Industrial Carbon and Graphite Materials. Группа авторов

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Also the content of the key component benzopyrene (c. 25 mg/kg) is not critical. Green coke is therefore classified as a nontoxic substance [3].

      No classification and labeling regarding toxicity, carcinogenicity, flammability, and environmental effects is required. Contents of Ni, V, Na, Ca, and Fe originating from the crude oil residues used as feed are accumulated in green coke. These levels can rises up to approximately 10–500 mg/kg. Small amounts of metals and anions are introduced with the cutting water, which makes up to 5–15% of green coke (cutting water content: Na, Ca, Cl, images). Other heavy metals (Hg, Cd, Pb, Cr, Cu, Co, As) are not traceable (level <1 mg/kg). Hydrocarbons and metals in green coke cannot be elutriated with water (S4 eluate method). No classification and labeling regarding toxicity, carcinogenicity, flammability, and environmental effects is required.

      The following classification is employed for the combustion and explosion behavior (measurement of Deutsche Montan Technologie [DTM], mining test circuit, Dortmund):

Combustion behavior BZ 3 (local combustion or glowing without spreading)
Glow temperature 300 °C
Ignition temperature 700 °C
Dust explosiveness Contents >60 g/m3 and with ignition source of >10 000 J

      Green coke is normally stored in open piles with sidewalls as protection against the wind. In order to reduce the dust discharge, green coke piles are sprinkled with water.

      The potential dust emission is visibly improved by means of dosing antidust additives (polyacrylate types or extract of orange peel) to the sprinkling water.

      The general explosive boundary value at work of 6 mg/m3 for fine dust concentrations is to be complied with.

      6.1.2.6.2 Calcined Petroleum Coke

      All hydrocarbons in green coke are eliminated by calcination. The remaining hydrogen content is <0.1%. Therefore, no polycyclic aromatics are traceable. The content of S, N, and metals is virtually unchanged. With water, only part of the salt content of the cutting water can be elutriated. No classification and labeling is required.

      Due to the dryness of the calcinate, irritation of eyes and throat by the dust is possible. The general boundary value at work (maximum 6 mg/m3 for fine dust concentration) is to be complied with.

      Calcined coke is usually stored in closed silos or bins to keep the material dry. To reduce dust formation, the calcinate is sucked off during transport and loading and the dust held back by filter stations. Sprinkling the calcinate with residue parts of 0.2–0.4 wt% (old process) or an aqueous emulsion of dust binder prevents environmental problems from dust. The dust forming factor (“R+D‐Carbon” method) must be <0.02 wt%. The combustion and explosive behavior of calcined coke presents no problem:

Combustion behavior BZ1 (no combustion)
Glow temperature No glowing up to 450 °C
Ignition temperature No ignition up to 850 °C
Dust explosive No

      References

      1 1 De Biase, R. and Elliott, J.D. (1982). Coking process reflects trends, innovations. Oil Gas J. 80 (16): 81–88.

      2 2 Montell, C.L. (1968). Carbon Graphite Handbook. New York, NY: Interscience Publishers.

      3 3 CONCAWE (2007). Reports nos. 93/105 and 95/95 ‐” The Classification and Labelling of Petroleum (CLP) substances according to the EU dangerous substances directive,” Brussels, July 1995 ‐ Second ATP (Adaption to Technical Process) to the CLP regulation Commission Regulation EU, No. 286, 2011 ‐ CONCAWE recommendations, August 2001; CLP according to the EU dangerrous substances directive ‐ API (American Petroleum Institut) – Report:”Petroleum Coke Category Analysis and Hazard Charakterization”.

      4 4 Sojka, M. (2011). Orinoco Oil Belt, PH 240, Stanford University.

      5 5 Dunbar, R.B. (2012). Strategy West Inc., Canada’Oil Sands, Internet.

      6 6 Chandelle, J.M. (2005). CEM Rev. 220: 1–22.

      7 7 Jacobs Consultancy Offices (2011). 10th Annual Petcoke Conference, San Diego, CA.

      8 8 Statistik der Kohlewirtschaft, Essen (1995).

      9 9 EIA (2013). U.S. Energy Information Administration, March 2013.

      10 10 Billege, I. (2009). 700 refineries supply oil products to the world. NAFTA 60 (7–8): 401–403.

      11 11 Predel, H. (1990). Delayed coking. Erdöl Kohle Erdgas Petrochem. 43: 145–146.

      12 12 Conoco Inc. (1984). Method of reducing coke yield. US 44,55,219 (H.R. Janssen, G.L. Poffenbarger).

      13 13 Conoco Inc. (1985). Process for improving product yields from delayed coking. US 45,18,487 (H.G. Graf, H.R. Janssen).

      14 14 Elliott, J.D. (2008). ImpaCT of feed properties and operating parameters on delayed coker petcoke quality. Presented at ERTC Conference

      15 15 Predel, H. (1992). Theoretical and practical methods for coke yield calculations and optimisation. In: Light Metals 1992, 601–609. San Diego, CA: TMS.

      16 16 Liebermann, N. (1985). Troubleshooting in Process Operations, 16–26. Metairie, LA: Pen Well Publishing Comp.

      17 17 Predel, H. (1992). New developments in delayed coker operations. Carbon Conference (22–26 June 1992). Essen.

      18 18 Stefani, A. (1996). Debottleneck delayed cokers for greater profitability. Hydrocarbon Process. 6: 99–103.

      19 19 Mobil Oil Corporation (1978). Conversion of solid wastes to fuel coke and gasoline. US 4,118,281 (T.‐Y. Yan).

      20 20 Elliott, J.D. and Klick, R. (1994). Trends in delayed coker design. Hydrocarbon Technol. Int. J. 71 (1) Summer): 17–23.

      21 21 Elliott, J.D. (1993). Latest coker designs increase liquid yields, reduce emissions. Oil Gas J. 91: 14–20.

      22 22 Elliott, J.D. (1992). Maximize distillate liquid products. Hydrocarbon Process. 71 (1): 79–84.

      23 23 NPRA (National Petroleum Refiners Association) (1994). Refiners exchange experiences on FCC problems, coking operations. Oil Gas J. 92: 110–115.

      24 24 Parrish, M.R., Hammond, D.G., and Citarella, V.A. (1996). Fluid coking: a continuous, flexible and reliable conversion process. Hydrocarbon Technol. Int. J. Spring: 25–31.

      25 25 Diff. autors (1996). Refining 1996, Hydrocarbon Process. 75 Special Edition,

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