‬ ‫- ٥٤ -‬
  • 47. ‫٢- ﻨﻅﺎﻡ ﺍﻟﺨﻁ ﺍﻟﺭﺌﻴﺴﻰ ‪:Trunk Line System‬‬ ‫ﻭﺘﻜﻭﻥ ﺍﻟﻤﺭﺤﻠﺔ ﺍﻟﺜﺎﻨﻴﺔ ﻫﻰ ﻨﻘل ﺍﻟﺯﻴﺕ ﺍﻟﺨﺎﻡ ﻭﻤﻨﺘﺠﺎﺘﻪ ﻋﻥ‬ ‫ﻁﺭﻴﻕ ﺨﻁـﻭﻁ ﺃﻨﺎﺒﻴـﺏ ﺭﺌﻴﺴـﻴﺔ ‪Trunk Pipe –Lines‬‬ ‫ﻭﻴﺴﺘﺨﺩﻡ ﻨﻅﺎﻡ ﺍﻟﺨﻁ ﺍﻟﺭﺌﻴﺴﻲ ﻟﻨﻘل ﺍﻟﺒﺘﺭﻭل ﻭﻤﻨﺘﺠﺎﺘـﻪ ﻤـﻥ‬ ‫ﺍﻵﺒﺎﺭ ﻭ ﻤﻭﺍﻗﻊ ﺍﻹﻨﺘﺎﺝ ﺍﻷﺨـﺭﻯ ﺇﻟـﻰ ﻤﻨـﺎﻁﻕ ﺍﻟﻤﻌﺎﻟﺠـﺔ‬ ‫ﺃﻭﺍﻟﺘﻜﺭﻴﺭ ﻭﺍﻟﺘﺴﻭﻴﻕ ﻭﺫﻟﻙ ﺒﻜﻤﻴﺎﺕ ﻜﺒﻴﺭﺓ ﻭﻟﻤﺴﺎﻓﺎﺕ ﻁﻭﻴﻠﺔ.‬ ‫٣- ﺃﻨﻅﻤﺔ ﺍﻟﺘﻭﺯﻴﻊ ‪:Distribution Systems‬‬ ‫ﻴﺘﻡ ﻨﻘل ﺍﻟﻤﻨﺘﺠﺎﺕ ﺍﻟﺒﺘﺭﻭﻟﻴﺔ ﻤﻥ ﻤﺼﺎﺩﺭ ﺍﻹﻤﺩﺍﺩ ﻤﺜل ﻤﻌﺎﻤل‬ ‫ﺍﻟﺘﻜﺭﻴﺭ ﻭﺍﻟﻤﻭﺍﻨﻰ ﺍﻟﺒﺤﺭﻴﺔ ﺇﻟﻰ ﻤﻨـﺎﻁﻕ ﺍﻹﺴـﺘﻬﻼﻙ ﺃﺴﺎﺴـﺎ‬ ‫ﹰ‬ ‫ﺒﻭﺍﺴﻁﺔ ﺃﻨﻅﻤﺔ ﺨﻁ ﺍﻟﺘﻭﺯﻴـﻊ ‪Pipe Line Distribution‬‬ ‫‪ ،Systems‬ﻭﺘﻜﻭﻥ ﻤﻌﻅﻡ ﺍﻟﻤﻨﺘﺠﺎﺕ ﺍﻟﺒﺘﺭﻭﻟﻴﺔ ﻫـﻰ ﺃﻨـﻭﺍﻉ‬ ‫ﺍﻟﺒﻨﺯﻴﻥ ﺍﻟﻤﺨﺘﻠﻔﺔ، ﻭﻗﻭﺩ ﺍﻟﻨﻔﺎﺜـﺎﺕ، ﺍﻟﻜﻴﺭﻭﺴـﻴﻥ، ﺍﻟﺴـﻭﻻﺭ،‬ ‫ﺍﻟﻤﺎﺯﻭﺕ ﻭﻜﺫﻟﻙ ﺍﻟﺒﻭﺘﺎﺠﺎﺱ ﺍﻟﻤﺴﺎل ﻭﺘﺨﺘﻠﻑ ﺨﻁﻭﻁ ﺃﻨﺎﺒﻴـﺏ‬ ‫ﺍﻟﺘﻭﺯﻴﻊ ﻟﻠﻤﻨﺘﺠﺎﺕ ﻋﻥ ﺨﻁﻭﻁ ﺃﻨﺎﺒﻴﺏ ﺍﻟﺯﻴﺕ ﺍﻟﺨﺎﻡ ﻓـﻲ ﺃﻨﻬـﺎ‬ ‫ﻋﺎﺩﺓ ﺘﺒﺩﺃ ﻜﺄﻨﻅﻤﺔ ﺫﺍﺕ ﺴﻌﺎﺕ ﻜﺒﻴﺭﺓ ﻭﺘﺘﻔﺭﻉ ﺇﻟﻰ ﺃﻨﻅﻤـﺔ ﺫﺍﺕ‬ ‫ﺴﻌﺎﺕ ﺃﺼﻐﺭ ﻜﺈﻤﺩﺍﺩﺍﺕ ﻟﻠﻤﻭﺍﻗﻊ ﺍﻟﻤﺨﺘﻠﻔﺔ.‬ ‫- ٦٤ -‬
  • 48. ‫ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻼﺯﻡ ﻟﻤﺸﺭﻭﻉ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﺴﺘﻬﻠﻙ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻼﺯﻡ ﻟﻠﻤﺸﺭﻭﻉ ﺃﺴﺎﺴﺎ ﻓـﻲ ﺘﻜـﺎﻟﻴﻑ‬ ‫ﹰ‬ ‫ﺇﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﺃﻴﻀﺎ ﺘﻜﺎﻟﻴﻑ ﺇﻨﺸﺎﺀ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ.‬ ‫ﹰ‬ ‫١- ﺘﻜﺎﻟﻴﻑ ﺇﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﻌﺘﺒﺭ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻓـﻲ ﺇﻨﺸـﺎﺀ ﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫)ﺩﻭﻻﺭ/ﻁﻥ ﺃﻭ ﺩﻭﻻﺭ/ ﻜﻴﻠﻭﻤﺘﺭ( ﻴﺘﻨﺎﺴﺏ ﻤﻊ ﻭﺯﻥ ﻤﻭﺍﺴـﻴﺭ‬ ‫ﺍﻟﺨﻁ ﻭﻫﻭ ﻴﺴﺎﻭﻯ ﺜﻤﻥ ﺍﻟﻤﻭﺍﺴﻴﺭ = ﺃ × ﻭﺯﻥ ﺍﻟﻤﻭﺍﺴﻴﺭ، ﺤﻴﺙ‬ ‫ﺃﻥ ﺃ ﻤﻌﺎﻤل ﻭﺃﻥ ﻭﺯﻥ ﺍﻟﻤﻭﺍﺴﻴﺭ ﻴﻌﺘﻤﺩ ﻋﻠـﻰ ﻗﻁـﺭ ﻭﺴـﻤﻙ‬ ‫ﻭﻁﻭل ﻫﺫﻩ ﺍﻟﻤﻭﺍﺴﻴﺭ.‬ ‫٢- ﺘﻜﺎﻟﻴﻑ ﺇﻨﺸﺎﺀ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ:‬ ‫ﻴﻌﺘﺒﺭ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻓﻲ ﺇﻨﺸـﺎﺀ ﻤﺤﻁـﺔ ﻟﻠﻀـﺦ‬ ‫)ﺩﻭﻻﺭ/ ﺤﺼﺎﻥ( ﻴﺘﻨﺎﺴﺏ ﻤﻊ ﻗﺩﺭﺓ ﻫﺫﻩ ﺍﻟﻤﺤﻁﺔ ﻭﻫﻭ ﻴﺴـﺎﻭﻯ‬ ‫ﺍﻟﺜﻤﻥ ﺍﻷﺴﺎﺴﻰ ﻟﻠﻤﻀﺨﺎﺕ.‬ ‫- ٧٤ -‬
  • 49. ‫ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻤﺸﺭﻭﻉ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ:‬ ‫ﺘﻨﻘﺴﻡ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ ﺇﻟﻰ ﺍﻟﺒﻨﻭﺩ ﺍﻵﺘﻴﺔ :‬ ‫ﻤﺼﺎﺭﻴﻑ ﺍﻟﺘﺸـﻐﻴل ﻭﺍﻟﺼـﻴﺎﻨﺔ ﻟﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ‬ ‫١-‬ ‫ﻭﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﻭﺘﺸﻤل ﺇﺴﺘﻬﻼﻙ ﺍﻟﺘﻴﺎﺭ ﺍﻟﻜﻬﺭﺒـﺎﺌﻲ‬ ‫ﻭﺍﻟﻤﻴﺎﻩ ﻭﻗﻁﻊ ﺍﻟﻐﻴﺎﺭ ﻭﺍﻟﻭﻗﻭﺩ ﻭﺍﻟﺯﻴﻭﺕ، ﻭﺘﻜـﺎﻟﻴﻑ‬ ‫ﺃﻋﻤﺎل ﺍﻟﺼﻴﺎﻨﺔ ﺍﻟﺘﻲ ﺘﺘﻡ ﻋﻥ ﻁﺭﻴﻕ ﺍﻟﻐﻴﺭ.‬ ‫ﺍﻟﻤﺭﺘﺒﺎﺕ ﻭﺍﻷﺠﻭﺭ.‬ ‫٢-‬ ‫ﺍﻟﻀﺭﺍﺌﺏ ﻭﺍﻟﺘﺄﻤﻴﻨﺎﺕ ﻭﻤﺎ ﺸﺎﺒﻪ ﺫﻟﻙ.‬ ‫٣-‬ ‫ﻤﺼﺎﺭﻴﻑ ﺍﻹﻫﻼﻙ ﺍﻟﺴﻨﻭﻴﺔ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻤﺤﻁـﺎﺕ‬ ‫٤-‬ ‫ﺍﻟﻀﺦ ﻭﺘﻌﺭﻑ ﺒﺄﻨﻬﺎ ﻨﺴﺒﺔ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻹﻨﺸﺎﺀ‬ ‫ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻭ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﺇﻟﻰ ﺍﻟﻌﻤﺭ ﺍﻹﻓﺘﺭﺍﻀﻰ‬ ‫ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻭ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﺤﻴﺙ ﻴـﺘﻡ ﺤﺴـﺎﺏ‬ ‫ﻤﺼﺎﺭﻴﻑ ﺍﻹﻫﻼﻙ ﺍﻟﺴﻨﻭﻴﺔ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺘﻘﺴﻴﻡ ﺭﺃﺱ‬ ‫ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻹﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﻋﻠـﻰ ﺍﻟﻌﻤـﺭ‬ ‫ﺍﻹﻓﺘﺭﺍﻀﻰ ﻟﻠﺨﻁ )ﺤﻭﺍﻟﻰ ٣٣ ﻋﺎﻤـﺎ( ﻭﻜـﺫﻟﻙ ﻴـﺘﻡ‬ ‫ﹰ‬ ‫ﺤﺴﺎﺏ ﻤﺼﺎﺭﻴﻑ ﺍﻹﻫﻼﻙ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻤﺤﻁﺎﺕ ﺍﻟﻀـﺦ‬ ‫ﺒﺘﻘﺴﻴﻡ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺜﻤﺭ ﻹﻨﺸﺎﺀ ﻤﺤﻁﺎﺕ ﺍﻟﻀـﺦ‬ ‫ﻋﻠﻰ ﺍﻟﻌﻤﺭ ﺍﻹﻓﺘﺭﺍﻀﻰ ﻟﻠﻤﻀﺨﺎﺕ )ﺤﻭﺍﻟﻰ ٥٢ ﻋﺎﻤﺎ(.‬ ‫ﹰ‬ ‫ﺃﻯ ﻤﺼﺭﻭﻓﺎﺕ ﺃﺨﺭﻯ ﻤﺜل ﺍﻟﻔﺎﺌﺩﺓ ﻋﻠﻰ ﺭﺃﺱ ﺍﻟﻤﺎل‬ ‫٥-‬ ‫ﺍﻟﻤﻘﺘﺭﺽ.‬ ‫- ٨٤ -‬
  • 50. ‫ﻭﺒﺫﻟﻙ ﻴﻤﻜﻥ ﺤﺴﺎﺏ ﺘﻜﻠﻔﺔ ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﻭﻫﻰ ﺘﺴﺎﻭﻯ‬ ‫ﺇﺠﻤﺎﻟﻰ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ‬ ‫ﺘﻜﻠﻔﺔ ﺍﻟﻨﻘل )ﺩﻭﻻﺭ/ﻁﻥ(‬ ‫)ﺩﻭﻻﺭ(‬ ‫=‬ ‫ﻜﻤﻴﺔ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻨﻘﻭﻟﺔ ﻓﻲ ﺍﻟﻌﺎﻡ )ﻁﻥ(‬ ‫ﻭﺒﻨﺎﺀ ﻋﻠﻰ ﻤﺎ ﺴﺒﻕ ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﺴﻌﺭ ﻨﻘل ﺍﻟﺒﺘـﺭﻭل ﺒﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﺒﻀﺭﺏ ﺘﻜﻠﻔﺔ ﺍﻟﻨﻘل ﻓﻲ ﻤﻌﺎﻤل ﺒﺤﻴﺙ ﻻ ﻴﺘﻌﺩﻯ ﺴﻌﺭ‬ ‫ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﺒﺎﻟﻁﺭﻕ ﺍﻷﺨﺭﻯ ﻭﺘﻌﺘﻤﺩ ﻗﻴﻤﺔ ﻫﺫﺍ ﺍﻟﻤﻌﺎﻤل ﻋﻠـﻰ‬ ‫ﺃﺴﻌﺎﺭ ﺍﻟﻨﻘل ﻟﻠﺸﺭﻜﺎﺕ ﺍﻷﺨﺭﻯ ﺍﻟﻤﻨﺎﻓﺴﺔ‬ ‫ﺃﺴﺱ ﺇﺨﺘﻴﺎﺭ ﻗﻁﺭ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ:‬ ‫ﻴﻌﺘﻤﺩ ﺇﺨﺘﻴﺎﺭ ﻗﻁﺭ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻋﻠﻰ ﻋﻤل ﺩﺭﺍﺴﺔ ﺘﺸـﻤل‬ ‫ﺍﻵﺘﻲ:‬ ‫١- ﺤﺴﺎﺏ ﺘﻜﺎﻟﻴﻑ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ، ﻭﻫﻰ ﻜﻤـﺎ ﺒﺎﻟﺸـﻜل‬ ‫)١١( ﻤﻨﺤﻨﻰ ١ ﺘﺯﺩﺍﺩ ﺒﺯﻴﺎﺩﺓ ﻗﻁﺭ ﺍﻟﺨﻁ.‬ ‫٢- ﺤﺴﺎﺏ ﺘﻜﺎﻟﻴﻑ ﻭﺤﺩﺍﺕ ﺍﻟﻀﺦ ﻭﻫﻰ ﻜﻤﺎ ﻨﺭﻯ ﻤﻨﺤﻨﻰ‬ ‫٢ ﺘﻘل ﺒﺯﻴﺎﺩﺓ ﻗﻁﺭ ﺍﻟﺨﻁ.‬ ‫- ٩٤ -‬
  • 51. ‫ﻭﺒﺠﻤﻊ ﺍﻟﻤﻨﺤﻨﻴﻴﻥ ١، ٢ ﻨﺤﺼل ﻋﻠـﻰ ﺍﻟﺘﻜـﺎﻟﻴﻑ ﺍﻟﻜﻠﻴـﺔ‬ ‫ﺍﻟﺴﻨﻭﻴﺔ ﻤﻨﺤﻨﻰ ٣ ﻭﺍﻟﻘﻁﺭ ﺍﻷﻤﺜل ﺇﻗﺘﺼﺎﺩﻴﺎ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻫـﻭ‬ ‫ﹰ‬ ‫ﺍﻟﻘﻁﺭ ﺍﻟﺫﻯ ﻟﻪ ﺃﻗل ﺘﻜﻠﻔﺔ ﻜﻠﻴﺔ ﻭﻗﺩ ﻭﺠﺩ ﺃﻥ ﺍﻟﺴﺭﻋﺔ ﺍﻟﻤﻨﺎﺴـﺒﺔ‬ ‫ﻟﻠﺴﻭﺍﺌل ﻓﻲ ﺍﻷﻨﺎﺒﻴﺏ ﻓﻲ ﻫـﺫﻩ ﺍﻟﺤﺎﻟـﺔ ﺘﺘـﺭﺍﻭﺡ ﺒـﻴﻥ ١:٣‬ ‫ﻤﺘﺭ/ﺜﺎﻨﻴﺔ.‬ ‫ﻭﻴﺘﻀﺢ ﻤﻥ ﺍﻟﺨﺒﺭﺓ ﺍﻟﻌﻤﻠﻴـﺔ ﺃﻥ ﺍﻟﺴـﺭﻋﺔ ﺘﻘﺘـﺭﺏ ﻤـﻥ‬ ‫١ﻤﺘﺭ/ﺜﺎﻨﻴﺔ ﻟﻠﺴﻭﺍﺌل ﻤﺭﺘﻔﻌﺔ ﺍﻟﻠﺯﻭﺠﺔ ﻭﺃﻴﻀـﺎ ﺘﻘﺘـﺭﺏ ﻤـﻥ‬ ‫ﹰ‬ ‫٣ﻤﺘﺭ/ﺜﺎﻨﻴﺔ ﻟﻠﺴﻭﺍﺌل ﻤﻨﺨﻔﻀﺔ ﺍﻟﻠﺯﻭﺠﺔ ﻭﻴﻌﺘﺒﺭ ﻫـﺫﺍ ﺍﻟﻤـﺩﻯ‬ ‫ﻟﺴﺭﻋﺔ ﺴﺭﻴﺎﻥ ﺍﻟﺴﻭﺍﺌل ﺩﺍﺨل ﺍﻷﻨﺎﺒﻴﺏ ﻫﻭ ﺍﻟﻘﻴﺩ ﻟﺭﻓﻊ ﻜﻔـﺎﺀﺓ‬ ‫ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ.‬ ‫ﻭﻋﻨﺩ ﺇﺨﺘﻴﺎﺭ ﻗﻁﺭ ﺨﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﻴﺠـﺏ ﺃﻥ ﻴﺅﺨـﺫ ﻓـﻲ‬ ‫ﺍﻹﻋﺘﺒﺎﺭ ﻤﻌﺎﻤل ﺍﻟﺨﺩﻤـﺔ ‪ Service Factor‬ﻟﺨﻁـﺔ ﺍﻟﻨﻘـل‬ ‫ﺍﻟﺴﻨﻭﻴﺔ ﻭﻫﻭ ﻴﻜﻭﻥ ﻓﻲ ﺤﺩﻭﺩ ٢٨% ﺒﻤﻌﻨﻰ ﺃﻥ ﻴﺘﻡ ﻨﻘل ﺍﻟﻜﻤﻴﺔ‬ ‫ﺍﻟﻤﻁﻠﻭﺒﺔ ﺴﻨﻭﻴﺎ ﺨﻼل ٠٠٣ ﻴﻭﻡ ﻓﻘﻁ ﻭﺫﻟﻙ ﺤﺘـﻰ ﻻ ﻴـﺅﺜﺭ‬ ‫ﹰ‬ ‫ﺇﻴﻘﺎﻑ ﺍﻟﺨﻁ ﻷﻯ ﺴﺒﺏ ﻋﻠﻰ ﺘﺤﻘﻴﻕ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟـﺔ ﺴـﻨﻭﻴﺎ‬ ‫ﹰ‬ ‫ﻭﻟﺫﻟﻙ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺘﺴﺎﻭﻯ‬ ‫- ٠٥ -‬
  • 52. ‫ﺸﻜل )١١(‬ ‫6 01 × ) ‪(million ton / year‬‬ ‫=‪Q‬‬ ‫‪7200 × sp.gr‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ sp.gr‬ﻫﻰ ﺍﻟﻜﺜﺎﻓﺔ ﺍﻟﻨﺴﺒﻴﺔ ﻟﻠﺴﺎﺌل ﺍﻟﻤﻨﻘﻭل ﺒﺎﻟﺨﻁ‬ ‫ﻭﺃﻴﻀﺎ ﺘﻜﻭﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌـﺏ ﻓـﻲ ﺍﻟﺴـﺎﻋﺔ‬ ‫ﹰ‬ ‫ﺘﺴﺎﻭﻯ 2‪. Q = ١,٨٢٤ Di‬‬ ‫ﺤﻴﺙ ﺃﻥ ‪ V‬ﻫﻰ ﺴﺭﻋﺔ ﺍﻟﺴﺎﺌل ﺩﺍﺨل ﺍﻟﺨﻁ ﺒﺎﻟﻤﺘﺭ/ﺜﺎﻨﻴﺔ.‬ ‫- ١٥ -‬
  • 53. ‫‪ Di‬ﻫﻭ ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺒﻭﺼﺔ، ﻭﻤﻤﺎ ﺴﺒﻕ‬ ‫ﻴﺘﻀﺢ ﺃﻨﻪ ﻟﻜﻲ ﻴﺘﻡ ﻨﻘل ﺍﻟﺒﺘﺭﻭل ﺒﺼﻭﺭﺓ ﺇﻗﺘﺼـﺎﺩﻴﺔ ﺒﻤﻌﻨـﻰ‬ ‫ﺘﺤﻘﻴﻕ ﺃﻗل ﺘﻜﻠﻔﺔ ﻜﻠﻴﺔ ﻟﻠﻤﺸﺭﻭﻉ ﻴﻜﻭﻥ ﺍﻟﺤﺩ ﺍﻷﺩﻨـﻰ ﻟﻠﻜﻤﻴـﺔ‬ ‫ﺍﻟﻤﻨﻘﻭﻟﺔ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺘﺴـﺎﻭﻯ 2‪Qmin = 1.824 Di‬‬ ‫ﻭﺃﻴﻀﺎ ﺒﻬﺩﻑ ﺭﻓﻊ ﻜﻔﺎﺀﺓ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻴﻜﻭﻥ ﺍﻟﺤـﺩ ﺍﻷﻗﺼـﻰ‬ ‫ﹰ‬ ‫ﻟﻠﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺘﺴﺎﻭﻯ 2‪. Qmax = 5.472 Di‬‬ ‫ﺍﻟﻌﻭﺍﻤل ﺍﻟﻤﺅﺜﺭﺓ ﻋﻠﻰ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﻜﻠﻴﺔ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل‬ ‫ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻴﺘﻀﺢ ﻤﻤﺎ ﺴﺒﻕ ﺃﻥ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺘﻨﺨﻔﺽ ﺒﺯﻴﺎﺩﺓ‬ ‫ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻨﻘﻭﻟﺔ ﺴﻨﻭﻴﺎ ﻭﺃﻥ ﻤﺴﺎﻓﺔ ﺍﻟﻨﻘل ﻟﻬﺎ ﺘﺄﺜﻴﺭ ﻗﻠﻴل ﺠـﺩﺍ،‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﻭﻗﺩ ﺘﺨﺘﻠﻑ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺒﺈﺨﺘﻼﻑ ﻤﻭﺍﺼﻔﺎﺕ ﺍﻟﺴﺎﺌل‬ ‫ﺍﻟﻤﻨﻘﻭل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻨﺫﻜﺭ ﻋﻠﻰ ﺴـﺒﻴل ﺍﻟﻤﺜـﺎل ﺍﻟﻌﻭﺍﻤـل‬ ‫ﺍﻵﺘﻴﺔ:‬ ‫١- ﺘﺼﺒﺢ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺃﻗل ﻤﺎ ﻴﻤﻜﻥ ﻋﻨﺩ ﻨﻘل‬ ‫ﺴﺎﺌل ﻭﺍﺤﺩ ﺫﻭ ﻟﺯﻭﺠﺔ ﻤﻨﺨﻔﻀﺔ ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ.‬ ‫- ٢٥ -‬
  • 54. ‫٢- ﺘﺯﺩﺍﺩ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﺍﻟـﺫﻯ‬ ‫ﻴﻨﻘل ﺴﻭﺍﺌل ﻤﺘﻌﺩﺩﺓ ﺒﺴـﺒﺏ ﺍﻟﺘﺭﻜﻴﺒـﺎﺕ ﺍﻹﻀـﺎﻓﻴﺔ‬ ‫ﻭﺍﻟﺨﻁﻭﻁ ﺍﻟﻔﺭﻋﻴﺔ.‬ ‫٣- ﺘﺯﺩﺍﺩ ﺍﻟﺘﻜﺎﻟﻴﻑ ﺍﻟﺴﻨﻭﻴﺔ ﻟﻠﻨﻘل ﺒﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﻤﻌﺯﻭل‬ ‫ﺤﺭﺍﺭﻴﺎ ﺒﺴﺒﺏ ﺃﻋﺒﺎﺀ ﺘﻜﺎﻟﻴﻑ ﺍﻟﻌﺯل ﺍﻟﺤﺭﺍﺭﻯ ﻟﻠﺨﻁ‬ ‫ﹰ‬ ‫ﻭﺘﻜﺎﻟﻴﻑ ﺯﻴﺎﺩﺓ ﻋﻤﻕ ﺍﻟﺨﻁ ﺘﺤﺕ ﺍﻷﺭﺽ ﻋﻥ ﺍﻟﻌﻤﻕ‬ ‫ﺍﻟﻁﺒﻴﻌﻰ ﻭﺘﻜﺎﻟﻴﻑ ﺘﺴﺨﻴﻥ ﺍﻟﺴﺎﺌل ﻭﺃﻴﻀـﺎ ﺇﺭﺘﻔـﺎﻉ‬ ‫ﹰ‬ ‫ﺍﻟﻘﺩﺭﺓ ﺍﻟﻼﺯﻤﺔ ﻟﻀﺦ ﺍﻟﺴﺎﺌل ﺍﻟﻠﺯﺝ.‬ ‫ﺘﺼﻤﻴﻡ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ :‬ ‫ﻟﺘﺼﻤﻴﻡ ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﻴﺠﺏ ﺃﻭﻻ ﺘﺤﺩﻴﺩ ﺍﻟﺒﻴﺎﻨﺎﺕ ﺍﻵﺘﻴﺔ :‬ ‫ﹰ‬ ‫١- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﻤﺩﻯ ﻟﻠﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﺃﻯ ﺍﻟﻜﻤﻴـﺔ‬ ‫ﺍﻟﻤﺒﺩﺌﻴ ـﺔ ﻭﺍﻟﻘﺼ ـﻭﻯ ‪Initial And Ultimate‬‬ ‫ـ‬ ‫ـ‬ ‫‪Throughput‬‬ ‫٢- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﺍﻟﻀﻐﻁ ﺍﻵﻤﻥ ﺍﻟﺫﻯ ﻴﺘﺤﻤﻠﻪ ﻤﻌـﺩﻥ ﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﻭﻓﻲ ﺃﻏﻠﺏ ﺍﻷﺤﻴﺎﻥ ﻴﻜﻭﻥ ﻫﺫﺍ ﺍﻟﻀﻐﻁ ﻓـﻲ‬ ‫ﺤﺩﻭﺩ ٠٧ﻜﺠﻡ/ﺴﻡ٢.‬ ‫- ٣٥ -‬
  • 55. ‫٣- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﺍﻟﻀﻐﻁ ﻋﻨﺩ ﻨﻬﺎﻴـﺔ ﺨـﻁ ﺍﻷﻨﺎﺒﻴـﺏ ﺃﻯ‬ ‫ﺍﻟﻀﻐﻁ ﻋﻨﺩ ﻤﺤﻁﺔ ﺍﻹﺴﺘﻼﻡ ﻭﻫﻭ ﻴﻜﻭﻥ ﻓﻲ ﺤـﺩﻭﺩ‬ ‫٢ﻜﺠﻡ/ﺴﻡ٢.‬ ‫٤- ﻴﺘﻡ ﺘﺤﺩﻴﺩ ﻁﻭل ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺃﻯ ﺍﻟﻤﺴﺎﻓﺔ ﺒﻴﻥ ﻤﺤﻁﺔ‬ ‫ﺍﻟﺘﺩﻓﻴﻊ ﻭﻤﺤﻁﺔ ﺍﻹﺴﺘﻼﻡ.‬ ‫ﺨﻁﻭﺍﺕ ﺍﻟﺘﺼﻤﻴﻡ :‬ ‫١- ﻴﺘﻡ ﺤﺴﺎﺏ ﻤﺩﻯ ﻷﻗﻁﺎﺭ ﺍﻟﺨﻁﻭﻁ ﺍﻟﺘـﻲ ﺘﺴـﺘﻭﻋﺏ‬ ‫ﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬـﺎ ﺃﻯ ﺍﻟﺤـﺩ ﺍﻷﺩﻨـﻰ‬ ‫ﻭﺍﻷﻗﺼﻰ ﻷﻗﻁﺎﺭ ﺍﻟﺨﻁﻭﻁ، ﻭﺒﻤﺎ ﺃﻥ ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﻨﻘﻭﻟﺔ‬ ‫ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺘﺴﺎﻭﻯ 2‪Q = 1.842V Di‬‬ ‫ﻓﻴﻜﻭﻥ ﺍﻟﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺒﺎﻟﺒﻭﺼﺔ ﻴﺴﺎﻭﻯ‬ ‫= ‪ Di‬ﺤﻴﺙ ﺃﻥ ‪ V‬ﻫﻰ ﺴﺭﻋﺔ ﺍﻟﺴـﺎﺌل‬ ‫‪Q‬‬ ‫‪1.824V‬‬ ‫ﺩﺍﺨل ﺍﻟﺨﻁ ﺒﺎﻟﻤﺘﺭ/ﺜﺎﻨﻴﺔ، ﻭﻹﻴﺠﺎﺩ ﺍﻟﺤﺩ ﺍﻷﺩﻨﻰ ﻟﻠﻘﻁﺭ‬ ‫ﺍﻟ ـﺩﺍﺨﻠﻰ ﻨﻀ ـﻊ ﺍﻟﻜﻤﻴ ـﺔ ﺍﻟﻘﺼ ـﻭﻯ ‪Ultimate‬‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫ـ‬ ‫‪ Throughput‬ﻭﺃﻴﻀﺎ ‪ V=٣mt/sec‬ﻓﻲ ﺍﻟﻤﻌﺎﺩﻟﺔ‬ ‫ﹰ‬ ‫ﺍﻟﺴﺎﺒﻘﺔ‬ ‫‪Qult‬‬ ‫= ‪Minimum Di‬‬ ‫3 × 428.1‬ ‫- ٤٥ -‬
  • 56. ‫ﻭﻜﺫﻟﻙ ﻹﻴﺠﺎﺩ ﺍﻟﺤﺩ ﺍﻷﻗﺼﻰ ﻟﻠﻘﻁﺭ ﺍﻟﺩﺍﺨﻠﻰ ﻨﻀﻊ ﺍﻟﻜﻤﻴـﺔ‬ ‫ـﺎ ٥,١=‪V‬‬ ‫ـﻭﻯ ‪ Ultimate Throughput‬ﻭﺃﻴﻀـ ﹰ‬ ‫ﺍﻟﻘﺼـ‬ ‫‪ mt/sec‬ﻓﻲ ﺍﻟﻤﻌﺎﺩﻟﺔ ﺍﻟﺴﺎﺒﻘﺔ‬ ‫‪Qult‬‬ ‫= ‪Maximum Di‬‬ ‫5.1× 428.1‬ ‫٢- ﻴﺘﻡ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﺃﻯ ﺘﻘﺭﻴﺒﺎ ﻓﺎﻗـﺩ ﺍﻟﻀـﻐﻁ‬ ‫ﹰ‬ ‫ﺍﻟﻤﺭﺘﺒﻁ ﺒﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﻭﺫﻟﻙ ﻟﻤـﺩﻯ‬ ‫ﺍﻷﻗﻁﺎﺭ ﺍﻟﺘﻲ ﺘﻡ ﺇﺨﺘﻴﺎﺭﻫﺎ ﻓﻲ ﺍﻟﺨﻁﻭﺓ ﺍﻟﺴﺎﺒﻘﺔ ﻋـﻥ‬ ‫ﻁﺭﻴﻕ ﻤﻌﺎﺩﻟﺔ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜـﺎﻙ ﺁﺨـﺫﺍ ﻓـﻲ‬ ‫ﹰ‬ ‫ﺍﻹﻋﺘﺒﺎﺭ ﺍﻟﻤﻌﻁﻴﺎﺕ.‬ ‫- ٥٥ -‬
  • 57. ‫٣- ﻴﺘﻡ ﺘﺴﺠﻴل ﻨﺘﺎﺌﺞ ﺍﻟﺤﺴﺎﺒﺎﺕ ﻓﻲ ﺠﺩﻭل ﻜﺎﻵﺘﻲ :‬ ‫ﺭﺃﺱ‬ ‫ﺍﻟﻤﺎل‬ ‫ﻓﺎﻗﺩ‬ ‫ﺃﻗل‬ ‫ﺘﻜﺎﻟﻴﻑ‬ ‫ﺍﻟﻜﻤﻴﺔ‬ ‫ﺍﻟﻼﺯﻡ‬ ‫ﺘﻜﺎﻟﻴﻑ‬ ‫ﺇﺠﻬﺎﺩ ﺍﻟﻀﻐﻁ‬ ‫ﺇﻨﺸﺎﺀ‬ ‫ﺍﻟﻤﻨﻘﻭﻟﺔ‬ ‫ﺍﻟﻘﻁﺭ‬ ‫ﻹﻨﺸﺎﺀ‬ ‫ﺇﻨﺸﺎﺀ‬ ‫ﺨﻀﻭﻉ ﻋﻠﻰ‬ ‫ﻤﺤﻁﺎﺕ‬ ‫ﺒﺎﻟﻤﺘﺭ‬ ‫ﺴﻤﻙ ﺍﻟﺩﺍﺨﻠﻰ‬ ‫ﺨﻁ‬ ‫ﺨﻁ‬ ‫ﻟﻤﻌﺩﻥ ﻁﻭل‬ ‫ﻗﻁﺭ ﺍﻟﺨﻁ‬ ‫ﺍﻟﻀﺦ‬ ‫ﺍﻟﻤﻜﻌﺏ‬ ‫ﺍﻟﺨﻁ ﻟﻠﺨﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ‬ ‫ﺍﻟﻤﻭﺍﺴ ﺍﻟﺨﻁ‬ ‫-١‪α(P‬‬ ‫ﻓﻲ‬ ‫‪Di‬‬ ‫ﻭﻤﺤﻁﺎ‬ ‫‪α Di‬‬ ‫ﻴﺭ ‪(P١- min‬‬ ‫)٢‪P‬‬ ‫ﺍﻟﺴﺎﻋﺔ‬ ‫ﺕ‬ ‫)٢‪P‬‬ ‫‪σy‬‬ ‫ﺍﻟﻀﺦ‬ ‫- ٦٥ -‬
  • 58. ‫ﻭﻴﻤﻜﻥ ﺍﻟﺘﺤﻜﻡ ﻓﻲ ﺍﻟﻌﻭﺍﻤل ﺍﻟﻤﺘﻐﻴﺭﺓ ﻤﺜل ﻗﻁﺭ ﺍﻟﺨﻁ ﻭﻓﺎﻗﺩ‬ ‫ﺍﻟﻀﻐﻁ ﻋﻠﻰ ﻁﻭل ﺍﻟﺨﻁ ﺒﻬﺩﻑ ﺇﻴﺠﺎﺩ ﺃﻗل ﻗﻴﻤﺔ ﻤﻤﻜﻨﺔ ﻟـﺭﺃﺱ‬ ‫ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺨﺩﻡ ﻹﻨﺸﺎﺀ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﻭﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﻋﻠﻤـﺎ‬ ‫ﹰ‬ ‫ﺒﺄﻥ ﻤﻌﻅﻡ ﺭﺃﺱ ﺍﻟﻤﺎل ﺍﻟﻤﺴﺘﺨﺩﻡ ﻴﺴﺘﻬﻠﻙ ﻓـﻲ ﺇﻨﺸـﺎﺀ ﺨـﻁ‬ ‫ﺍﻷﻨﺎﺒﻴﺏ ﻨﻔﺴﻪ، ﻭﻗﺩ ﻴﺘﻀﺢ ﺃﻨﻪ ﻟﺘﺼﻤﻴﻡ ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺒﺄﻗل ﺭﺃﺱ‬ ‫ﻤﺎل ﻓﺈﻨﻪ ﻴﺠﺏ ﺇﺨﺘﻴﺎﺭ ﺍﻟﻤﻭﺍﺴﻴﺭ ﺫﺍﺕ ﺍﻷﻗﻁﺎﺭ ﺍﻟﺼﻐﻴﺭﺓ ﻭﻓـﻲ‬ ‫ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻓﺈﻥ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﻗﺩ ﺘﻜﻭﻥ ﻤﺘﻘﺎﺭﺒﺔ ﻭﻫﺫﺍ ﻴﺤﻘـﻕ‬ ‫ﺃﻋﻠﻰ ﺇﺴﺘﻔﺎﺩﺓ ﻤﻥ ﺍﻹﺴﺘﺜﻤﺎﺭﺍﺕ ﺍﻟﻤﺩﻓﻭﻋﺔ ﻓﻲ ﺃﻯ ﻭﻗـﺕ ﻓـﻭﺭ‬ ‫ﻀﺦ ﻫﺫﻩ ﺍﻹﺴﺘﺜﻤﺎﺭﺍﺕ ﻭﻴﺠﺏ ﺃﻥ ﻨﺘﻼﻗﻰ ﻀﺦ ﺃﻯ ﺇﺴﺘﺜﻤﺎﺭﺍﺕ‬ ‫ﻏﻴﺭ ﻀﺭﻭﺭﻴﺔ ﻤﺒﻜﺭﺍ ﺤﻴﺙ ﺃﻨﻪ ﻴﺘﺴﺒﺏ ﻓﻲ ﻋﺩﻡ ﺍﻹﺴﺘﻔﺎﺩﺓ ﻤﻥ‬ ‫ﹰ‬ ‫ﻫﺫﻩ ﺍﻹﺴﺘﺜﻤﺎﺭﺍﺕ ﻋﺩﺓ ﺴﻨﻭﺍﺕ.‬ ‫ﻤﺜﺎل ﻋﻠﻰ ﺘﺼﻤﻴﻡ ﺨﻁ ﺃﻨﺎﺒﻴﺏ :‬ ‫ﻤﻁﻠﻭﺏ ﻨﻘل ﺴﺎﺌل ﻟﻤﺴﺎﻓﺔ ﻗﺩﺭﻫﺎ ٠٩١ﻜﻴﻠﻭ ﻤﺘـﺭ ﻭﺒﻜﻤﻴـﺔ‬ ‫ﻗﺩﺭﻫﺎ ٢ ﻤﻠﻴﻭﻥ ﻁﻥ ﺴﻨﻭﻴﺎ ﺴﻭﻑ ﺘﺯﺩﺍﺩ ﻤﺴﺘﻘﺒﻼ ﺇﻟﻰ ٥ ﻤﻠﻴﻭﻥ‬ ‫ﹰ‬ ‫ﹰ‬ ‫ﻁﻥ ﺴﻨﻭﻴﺎ.‬ ‫ﹰ‬ ‫- ٧٥ -‬
  • 59. ‫ﺍﻟﺤل : ﻨﺤﺴﺏ ﺃﻭﻻ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﺒﺩﺌﻴﺔ ﻭﺍﻟﻘﺼﻭﻯ ﺍﻟﻤﻁﻠـﻭﺏ‬ ‫ﹰ‬ ‫ﻨﻘﻠﻬﺎ ﺒﺎﻟﻤﺘﺭ ﺍﻟﻤﻜﻌﺏ ﻓﻲ ﺍﻟﺴﺎﻋﺔ ﺒﻔﺭﺽ ﺃﻥ ﺍﻟﺴﺎﺌل ﺍﻟﻤﻁﻠـﻭﺏ‬ ‫6 01 × 2‬ ‫‪Q Initial‬‬ ‫= ‪= 2 × 10 ton / year‬‬ ‫6‬ ‫ﻨﻘﻠﻪ ﻫﻭ ﺍﻟﻤﺎﺀ.‬ ‫‪7200sp.gr‬‬ ‫‪Qinitial= ٢٧٧,٧٧ mt٣/hr‬‬ ‫6 01 × 5‬ ‫= ‪QUltimate = 5 × 10 6 ton / year‬‬ ‫‪= 694.44mt 3 / hr‬‬ ‫‪7200sp.gr‬‬ ‫ﺜﻡ ﻨﺤﺴﺏ ﺍﻟﺤﺩ ﺍﻷﺩﻨﻰ ﻭﺍﻷﻗﺼﻰ ﻷﻗﻁﺎﺭ ﺍﻟﺨﻁﻭﻁ ﺍﻟﺘـﻲ‬ ‫ﺘﺴﺘﻭﻋﺏ ﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ‬ ‫44. 496‬ ‫= ‪min .D i‬‬ ‫‪= 11 .265 inch‬‬ ‫274. 5‬ ‫44. 496‬ ‫= ‪max .D i‬‬ ‫‪= 15 .93 inch‬‬ ‫637. 2‬ ‫ﻭﻤﻤﺎ ﺴﺒﻕ ﻨﺴﺘﻨﺘﺞ ﺃﻥ ﺃﺩﻨﻰ ﻭﺃﻗﺼﻰ ﻗﻁﺭ ﻟﻨﻘل ﻫﺫﺍ ﺍﻟﻤـﺩﻯ‬ ‫ﻤﻥ ﺍﻟﻜﻤﻴﺎﺕ ﻴﺴﺎﻭﻯ٢١، ٦١ ﺒﻭﺼﺔ ﻋﻠﻰ ﺍﻟﺘـﻭﺍﻟﻰ، ﻭﺒـﺫﻟﻙ‬ ‫ﻴﻤﻜﻥ ﺇﺨﺘﻴﺎﺭ ٣ ﺃﻗﻁﺎﺭ ﻟﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ ﺍﻟﻼﺯﻡ ﻟﻨﻘل ﻫﺫﺍ ﺍﻟﻤـﺩﻯ‬ ‫ﻤﻥ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﻭﻫﺫﻩ ﺍﻷﻗﻁﺎﺭ ﻫﻰ ٢١ ﺒﻭﺼـﺔ،‬ ‫٤١ ﺒﻭﺼﺔ ﻭ٦١ ﺒﻭﺼﺔ.‬ ‫- ٨٥ -‬
  • 60. ‫: ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺒﻘﻁﺭ ٢١ ﺒﻭﺼﺔ ﺒﻤﺤﻁﺔ ﻀﺦ ﻭﺍﺤﺩﺓ‬ ‫ﺃﻭﻻ‬ ‫ﹰ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ ﻭﻴـﺘﻡ ﺇﻀـﺎﻓﺔ ﻤﺤﻁـﺔ ﻀـﺦ‬ ‫ﻤﺴﺎﻋﺩﺓ ﻓﻲ ﻤﻨﺘﺼﻑ ﺍﻟﻁﻭل ﺘﻘﺭﻴﺒﺎ ﻓﻴﻤﺎ ﺒﻌﺩ ﺜﻡ ﺒﻌـﺩ‬ ‫ﹰ‬ ‫ﺫﻟﻙ ﻴﺘﻡ ﺇﻀﺎﻓﺔ ﻋﺩﺩ ٢ ﻤﺤﻁﺔ ﻀﺦ ﻤﺴﺎﻋﺩﺓ ﻋﻠـﻰ‬ ‫ﻤﺴﺎﻓﺔ ﺭﺒﻊ ﻁﻭل ﺍﻟﺨﻁ ﺘﻘﺭﻴﺒﺎ ﻤﻥ ﺒﺩﺍﻴﺘـﻪ ﻭﻨﻬﺎﻴﺘـﻪ‬ ‫ﹰ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ‬ ‫ﻭﻓﻲ ﻫﺫﻩ ﺍﻟﺤﺎﻟﺔ ﻴﺘﻡ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﺃﻯ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ‬ ‫ﺍﻟﻤﺭﺘﺒﻁ ﺒﻤﺩﻯ ﺍﻟﻜﻤﻴﺎﺕ ﺍﻟﻤﻁﻠﻭﺏ ﻨﻘﻠﻬﺎ ﻜﺎﻵﺘﻲ :‬ ‫ﻟﻠﺨﻁ ٢١ ﺒﻭﺼﺔ ‪ Standard weight‬ﺴـﻤﻙ ﺍﻟﺨـﻁ =‬ ‫٥٧٣,٠ ﺒﻭﺼﺔ‬ ‫‪Di=١٢,٧٥ – ٢ (٠,٣٧٥) = ١٢// and L = ١٩٠ kmt‬‬ ‫١( ﻟﻠﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ ‪QI=٢٧٧,٧٧ m٣/hr‬‬ ‫77.772‬ ‫=‪V‬‬ ‫‪= 1.057mt / sec‬‬ ‫2 )21(428.1‬ ‫ﺒﺘﻁﺒﻴﻕ ﻤﻌﺎﺩﻟﺔ ﺤﺴﺎﺏ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻟﻠﺴﺭﻴﺎﻥ ﺍﻟﻤﻀﻁﺭﺏ‬ ‫ﺩﺍﺨل ﺍﻷﻨﺎﺒﻴﺏ‬ ‫57.1 77.772)091( 52.01‬ ‫× 5245.71 = ‪h f‬‬ ‫‪= 471.2mt‬‬ ‫57.4 21‬ ‫- ٩٥ -‬
  • 61. ‫ﻭﺒﺫﻟﻙ ﻴﻜﻭﻥ ﻓﺎﻗﺩ ﺍﻹﺤﺘﻜﺎﻙ ﻓﻲ ﺼـﻭﺭﺓ ﻀـﻐﻁ ﻴﺴـﺎﻭﻯ‬ ‫‪sp.gr‬‬ ‫× 2.174‬ ‫2 ‪= 47.12kg / cm‬‬ ‫01‬ ‫ﻭﻴﺘﻀﺢ ﻤﻤﺎ ﺴﺒﻕ ﺃﻨﻪ ﻴﻜﻔﻲ ﺘﺭﻜﻴﺏ ﻤﺤﻁﺔ ﻀﺦ ﻭﺍﺤﺩﺓ ﻓﻲ‬ ‫ﺒﺩﺍﻴﺔ ﺍﻟﺨﻁ ﻭﺫﻟﻙ ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ.‬ ‫٢( ﻟﻠﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ ‪Qu = ٦٩٤,٤٤ m٣/hr‬‬ ‫ﻨﻜﺭﺭ ﻨﻔﺱ ﺍﻟﺨﻁﻭﺍﺕ ﺍﻟﺴﺎﺒﻘﺔ:‬ ‫‪V = ٢,٦٤ mt/sec‬‬ ‫٢‪hf = ٢٣٤,٢ kg/cm‬‬ ‫ﻭﺤﻴﺙ ﺃﻥ ﻓﺎﻗﺩ ﺍﻟﻀﻐﻁ ﻴﺘﻌﺩﻯ ﺍﻟﻀﻐﻁ ﺍﻵﻤﻥ ﺍﻟﺫﻯ ﻴﺘﺤﻤﻠﻪ‬ ‫ﻤﻌﺩﻥ ﺨﻁ ﺍﻷﻨﺎﺒﻴﺏ، ﻟﺫﻟﻙ ﻴﻜﻭﻥ ﻋﺩﺩ ﻤﺤﻁﺎﺕ ﺍﻟﻀﺦ ﺍﻟﻤﻁﻠﻭﺒﺔ‬ ‫ﻭﻤﻤـﺎ ﺴـﺒﻕ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ ﻴﺴﺎﻭﻯ 643.3 =‬ ‫2.432‬ ‫07‬ ‫ﻴﺘﻀﺢ ﺃﻨﻪ ﻴﺠﺏ ﺘﺭﻜﻴﺏ ٤ ﻤﺤﻁﺎﺕ ﻀﺦ ﻋﻠﻰ ﻁـﻭل ﺍﻟﺨـﻁ‬ ‫ﻭﺫﻟﻙ ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ.‬ ‫: ﺨﻁ ﺃﻨﺎﺒﻴﺏ ﺒﻘﻁﺭ ٤١ ﺒﻭﺼﺔ ﺒﻤﺤﻁﺔ ﻀﺦ ﻭﺍﺤﺩﺓ‬ ‫ﺜﺎﻨﻴﺎ‬ ‫ﹰ‬ ‫ﻟﻨﻘل ﺍﻟﻜﻤﻴﺔ ﺍﻟﻤﺒﺩﺌﻴﺔ ﺜﻡ ﺒﻌﺩ ﺫﻟﻙ ﻴﺘﻡ ﺇﻀﺎﻓﺔ ﻤﺤﻁـﺔ‬ ‫ﻀﺦ ﻤﺴﺎﻋﺩﺓ ﻓﻲ ﻤﻨﺘﺼﻑ ﻁﻭل ﺍﻟﺨﻁ ﺘﻘﺭﻴﺒﺎ ﻟﻨﻘـل‬ ‫ﹰ‬ ‫ﺍﻟﻜﻤﻴﺔ ﺍﻟﻘﺼﻭﻯ.‬ ‫- ٠٦ -‬