INTEGRATED HEAVY OIL PYROLYSIS PROCESS

Abstract: Process for the production of olefins from heavy oils. Heavy feed is first cracked at high temperatures and low residence times then separated into three fractions of light, medium and heavy oils. The light and medium fractions are cracked in parallel streams. These cracked streams are combined and further cracked to produce olefins. Apparatus for performing the process is also disclosed.

Description: INTEGRATED HEAVY OIL PYROLYSIS PROCESS BACKGROUND OF THE INVENTION 1. FIELD OF THE INVENTION This invention relates to the production of olefins from hydrocarbon feedstock. More particularly, the invention relates to the production of olefins from heavy hydrocarbon feedstocks. Most specifically, the 10 invention relates to the production σf olefins from heavy hydrocarbon feedstocks by a combination of pre- treatment of the heavy hydrocarbon feedstock in which a liquid fuel product first is produced as a method of preferentially rejecting carbon to enhance the production **-"-- ■' of olefins ultimately converted from the hydrocarbon feedstock. 2. DESCRIPTION OF THE PRIOR ART The petrochemical industry has . long used 20 naturally forming hydrocarbon feedstocks for the pro¬ duction of valuable olefinic materials, such as ethylene and propylene. Ideally, commercial operations have been carried out using normally gaseous hydrocarbons such as ethane and propane as the feedstock. As the lighter *" hydrocarbons have been consumed and-the availability of the lighter hydrocarbons has decreased, the industry has been required to crack heavier hydrocarbons. Hydrocarbons such as naphtha and atmospheric gas oil (AGO) which have higher boiling points than the gaseous hydrocarbons have 30 been used commercially. Processes are under development for the use of still heavier, less expensive feeds such as vacuum gas oil (VGO) or residues from atmospheric distillation columns, commonly called atmospheric tower • bottoms (ATB) . However, none of these processes using 35 feeds with normal boiling points above 650°F. have achieved broad commercial success. The major impediment -to the use of feeds heavier than AGO has been the need to increase the quantity of dilution steam necessary to inhibit coke formation. A further problem results from the need to dispose of increasing yields of the poor quality fuel oil by-product of the olefin producing process when the heavy hydrocarbons are used as feedstock. A typical process for the production of olefins 10 from naturally forming hydrocarbon feedstocks is the thermal cracking process. Illustratively, process fired heaters are used to provide the requisite heat for the reaction. The • *- > feedstock flows through a plurality of coils within the fired heater, the coils being arranged in a manner that maximizes the heat transfer to the hydrocarbon flowing through the coils. . In conventional coil pyrolysis, dilution steam is used to inhibit coke formation in the 0 cracking coil. A further benefit of high steam dilution is the inhibition of the coke deposition in the exchangers used to rapidly quench the cracking reaction. An illustration of the conventional proct ss is seen in United States Letters Patent No. 3,48" ,121 (Hallee) . 5 More recently, the thermal cracking process has been conducted in apparatus which allow the hydrocarbon feed¬ stock to pass through a reactor in the presence of steam while providing for heated solids as the heat carrier. 0 The use of steam, in the hydrocarbon stream requires larger furnace capacity and equipment than would be necessary for the hydrocarbon without steam. Further, when steam is used, energy and equipment must be provided to generate and superheat the steam. 5 In the production of olefins from hydrocarbon feedstocks the generation of coke has been a problem regardless of the process used. Typically, the cracking reaction will cause production of heavy tar and coke materials which foul the equipment and provide no useful function. The problem is particularly acute in the coil cracking environment where the furnaces must be taken from service to remove the coke and tar from the coils to enable the process to continue efficiently. The use of heavier hydrocarbon feedstocks, such as residual oils with the attendant high asphaltene and coke precursor content, intensifies and magnifies the problem of coke formation * and the associated eσuipment fouling problems in coil processes. To compensate, the steam rate must be increased, which would increase the specific energy, i.e., energy consumed per unit of ethylene/olefins produced. When using VGO as a feedstock, for example, the specific energy can be 50% above that needed for a light hydrocarbon such as naphtha. Similarly, the amount of ethylene that can be produced from a given size pyrolysis coil when using VGO is often less than half that obtained from naphtha. Another problem attendant to the use of higher boiling range feedstocks is the increased production of poorer quality fuel oil. The cracking severity needed to produce olefins from these heavy feeds is much higher than that used for conventional thermal crackers designed to produce gasoline and fuel oil. This high severity results in the simultaneous production of olefins and poor quality fuel oil rich in asphaltenes and free carbon. All of the above problems have detracted from the use of high boiling, less expensive feeds for pro¬ ducing olefins. A variety of attempts have been made to pre- treat the heavy hydrocarbon feedstock to render it suitable " for thermal cracking. Hydro-treating of the feedstock is one effort. Another effort, is the vapor¬ ization of the feedstock with large quantities of steam to create a very low system .partial pressure (Gartside, United States Letters Patent No. 4,264,432). Others have proposed solvent extraction pretreatment of the hydrocarbon to remove the asphaltene and coke precursors. Another attempt is the thermal pretreatment of resids to yield a heavy hydrocarbon, then catalytically hydrotreating a portion of the heavy hydrocarbon feedstock -before the steam cracking step (United States Letters Patent No. 4,065,379, Soonawala, et al.) and similarly, the pre-treatment of hydrocarbon feedstock by initial catalytic cracking to produce a naphtha or naphtha-like feed for ultimate thermal cracking (United States Letters Patent No. 3,862,898, Boyd, et al.). These processes all improve the cracking of heavy hydrocarbon, however, in most instances the process suffers from either the expense of large steam dilution equipment or the unsatisfactory reduction of tar and coke accumulation in the process equipment. SUMMARY OF THE INVENTION It is an object of the present invention to provide a process in which heavy hydrocarbon can be cracked to produce valuable olefins with a minimum of asphaltene and coke generation. .It is another object of the present invention to provide a process in which olefins are produced from heavy hydrocarbon feedstocks with an associated liquid fuel generation step in which the asphaltene precursors . are concentrated in the liquid product. It is " a further object of the present invention to provide a process in which heavy hydrocarbons can be cracked to olefins with a minimal amount of dilution steam. It is a still further object of the present invention to provide a means for integrating a feed pre¬ treatment step with conventional or developmental cracking technologies without incurring additional capital or utility generation expenditures. To this end, the process proceeds in which the heavy hydrocarbon feedstock is initially pre-treated to temperature levels below that at which significant conversion of the feed to olefins will take place. For example, a temperature of about 750 β F. is the pre-heat temperature for vacuum gas oils. The pre-heated feed is then heated in a pre-pyrolysis cracker operated at high pressure, i.e., above 300 psig at the outlet and temperature levels below 1200°F. Thereafter, the hydrocarbon stream is subjected to considerable pressure reduction; i.e., to about 100 psig to cause essentially complete vaporization of all hydrocarbons boiling below about 1000 β F. at atmospheric pressure. Thus, separate liquid and vapor fractions are produced in which the heavy liquid fraction is comprised of high boiling polyaro atics produced in the prior process steps, 5 essentially from the coke precursors. The heavy liquid fraction is removed and taken as a fuel and the vapor fraction" is passed downstream for conversion to olefins. The lighter treated heavy hydrocarbon fraction 1 Q and the light overhead fraction are initially passed through a pre-cracker in which pentane conversion is maintained at lower levels, i.e., approximately 15 to 40 percent equivalent normal pentane conversion. Thereafter, the partially cracked heavy hydrocarbon is passed • j e downsteam for ultimate thermal cracking. Various conventional thermal cracking processes can be used to complete the olefin producing process, however, the pre-treated hydrocarbon is particularly 2 well suited for final cracking in a DUOCRACKING environ¬ ment. The basic DUOCRACKING procedure is accomplished by partially era? king a hea^y hydrocabon at a low temperature in the presence of a small amount of steam, i.e., less than 0.2 pound of steam per pound of hydro- 5 carbon and thereafter, joining the partially cracked heavy hydrocarbon with a stream of completely cracked lighter hydrocarbon to effect complete cracking of the partially cracked heavy hydrocarbon. United States Letters Patent Application Serial No. 431,588 illustrates the DUOCRACKING process. DESCRIPTION OF THE DRAWING The drawing is an elevational schematic of the process of the present invention shown in a furnace c system environment. DESCRIPTION OF THE PREFERRED EMBODIMENT As has been previously indicated, the process of the present invention is directed to providing a means e for treating heavy hydrocabon feedstocks for the purpose of producing olefins. The heavy hydrocarbons contemplated as the feedstock have an average boiling point above 1000°F- or an average molecular weight above 400. These feedstocks include the high boiling distillate gas • j oils, atmospheric gas oils, vacuum gas oils, atmospheric tower bottoms and.other residual feedstocks. However, it should be noted that the process has general application for cracking hydrocarbons to produce olefins and in particular, in applications in which steam dilution 15 is used to suppress or reduce the formation of asphaltene and coke from the polyaromatics and other coke precursors found in naturally occuring hydrocarbon feedstocks. As best seen in the drawing, the process of 20 the present invention can be performed in an integrated thermal cracking system incorporating a pre-pyrol sis cracker 16, a primary separator 8, a pyrolysis furnace 4, a DUOCRACKER section 14, and a quench exchanger 20. The pyrolysis furnace 4 includes a convection section 6, 25 a pre-cracker 10 for cracking heavy hydrocarbons, and a radiant section 12 for cracking light hydrocarbons. The quench exchanger 20 can be a conventional pyrolysis quench apparatus such as a USX heat exchanger shown in detail in United States Letters Patent No. 3,583,476 30 (Woebcke, et al.). A line 18 is provided for the heavy hydrocarbon feed and a line 24 for a light hydrocarbon feed is also provided. The heavy hydrocarbon line 18 is arranged to -e pass through a heat exchanger 52 located in the wash section of the primary separator 8. Similarly, the light hydrocarbon line 24 is arranged to pass through a coil 26 in the convection section 6 of the pyrolysis furnace 4. A steam line 70 is arranged to deliver steam to the light hydrocarbon feed line 24. A line 28 is provided to deliver the preheated heavy hydrocarbon to the pre-pyrolysis cracker 16 and a line 30 is provided to deliver the pre-pyrolysis cracked feedstock from the pre-pyrolysis cracker 16 to the primary separator 8. A steam line 50 is arranged to deliver steam to the - pre-pyrolysis cracked feedstock in line 30 if desired. The primary separator 8 is provided with an effluent line 34 for the lighter treated heavy hydrocarbon feedstock to be passed downstream for further processing to olefins. The primary separator 8 is provided with an overhead line 32 for the lighter overhead fraction, to be provided as feed for the light hydrocarbon cracking furnace through line 24, if desired or as feed to the lighter treated heavy hydrocarbon line 34 through line 54. Line 60 is arranged to deliver steam to the lighter treated heavy hydrocarbon feed line 34. The primary separator 8 is further provided with a line 56 from which the heavy liquid material is taken in the form of a fuel oil. Coils 36 are provided in the convection section 6 of the pyrolysis furnace 4 to further heat the lighter treated heavy hydrocarbon feedstock and optionally the light overhead fraction from the primary separator 8 and a radiant coil 38 is provided in the pre-cracker 10 for partially cracking the lighter treated heavy hydrocarbon feedstock. The pre-cracker 10 is also provided with con¬ ventional burners shown illustratively as 40. Similarly, the light hydrocarbon cracking section 12 is a radiant section provided with a coil 42 and conventional radiant burners 44. An effluent discharge line 54 is provided in which the partially cracked heavy hydrocarbon stream and the cracked light hydrocarbon stream combine prior to being fed to the single coil 46 in the DUOCRACKER 14. Again, conventional radiant burners 48 are provided in the DUOCRACKER section 14. In essence, the process of the present invention is conducted by delivering a heavy hydrocarbon feedstock through line 18 to the heat exchanger 52 wherein the temperature of the heavy hydrocarbon is elevated to about 750°F. Optionally, steam is delivered through a steam line 80 to the heavy hydrocarbon feedstock in line 18. The heated hydrocarbon is delivered to the pre- pyrolysis cracker 16 through line 28 wherein a pressure in the range of 150 psig to 400 psig, preferably above 200 psig and most preferably above 300 psig is maintained at the outlet. A residence time of 0.5 to 3 minutes for the hydrocarbon in the pre-pyrolysis cracker 16 is required. The outlet temperature of the pre-pyrolysis cracker 16 is below 1200°F., preferably above 950 β F., i.e., 950 β F to 990°F. The pre-pyrolysis cracked hydrocarbon feedstock is discharged through line 30 where it is subjected to considerable pressure reduction by conventional means then fed to the primary separator 8. Practice has shown that a pressure reduction of the pre-pyrolysis cracked feedstock stream to approximately 100 psig prior to being fed to the primary separator 8 is desirable. The primary separator 8 is a conventional device such as a cyclone or a fractionation column. The separation of the pre-pyrolysis cracked feedstock in the primary separator 8 occurs at about 100 psig. The primary separator 8 is provided with reflux means shown as line 66, which recycles a liquid cut through the heat exchanger 52, and back to the primary separator 8. The reflux stream is at a temperature of about 800 β F. and provides a wash for the primary separator 8 to insure a j.0 light overhead fraction with a minimun of entrained polyaromatics. The pre-pyrolysis cracked feedstock is separated into several fractions in the primary separator 8; i.e., 15 a heavy fuel oil fraction, a lighter treated heavy hydrocarbon fraction and a light overhead fraction each of which exits the primary separator 8 at about 100 psig. 0 The heavy fuel oil fraction leaving the primary separator 8 through line 56 is rapidly quenched to a temperature below 900 β F, preferably below 850°F. The heavy fuel oil fraction is delivered to a stripper 82, where a heavy hydrocarbon fraction is separated from the '- heavy fuel oil fraction and recycled to the heavy hydrocarbon f edstock line 18 through the line 62. Typically, the heavy fuel oil fraction leaving the stripper 82, through line 58 will have an asphaltene 30 concentration of 1.5 to 5 weight percent, preferably less than 2 weight percent and a hydrogen concentration of 6.0 to 8.5 weight percent, preferably below 7.0%. The heavy fuel oil fraction will also contain at least 80 weight percent of the asphaltene precursors found in 35 the original feedstock, preferably over 90 weight precent. The heavy fuel oil fraction may be cut with recycled stock depending of the characteristics of the fuel desired. The lighter treated heavy hydrocarbon fraction taken through the line 34 from the side of the separator 8 is a hydrocarbon boiling in the range between 450 β F and fuel oil (I.B.P. 650°F to 950 β F) and will exit the primary separator 8 at a temperature of about 400 β F to 700°F. The light overhead fraction taken overhead through the line 32 from the primary separator 8 is a hydrocarbon fraction boiling at 450 β F and below (450 β F-) . and exits the primary separator 8 at about 700°F to 1000°F. Typically, the combined lighter treated heavy hydrocarbon fraction and the light overhead fraction exiting the primary separator 8 will have a hydrogen concentration of over 17 weight percent and an asphaltene precursor concentration below 100 ppm. The lighter treated heavy hydrocarbon fraction is particularly well suited for cracking in the heavy hydrocarbon cracking furnace side of the DUOCRACKING system. The light overhead fraction can be cracked either as a light hydrocarbon or as a heavy hydrocarbon and thus may be delivered to either the light hydrocarbon cracking furnace side of the DUOCRACKING system or to the heavy hydrocarbon cracking furnace side of the DUO¬ CRACKING system. It is contemplated that if DUOCRACKING is used to crack the treated heavy hydrocarbon of the process, the light overhead fraction taken through line 32 will be used as the feed for the light hydrocarbon cracking furnace side of the DUOCRACKING process if a naturally occurring light hydrocarbon is unavailable. ' Dilution steam is delivered at the rate of 0.2 pound of steam per pound of hydrocarbon feed or less through line 60 to line 68, through which the lighter treated heavy hydrocarbon fraction and optionally the light overhead fraction flow. The lighter treated heavy hydrocarbon fraction passes through the convection coil 36 and enters the pre-cracker 10 at about 840 β F. to 1110 β F., and usually 950 β F. The temperature in the pre-cracker 10 is in the range of 950°F to 1400 β F and the residence time is between 0.05 to 0.2 seconds, with the coil outlet temperature preferably in the range of 1350 β F. The conditions in the pre-cracker 10 are selected to maintain a cracking severity of below 15 to 40 percent equivalent normal pentane conversion. The effluent from the pre-cracker 10 is thus characterized as a partially cracked heavy hydrocarbon. The light hydrocarbon cracking furnace 12 will operate in a conventional manner with coil outlet temperatures as high as 1600°F., residence time of 0.1 to 0.5 seconds and 0.3 to 0.6 pound of dilution steam per pound of hydrocarbon. The light hydrocarbon feedstocks contemplated are ethane, propane, normal and iso-butane, propylene mixtures thereof, raffinates or naphthas. The conversion to olefins of the light hydrocarbons in the light hydrocarbon cracking furnace 12 is intended to be the maximum achievable and the effluent discharging from the furnace 12 is thus characterized as a completely cracked light hydrocarbon. The partially cracked heavy hydrocarbon effluent stream is delivered to the common line 54 at a temperature in the range of 1300°F. to 1400 β F., e.g. 1350°F., and the completely cracked light hydrocarbon effluent stream is delivered to the common line 54 at a temperature of about 1600 β F., wherein the streams are mixed. The composite stream passes downstream through a 5 DUOCRACKER coil 46 to effect a complete conversion of the partially cracked heavy hydrocarbon to levels required for commercial yields of olefins. The light hydrocarbon component of the mixed stream in line 54 provides over 80% of the heat to effect complete cracking of the in partially cracked heavy hydrocarbon component. Con- commitantly, the completely cracked light hydrocarbon effluent is quenched by the lower temperature partially cracked heavy hydrocarbon effluent in the common line 54. The composite effluent product exiting the DUOCRACKER T c coil ' 46 is passed downstream and quenched in conventional quenching equipment such as a USX (Double Tube Exchanger) 20. Thereafter, the effluent is separated into the various specific products. 20 One embodiment of the process of the present invention is shown in the drawing and illustrated by the following example (Table I - A) wherein the process conditions are given and the characteristics of the hydrocarbon product which'will be obtained are shown: 25 30 35 IrøS I - ES HiS OF H-OEES O? INBL-imi. Exaipte line # (see K_dng) E ylεne Yield Hgavy Lglit " IB 32 3 54 56 58 62 60 70 80 82 24 Wt% Rxr____Wt% E unte Ibtal A. VaαxiriGas Oil Pressure (psig) 0 MX) 100 - ICO 25 25 — _ — TθTperature (°F) 300 825 800 800 — — — Ilyatrϋattn Fteed (Bxtrls) ICO 36 54 — 13 ID 3 10 23 0 23 23 — — 23 Ibαral Boiling R_ nt (°F) 650/ 450- 450/ 95CM- 105CH- 850/ — sbβam l±OO 950 1050 B. λfecuuriGas Oil + Naj t_r_5i H^idrrxarbn Faal r-l Noαral Rmiling 23 10.8 30 10.8 21.6 I-bint (°F) 650/ 960- 960- 9501- 10501- 850/ steεm uω 1050 C NcnraL Boilijrg 24 24 — — 24 I-bint (°F) 650- 950 !D50- 850/ — stean 1050 D. ' Atm_qiτer_c Ibwer Bottαre +N_ξ_K_ha Hvτ5__oα_u±α_ Feed (Bounds) 53 45 0 45 11 8 24 40 N___ΠB1 Boiling 24 12 40 12 24 E int (°F) 960- 950- 9601- 1D50H 850/ — steau 1050 When one hundred pounds of an East Texas vacuum gas oil with a normal boiling point range from 650°F to 1100°F. is to be treated using the process of the present invention, the feedstock at 300 β F. and - > atmospheric pressure is pumped through the heat exchanger 52 of the primary separator 8 , and further heated to about 750°F., then introduced into the pre-pyrolysis cracker at a temperature of about 980 β F. and a pressure in the range of 400psig. The olefin precursors are O separated from their aromatic linkages by reducing both -=• the weight and hydrogen concentration in the 1020°F.+ boiling range. Thereafter the pre-pyrolysis cracked feedstock is introduced into the primary separator 8 through a line 30 wherein the pressure is reduced to "' "" about 100 psig. The light overhead fraction is introduced through line 32 into line 24 and used as feedstock for the light hydrocarbon cracking furnace. The light over¬ head fraction of 36 pounds has a normal boiling point of about 450°F. The lighter treated heavy hydrocarbon 0 stream in line 34 has a normal boiling point range of 450°F. to 950°F. This stream is diluted with steam provided by line 60 at a rate of 10 pounds per 54 pounds of hydrocarbon. The resultant diluted lighter treated heavy hydrocarbon stream is further heated in coil 36 o 5 the convection section 6 before being partially cracked^ in coil 38 of the furnace pre-cracker section 10 at a temperature of about 1350°F. Simultaneously, 36 pounds of light hydrocarbon is preheated in coil 26 and diluted with 20 pounds of steam provided through line 70, then 0 cracked at 1600°F. in coil 42 of light hydrocarbon cracking furnace section 12. The cracked light hydro¬ carbon from the coil 42 and the partially cracked heavy hydrocarbon from coil 38 are joined in line 54 and delivered to coil 46 of the DUOCRACKER 14 wherein the 5 completely cracked light hydrocarbon is partially quenched and the partially cracked heavy hydrocarbon is further cracked to completion. The resultant product is quenched in quench exchanger 20 and the products separated and analyzed. The ethylene yield attributable to the original 100 pounds of heavy hydrocarbon feed is 20 weight percent. The heavy fuel oil fraction of 13 pounds exiting the primary separator 8 through line 56 is rapidly quenched to a temperature of about 825°F. The heavy fuel oil fraction is then fed to the stripper 82 where a 3 pound heavy hydrocarbon fraction is separated from the heavy fuel oil fraction and recycled to the heavy hydrocarbon feedstock line 18 through line 62. Ten pounds of the heavy fuel oil fraction is removed through line 58. Three examples in addition to the previous one are shown in tabular form (Table I). Example B illustrates the effect of the invention on a vacuum gas oil as a heavy hydrocarbon feedstock and a purchased light hydrocarbon (naphtha) as the feedstock for the light hydrocarbon cracking furnace side of the DUOCRACKING' process. Example C illustrates the effect of the invention on an atmospheric towers bottom as the heavy hydrocarbon feedstock and dilution steam introduced through line 80 prior to the pre-pyrolysis cracking step. Example D illustrates the effect of the invention on an atmospheric towers bottom as the heavy hydrocarbon feedstock with dilution steam as in Example C and additionally a purchased light hydrocarbon (naphtha) as the feedstock for the light hydrocarbon cracking furnace side of the DUOCRACKING process. As seen in the foregoing examples, this invention relates generally to a process of improving olefin production from heavy hydrocarbon feedstocks by separating olefin precursors from their aromatic linkages by reducing both the weight and hydrogen concentration in the 1020 β F.+ boiling range and thereby forming a carbon rfch liquid fuel product. Specific embodiments of the invention have been described and shown in the examples accompanying drawing to illustrate the application of the inventive principles.

Claims: WHAT IS CLAIMED IS: 1. A process for converting heavy hydrocarbon feedstocks to olefins comprising the steps of: (a) subjecting the heavy hydrocarbon feedstock to pre-pyrolysis cracking at pressures above 150 psig; temperatures above 850 β F. and residence times of 0.5 to 3 minutes; (b) subjecting the pre-pyrolysis cracked feedstock to. a pressure drop; (c) separating the pre-pyrolysis cracked feedstock into a lighter treated heavy hydrocarbon fraction and a heavy fuel oil fraction; and (d) thermally cracking the lighter treated heavy hydrocarbon fraction to produce olefins.. 2. A process as in Claim 1 wherein the pre-pyrolysis cracking pressure is above 300 psig, the pressure drop to which the pre-pyrolysis cracked feedstock is subjected is about 200 psi and the separation of the pre-pyrolysis cracked feedstock into fractions occurs at about 100 psig. 3. A process as in Claim 1 wherein-the pre-pyrolysis cracking pressure is above 400- sig, the pressure drop to which the pre-pyrolysis cracked feedstock is subjected is about 300 psi and the separation of the pre-pyrolysis cracked feedstock into fractions occurs at about 100 psig. 4. A process as in Claim 1 wherein the heavy hydrocarbon feedstock is a hydrocarbon having an average boiling point above 1000°F. 5. A process as in Claim 1 wherein the heavy hydrocarbon feedstock is selected from the group con¬ sisting of vacuum gas oil, atmospheric gas oil, atmospheric tower bottoms, high boiling distillate gas oils and other residual feedstock. 6. A process as in Claim 1 comprising the further -step of diluting the heavy hydrocarbon feedstock with steam in a ratio of less than 0.1 pound of steam per pound of heavy hydrocarbon prior to the pre-pyrolysis cracking step. 7. A process as in Claim 1 wherein the pre-pyrolysis cracking temperature -is above 950°F and the pressure is above 300 psig. 8. A process as in Claim 4 wherein the cracking severity in terms of methane yield is less than 2 percent. 9. A process as in Claim 5 wherein the cracking severity in terms of methane yield is less than 1 percent. 10. A process as in Claim 1 wherein the concentration of asphaltene precursors in the lighter treated heavy hydrocarbon fraction * and the light overhead fraction is reduced to below 100 ppm. 11. A process as in Claim 1 wherein the heavy fuel oil fraction contains at least 80 weight percent of the asphaltene precursors found in the original heavy hydrocarbon feedstock and a hydrogen concentration below 8.5 weight percent. 12. A process as in Claim 1 further comprising the step of separating a light overhead * fraction from the lighter treated heavy hydrocarbon fraction. 13. A process as in Claim 10 wherein the lighter treated heavy hydrocarbon fraction and the light overhead fraction contain over 17 weight percent hydrogen and over 80 percent of the olefin precursors available from the original heavy hydrocarbon feedstock. 14. A process as in Claim 1 wherein the heavy fuel oil fraction is quenched to below 900°F in less than 10 milliseconds. .•- 15. A process as in Claim 11 wherein the heavy fuel oil fraction .. is quenched to below 850 β F in less than 10 milliseconds. 16. A process as in Claim 12 comprising the further steps of feeding the light overhead fraction to the light hydrocarbon cracking furnace of the DUOCRACKING system; completely cracking the lig'it overhead fraction in the light hydrocarbon cracking, furnace of the DUO¬ CRACKING system; diluting the lighter treated heavy hydrocarbon fraction with steam; feeding the diluted lighter treated heavy hydrocarbon fraction to the pre-cracker section of the DUOCRACKING system; partially cracking the lighter treated heavy hydrocarbon fraction in the pre-cracker section of the DUOCRACKING system; combining the competely cracked light overhead fraction and the partially cracked heavy hydrocarbon fraction; then feeding the combined completely cracked light over¬ head fraction and the partially cracked heavy hydrocarbon fraction to a cracking furnace to completely crack the partially cracked heavy hydrocarbon fraction. 17. A process as in Claim 1 comprising the further steps of diluting the lighter treated heavy hydrocarbon fraction with steam; partially cracking the diluted lighter treated heavy hydrocarbon fraction at a temperature of 930 C F to 1500°F and a pressure of over 50 psig; cracking a light hydrocarbon completely; and combining the completely cracked light hydrocarbon stream and the partially cracked heavy hydrocarbon fraction to further crack the partially cracked heavy hydrocarbon fraction. 18. A process as in Claim 13 wherein the total amount of dilution steam used in pyrolyzing the lighter treated heavy hydrocarbon fraction is less than 0.5 pound of steam per pound of hydrocarbon. t 19. A process as in Claim 13 wherein the fuel oil product from the integrated pyrolyzing process contains less than 5% asphaltenes. 20. A thermal treatment process for producing olefins from heavy hydrocarbon feedstocks comprising: (a) a subjecting the heavy hydrocarbon feedstock to pre-pyrolysis cracking whereby the olefin precursors are separated from their aromatic linkages by reducing both the weight and hydrogen concentration in the higher boiling point fraction; (b) separating the lighter olefin precursor concentrate from the heavier carbon rich fuel product; and (c) cracking the light concentrate to produce olefins. i i , 21. A process for converting heavy hydrocarbon feedstocks to olefins comprising the steps of: (a) preheating the heavy hydrocarbon feedstock to a temperature of 750°F; (b) subjecting the heavy hydrocarbon feedstock to prε-pyrolysis cracking at a pressure of 400 psig and a temperature of 980°F; (c) subjecting the pre-pyrolysis cracked feedstock to a pressure drop of 300 psig; 10 (d) separating the pre-pyrolysis cracked feedstock into a light overhead fraction, a heavy fuel oil fraction and a lighter treated heavy hydrocarbon? and (e) thermally cracking the light overhead •*" fraction and the lighter treated heavy hydrocarbon to produce olefins. 22. A process as in Claims 16 or 21 wherein the light overhead fraction is a hydrocarbon with a 0 boiling point of 450°F and below, the heavy fuel oil fraction is a hydrocarbon,with a boiling point of 950°F and above.and the lighter treated heavy hydrocarbon has a boiling point between 450°F and 950°F. 5 0 5 23. A process as in Claim 17 wherein the light overhead fraction is thermally cracked to temperatures between 1500°F to 1700°F at a residence time of 0.1 seconds; the lighter treated heavy hydrocarbon is partially cracked to a temperature of about 950°F to 1400°F at a residence time of 0.05 to 0.2 seconds; and the completely cracked light overhead fraction and the partially cracked heavy hydrocarbon fraction are combined in a single stream which composite stream is subjected to further cracking conditions to temperatures of 1400 C F to 1600°F at residence times of 0.02 to 0.05 seconds to completely crack the partially cracked heavy hydrocarbon fraction. 24. An apparatus for cracking a heavy hydrocarbon feedstock to produce olefins comprising: (a) a pre-pyrolysis cracker; _» (b) a primary separator for separating the effluent from the pre-pyrolysis cracker into a heavy fuel oil fraction and a treated heavy hydrocarbon fraction; (c) a pyrolysis furnace having a heavy hydrocarbon cracking coil for partially cracking the treated heavy hydrocarbon fraction emanating from the primary separator and also having a light hydrocarbon cracking coil for completely cracking a light hydrocarbon feedstock; (d) a DUOCRACKER for completely cracking the partially cracked heavy hydrocarbon stream emanating from the heavy hydrocarbon cracking coil of the pyrolysis furnace while quenching the completely cracked light hydrocarbon stream emanating from the light hydrocarbon cracking coil of the pyrolysis furnace; and (e) a quencher for quenching the composite stream of heavy and light hydrocarbons from the DUOCRACKER to terminate the reactions.

Inventors: JOHNSON AXEL R, NARAYANAN SWAMI, WOEBCKE HERMAN, JOHNSON, AXEL, R., NARAYANAN, SWAMI, WOEBCKE, HERMAN
Applicants: STONE & WEBSTER ENG CORP, STONE & WEBSTER ENGINEERING CORP.
Application year: 1985
Main classification: C10G51
IPC codes: C10G51