Process scheme for maximizing heavy oil conversion through phased asphaltene elimination

Abstract

A system is provided for upgrading an input stream 101 of straight run vacuum residue or cracked feedstock, including a vacuum tower 500, a hydrocracking unit 510, a high lift solvent deasphalting unit 520, a low lift solvent deasphalting unit 530, and a bitumen injection unit 540 or a pitch pelletizing unit 640, and optionally a hydrotreating reactor 750. The system and its components can deliver distillate and naphtha products, light ends products, an asphaltene lean heavy deasphalted oil stream 125, an asphaltene rich pitch stream 126, a light deasphalted oil that is a lubricant base oil feedstock, a heavy oil stream 137, a bitumen and asphalt stream 145, or a solid fuel. Further provided is a process including the steps of introducing straight run vacuum residue or cracked feedstock into the system and operating the system, the steps of operating the system including fractionation, solvent stage deasphalting, and hydrocracking.

Description

Background Art

[0001] Refinery residues are often blended with cutter stocks to produce a transportable and marketable fuel oil. Some refineries employ pyrolysis technology to produce fuel oil.

[0002] A typical pyrolysis technology platform may include both a visbreaking unit and a pyrolysis unit. The fuel oil produced by these operations becomes what is known as "cracked fuel oil". Straight-run residues (i.e., those not cracked) are also used to produce fuel oil, and straight-run residues may be blended or mixed with the cracked fuel oil.

Summary of the Invention

Means for Solving the Problems

[0003] [[ID=第十九条]]This summary is provided to introduce selected concepts that will be further described in the detailed description. This summary is not intended to identify key or essential features of the claimed subject matter, nor is it intended to be used as an aid in limiting the scope of the claimed subject matter.

[0004] In one embodiment, one or more embodiments disclosed relate to an input flow upgrading system, which may include a vacuum tower, a hydrocracking unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower, a high-lift solvent delamination unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower, a low-lift solvent delamination unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower, and a bitumen injection unit connected downstream of the vacuum tower and the high-lift solvent delamination unit and in fluid communication with the vacuum tower and the high-lift solvent delamination unit. The vacuum tower may receive an input flow of straight-run vacuum residue or cracking feed material and be configured to separate the input flow into a vacuum tower light flow and a vacuum residue flow. The hydrocracking unit may receive a combined flow of the vacuum tower light flow and heavy delamination oil flow, as well as a hydrogen flow, and be configured to feed distillates and naphtha products, as well as light end products. The heavy deburring oil stream may be in fluid communication with a hydrocracking unit and a high-lift solvent deburring unit. The high-lift solvent deburring unit may receive a butane stream and a combined stream that may include a first portion of a reduced-pressure residue stream, a first portion of a hydrocracking bleed stream, and a heavy oil stream, and may be configured to deliver an asphaltene lean heavy deburring oil stream and an asphaltene rich pitch stream. The unconverted oil stream may be in fluid communication with the hydrocracking unit, the high-lift solvent deburring unit, and a bitumen injection unit. The low-lift solvent deburring unit may receive a propane stream and a second portion of a reduced-pressure residue stream, and may be configured to deliver a light deburring oil that may be a lubricating oil base oil feedstock and a heavy oil stream. The heavy oil stream may be in fluid communication with the high-lift solvent deburring unit. The bitumen injection unit may be configured to receive the combined flow of the second portion of the hydrocracking bleed flow, the remainder of the reduced-pressure residue flow, and the low-viscosity diesel flow, and to deliver the bitumen and asphalt flow. The low-viscosity diesel flow may be in fluid communication with the bitumen injection unit. The reduced-pressure residue flow may be in parallel with the high-lift solvent delamination unit, the low-lift solvent delamination unit, and the bitumen injection unit.

[0005] In another embodiment, one or more embodiments disclosed relate to an input flow upgrading system, which may include an input flow of straight-run vacuum residue or cracking feed material, a vacuum tower, a hydrocracking unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower, a high-lift solvent delamination unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower, a low-lift solvent delamination unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower, and a pitch pelletizing unit connected downstream of the high-lift solvent delamination unit and in fluid communication with the high-lift solvent delamination unit. The vacuum tower may be configured to receive the input flow and separate the input flow into a vacuum tower light flow and a vacuum residue flow. The hydrocracking unit may be configured to receive a combined flow of the vacuum tower light flow and a heavy delamination oil flow, as well as a hydrogen flow, and to feed distillates and naphtha products, as well as light end products. The heavy deflaking oil stream may be in fluid communication with a hydrocracking unit and a high-lift solvent deflaking unit. The high-lift solvent deflaking unit may receive a combined flow of butane, a first portion of the reduced-pressure residue stream, an unconverted oil stream as a hydrocracking bleed stream, and a heavy oil stream, and deliver an asphaltene-lean heavy deflaking oil stream and an asphaltene-rich pitch stream. The unconverted oil stream may be in fluid communication with the hydrocracking unit and the high-lift solvent deflaking unit. The low-lift solvent deflaking unit may receive a combined flow of propane, a second portion of the reduced-pressure residue stream, and deliver a light deflaking oil, which is a raw material for lubricating oil base oil, and a heavy oil stream. The heavy oil stream may be in fluid communication with the high-lift solvent deflaking unit. The pitch pelletizing unit may receive an asphaltene-rich pitch stream and deliver solid fuel. The asphaltene-rich pitch flow may be in fluid communication with the high-lift solvent delamination unit and the pitch pelletization unit. The reduced-pressure residue flow may be in parallel with the high-lift solvent delamination unit and the low-lift solvent delamination unit.

[0006] In another embodiment, one or more embodiments disclosed relate to an input flow upgrade system, which may include an input flow of straight-run vacuum residue or cracking feed material; a vacuum tower; a hydrocracking unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower; a high-lift solvent delamination unit connected downstream of the vacuum tower and in fluid communication with the vacuum tower; a low-lift solvent delamination unit connected downstream of the high-lift solvent delamination unit and in fluid communication with the high-lift solvent delamination unit; a hydrogenation reactor connected downstream of the high-lift solvent delamination unit and the low-lift solvent delamination unit and in fluid communication with the high-lift solvent delamination unit and the low-lift solvent delamination unit; and a bitumen injection unit connected downstream of the vacuum tower and the high-lift solvent delamination unit and in fluid communication with the vacuum tower and the high-lift solvent delamination unit. The vacuum tower may be configured to receive the input flow and separate the input flow into a vacuum tower light flow and a vacuum residue flow. The hydrocracking unit may be configured to receive a hydrogen stream and a combined stream of the light stream from the vacuum column and the effluent from the hydrocracking reactor, and to feed distillates, naphtha products, and light end products. The effluent from the hydrocracking reactor may be in fluid communication with the hydrocracking unit as an effluent hydrocracking feed stream, and may also be in fluid communication with the hydrocracking reactor. The high-lift solvent delamination unit may be configured to receive a butane stream and a combined stream of the first portion of the vacuum residue stream and the first portion of the hydrocracking bleed stream, and to feed asphaltene lean heavy delamination oil streams and asphaltene rich pitch streams. The unconverted oil stream may be in fluid communication with the hydrocracking unit, the high-lift solvent delamination unit, and the bitumen injection unit. The low-lift solvent delamination unit may be configured to receive a propane stream and a first portion of the asphaltene lean heavy delamination oil stream, and to feed light delamination oil and heavy oil streams, which are the base oil feedstocks for the lubricating oil. The heavy oil stream may be in fluid communication with the hydrogenation reactor. The hydrogenation reactor may be configured to receive the hydrogen stream, as well as the combined stream of the second portion of the asphaltene lean heavy deslag oil stream and the heavy oil stream, and to deliver the light end product.The bitumen injection unit may be configured to receive a combined flow of a second portion of the hydrocracking bleed flow, a second portion of the reduced-pressure residue flow, an asphaltene-rich pitch flow, and a low-viscosity diesel flow, and to deliver the bitumen and asphalt flow. The low-viscosity diesel flow may be in fluid communication with the bitumen injection unit. The reduced-pressure residue flow may be in parallel with the high-lift solvent delamination unit and the bitumen injection unit.

[0007] In yet another embodiment, one or more embodiments disclosed may include the steps of introducing straight-run vacuum residue or cracking feed into a system and operating the system, wherein the steps of operating the system include a fractional distillation step, a solvent step delamination step, and a hydrocracking step. The fractional distillation step may include operating the system using the input of straight-run vacuum residue or cracking feed to produce fractionally distilled distillates, diesel products, and vacuum residue from a vacuum tower, and combining the fractionally distilled distillates and diesel products into a single internal flow as a vacuum tower light flow. The solvent step delamination step may include operating the system using the input of a combined internal flow of vacuum residue and unconverted oil to produce asphaltene lean heavy delamination oil and asphaltene rich pitch from a high-lift solvent delamination unit. The solvent deflaking step may further include operating the system using the input of vacuum residue or asphaltene lean heavy deflaking oil to produce light deflaking oil and heavy oil, which are the raw materials for the lubricating oil base oil supply, from a low-lift solvent deflaking unit. The hydrocracking step may further include operating the system using the input of a combined internal flow of vacuum residue and asphaltene lean heavy deflaking oil to produce naphtha products and unconverted oil from a hydrocracking unit.

[0008] Other aspects and advantages of the subject matter of the claims will become apparent from the following detailed description and the attached claims. [Brief explanation of the drawing]

[0009] [Figure 1]Figure 1 shows a system which is a parallel solvent de-cleaning residue oil upgrading complex including bitumen generation, according to one or more embodiments.

[0010] [Figure 2] Figure 2 shows a system that is a parallel solvent delamination residue upgrading complex that does not involve bitumen formation, according to one or more embodiments.

[0011] [Figure 3] Figure 3 shows a system that is a solvent de-clearing and decomposition raw material residue upgrading complex including bitumen generation, according to one or more embodiments. [Modes for carrying out the invention]

[0012] Detailed explanation One or more embodiments relate to systems and processes for oil separation and upgrading. Specifically, the systems are used to convert residues into fuel and petrochemical feedstock.

[0013] One or more embodiments of the present disclosure relate to a heavy oil conversion process. The process can convert a reduced-pressure residue stream into fuels (diesel, gasoline, and naphtha, etc.); lubricating oil base oil feedstocks; olefins such as ethylene and propylene; and aromatic compounds such as butylene, benzene, toluene, and xylene.

[0014] A system for oil separation and upgrading includes, in one or more embodiments, an input stream containing residue, a vacuum tower, a vacuum tower light stream (distillate and diesel fuel), a vacuum residue stream, a hydrocracking unit, a high-lift solvent delamination unit, a low-lift solvent delamination unit, and a bitumen injection unit.

[0015] The process includes fractional distillation and stepwise solvent delamination. Stepwise solvent delamination can also be called stepwise asphaltene removal. In one or more embodiments, asphaltene removal of the vacuum residue is made possible by stepwise solvent delamination. The resulting delamination oil in one or more embodiments is treated by hydrocracking or fluid catalytic cracking units. For example, heavy pitch removed from the solvent delamination stage can be upgraded to bitumen or used as fuel for gasification.

[0016] The system may include a vacuum tower, a hydrocracking unit, a high-lift solvent delamination unit, and a low-lift solvent delamination unit. The system may further include a bitumen injection unit or a pitch pelletization unit. The bitumen injection unit is configured to receive vacuum residue and may therefore also be called a vacuum residue bitumen injection unit.

[0017] The products generated from the hydrocracking unit, the low-lift solvent delamination unit, and the bitumen injection unit can be fuel products, such as white oil, lubricating oil base oil feedstocks, petrochemical feedstocks, and combinations thereof.

[0018] The input flow is introduced into a vacuum tower. The input flow may be straight-run atmospheric residue or cracking feedstock. The vacuum tower is configured to receive the input flow and separate it into a vacuum tower light flow (diesel fuel) and a vacuum residue flow (bottom flow). The vacuum tower light flow contains substances that boil at a true boiling point (TBP) below nominal 560°C.

[0019] The hydrocracking unit is connected downstream of the vacuum tower and is in fluid communication with the vacuum tower. The hydrocracking unit is configured to treat the light flow from the vacuum tower and the heavy oil flow from the high-lift solvent defraction unit using hydrogen and catalysts. The hydrocracking unit converts light oil, distillates, and heavy defraction oil into naphtha, distillates, and high-value fuel products such as "light end" products, such as liquefied petroleum gas (LPG) and natural gas. The hydrocracking unit is configured to feed distillates and naphtha products, as well as light end products. Similarly, the hydrocracking unit is configured to feed an unconverted oil flow called the hydrocracking bleed flow. The unconverted oil (exclusion) flow is fed to the bitumen injection unit.

[0020] The high-lift solvent delamination unit is connected downstream of the vacuum tower and the low-lift solvent delamination unit and is in fluid communication with the vacuum tower and the low-lift solvent delamination unit. The high-lift solvent delamination unit is in fluid communication with the hydrocracking unit. The high-lift solvent delamination unit is configured to produce asphaltene lean heavy delamination oil and asphaltene rich pitch.

[0021] The low-lift solvent deflaking unit generates light deflaking oil and heavy oil flows, which are the raw materials for supplying lubricating oil base oil. The heavy oil flows are sent to the high-lift solvent deflaking unit.

[0022] The bitumen injection unit is connected downstream of the depressurization tower and the high-lift solvent delamination unit and is in fluid communication with the depressurization tower and the high-lift solvent delamination unit. In one or more embodiments, the bitumen injection unit is connected downstream of the depressurization tower, the high-lift solvent delamination unit, and the hydrocracking unit and is in fluid communication with the depressurization tower, the high-lift solvent delamination unit, and the hydrocracking unit. The high-lift solvent delamination unit (bottom of the tower) pitch is blended with a small amount of light excavation fuel flow produced using a composite, and air may be injected. The small amount of light excavation fuel flow is about 3 to about 10% of the fresh feed rate to the depressurization tower. The bitumen injection unit produces bitumen and asphalt, which may be road / pavement asphalt.

[0023] The pitch pelletizing unit produces pelletized or flaked pitch that can be used as a solid fuel.

[0024] In one or more embodiments, the hydrocracking unit is replaced by a hydrotreating with a fluid catalytic cracking unit.

[0025] In one or more embodiments, if asphalt cannot be produced, the pitch can be disposed of as fuel to a boiler or a partial oxidation unit.

[0026] One or more embodiments relate to a parallel solvent deasphalting residue upgrading complex including bitumen production.

[0027] One or more embodiments relate to a parallel solvent deasphalting residue upgrading complex not including bitumen production.

[0028] One or more embodiments relate to a solvent deasphalting cracked feedstock residue upgrading complex including bitumen production. Parallel solvent deasphalting residue upgrading complex including bitumen production

[0029] FIG. 1 shows a system that is a parallel solvent deasphalting residue upgrading complex including bitumen production. System 100 is a residue upgrading complex including parallel solvent deasphalting and bitumen production. This means that the high-lift solvent deasphalting unit and the low-lift solvent deasphalting unit have a parallel input of vacuum residue from a single source. In one or more embodiments, the bitumen injection unit also has a parallel input of vacuum residue from the same source.

[0030] System 100 has several feed streams and product streams. The input stream 101 is introduced into the vacuum tower 500 and contains hydrocarbons having a true boiling point (TBP) above 370°C. The input stream 101 may be, but is not limited to, input refinery residue containing atmospheric residue oil produced from a crude oil distillation unit having a TBP above 370°C. The hydrogen feed stream 115 is introduced into the hydrocracking unit 510 and consists of hydrogen. The low-viscosity diesel stream 142 is combined with the other streams to form the bitumen injection unit feed stream 144. The low-viscosity diesel stream may have a TBP in the range of about 300°C to about 450°C and a viscosity in the range of about 3 centistokes (cSt) to about 8 cSt. The low-viscosity diesel stream 142 is such that the bitumen injection unit feed stream 144 (combined stream) may have a viscosity in the range of about 800 cSt to about 1200 cSt. The bitumen injection unit supply stream 144 may contain approximately 50% by weight of reduced pressure residue (derived from reduced pressure residue stream 103C), approximately 30% by weight of pitch (derived from asphaltene-rich pitch stream 126), and the remainder derived from the low-viscosity diesel stream 142 and the hydrocracking bleed stream 111B. The hydrocracking bleed stream 111B may contain approximately 2% to 20% by weight of diesel compared to the total bitumen injection unit supply stream 144.

[0031] The light end stream 116 is produced as light gases and light materials derived from hydrocracking. The light end stream may contain saturated material in addition to an olefin content of less than approximately 2%. The light end stream 116 exits the hydrocracking unit 510 and contains excess hydrogen derived from the operation of the hydrocracking unit.

[0032] The combined distillate and naphtha product stream 117 exits the hydrocracking unit 510. The combined distillate and naphtha product stream contains fuel or petrochemical feedstock.

[0033] The light deburring oil product stream 136 exits the low-lift solvent deburring unit 530. The light deburring oil product stream contains light deburring oil, which can be a lubricating oil base oil feedstock that can be used, for example, to produce bright oil.

[0034] The bitumen and asphalt flow 145 exits from the bitumen injection unit 540. Bitumen and asphalt flows 145 may include roof grade, pavement grade, road grade asphalt (bitumen), or a combination thereof.

[0035] In system 100, the input flow 101 is introduced into system 100 via the vacuum tower 500. In one or more embodiments, the configuration of system 100 enables the generation of two products from the vacuum tower 500: a vacuum tower light flow 102, which is a combined flow of distillate flow 102A and vacuum light oil flow 102B containing hydrocarbons that boil at a TBP of less than 560°C, and a vacuum residue flow 103 containing hydrocarbons that boil at a TBP of 560°C or higher.

[0036] Distillate flow 102A contains hydrocarbons that boil at a TBP of less than approximately 370°C, and reduced-pressure diesel flow 102B contains hydrocarbons that boil at a TBP between approximately 370°C and approximately 560°C.

[0037] System 100 is configured such that the reduced-pressure residue flow 103 exiting the reduced-pressure tower 500 is proportionally divided into three parallel flows. The first portion 103A of the reduced-pressure residue flow is led to a high-lift solvent de-abrasion unit 520 for processing. The first portion 103A of the reduced-pressure residue flow is about 40% to about 60% by weight, for example, about 45% to about 55% by weight. The second portion 103B of the reduced-pressure residue flow is led to a low-lift solvent de-abrasion unit 530 for processing. In one or more embodiments, the second portion 103B of the reduced-pressure residue flow is about 5% to about 15% by weight of the reduced-pressure residue flow 103, for example, about 8% to about 12% by weight, and is sent to the low-lift solvent de-abrasion unit. The remainder 103C of the reduced-pressure residue stream is led to the bitumen injection unit 540 for processing, for example, in a concentration of about 25% to 45% by weight, or about 35% to 45% by weight. The remainder 103C of the reduced-pressure residue stream is introduced into the bitumen injection unit supply stream 144, which is then introduced into the bitumen injection unit 540.

[0038] The reduced-pressure residue flow 103, divided into three parallel flows, may be advantageous when feed quality is lower compared to when each flow is in series. While we do not wish to be constrained by theory, the parallel flow configuration allows the defraction oil (DAO) to maintain a quality sufficient for supply to the fixed-bed catalyst unit. In contrast, the series flow configuration is more likely to require a residue hydrogenation treatment using fluid catalytic cracking (FCC), which consequently limits treatment options.

[0039] System 100 is configured such that a second portion 103B of the reduced-pressure residue flow can be sent to a low-lift solvent delamination unit 530. The low-lift solvent delamination unit 530 is configured to combine the second portion of the reduced-pressure residue flow with a propane flow (as a solvent, not shown) to separate the second portion of the reduced-pressure residue flow into two products. The solvent:reduced-pressure residue feed ratio may be about 6:1 to about 8:1 in one or more embodiments. The low-lift solvent delamination unit 530 provides a lift of 40% or less, for example, less than 40%, less than about 35%, less than about 30%, or less than 30%. In one or more embodiments, the low-lift solvent delamination unit 530 provides a non-zero lift, meaning the lift is not 0%.

[0040] System 100 is configured such that the low-lift solvent deblecking unit 530 can produce two product flows: a light deblecking oil product flow 136 that exits System 100 as a product, and a heavy oil flow 137 that can exit from the bottom as an excavation flow. The produced light deblecking oil is a cleaner lubricating oil base oil feedstock than the deblecking oil. The produced light deblecking oil can meet the Group I base oil feedstock brightstock quality by containing less than 1.5 ppm (parts per million) of metal in the light deblecking oil product flow 136 and having a viscosity of less than 35 cSt (centistokes), which will be understood by those skilled in the art.

[0041] The system 100 is configured such that a light flow 102 from the vacuum tower can be directed toward the hydrocracking unit 510. The asphaltene lean heavy deflaking oil flow 125 from the high-lift solvent deflaking unit 520 can combine with the light flow 102 from the vacuum tower to form a hydrocracking feed flow 113. Furthermore, a hydrogen feed flow 115 consisting of hydrogen is introduced into the hydrocracking unit 510. The hydrocracking unit includes a fixed-bed catalyst, which will be described later. The feed to the hydrocracking unit 510 may be limited by the amount of heavy deflaking oil as a component. The heavy deflaking oil may be from a high-conversion-rate hydrocracking unit, for example, a unit with a conversion rate of 95% or more, or it may be 40% by weight or less of the feed.

[0042] In one or more embodiments, the system 100 is configured such that the hydrocracking unit 510 can operate under hydrocracking conditions and in the presence of excess hydrogen and catalyst. During operation, the hydrocracking unit is configured to convert combined distillates, diesel fuel, and asphaltene lean heavy detrecced oil into distillates, naphtha, light end, and purported waste. In one or more embodiments, the operating temperature of the hydrocracking unit is in the range of approximately 360°C to 420°C. The operating pressure of the hydrocracking unit is in the range of approximately 70 absolute bar (bara) to 170 bara (partial pressure of hydrogen).

[0043] The hydrocracking unit 510 may also be configured to separate the products into several product streams. The right end products and excesses may be configured so that the distillate and naphtha products exit the hydrocracking unit 510 and system 100 as a combined distillate and naphtha product stream 117 for further processing. The hydrocracking unit 510 may be further configured so that the right end products and excess hydrogen can exit the hydrocracking unit 510 and system 100 as a right end stream 116. The hydrocracking unit 510 may be further configured so that the waste material from the hydrocracking unit 510 exits the unit as a hydrocracking bleed stream 111, which is a system recycling stream.

[0044] In one or more embodiments, the configuration of system 100 may be such that the hydrocracking unit 510 is a catalytic cracking unit. The catalytic cracking unit may be a conventional riser fluid contact unit or a high catalyst / oil ratio downer design.

[0045] System 100 is configured such that a hydrocracking bleed stream 111 containing unconverted oil (or unconverted oil stream) is split into two streams. A first portion 111A of the hydrocracking bleed stream, for example about 80% to 100% by weight, may be sent to a high-lift solvent delamination unit 520. Before being introduced to the high-lift solvent delamination unit 520, the first portion 111A of the hydrocracking bleed stream may be combined with other streams to form a high-lift solvent delamination unit feed stream 124. A second portion 111B of the hydrocracking bleed stream, for example more than 0% to about 20% by weight, may be sent to a bitumen injection unit 540 for further processing. Before being introduced to the bitumen injection unit 540, the second portion 111B of the hydrocracking bleed stream may be combined with other streams to form a bitumen injection unit feed stream 144.

[0046] In the configuration of system 100, multiple flows can be combined to form a high-lift solvent delamination unit supply flow 124. In system 100, a first portion 103A of the reduced-pressure residue flow can be combined with both a first portion 111A of the hydrocracking bleed flow and a heavy oil flow 137 from the low-lift solvent delamination unit 530 to form the high-lift solvent delamination unit supply flow 124. System 100 can be configured to supply the high-lift solvent delamination unit with a mixture of reduced-pressure residue, asphaltized heavy oil, and recycled material from the hydrocracking unit.

[0047] The high-lift solvent delamination unit can be considered a "last resort unit" in system 100, in that it can return useful fluid products to system 100 for recycling. That is, the bottom products from this unit are sent for conversion in the bitumen injection process and are no longer available for recovery of useful materials for chemical treatment. System 100 may be configured so that the high-lift solvent delamination unit feed stream 124 can be introduced into the high-lift solvent delamination unit 520. System 100 may also be configured so that the high-lift solvent delamination unit 520 can be treated with a mixture of reduced-pressure residue, unconverted oil, and heavy oil in the presence of butane solvent to produce asphaltene lean products and asphaltene rich products. The high-lift solvent delamination unit may be configured to receive a butane stream. The solvent (butane):oil (combined vacuum residue, unconverted oil, and heavy oil) ratio may range from approximately 3:1 to approximately 8:1, for example, approximately 3:1 to approximately 7:1, approximately 3:1 to approximately 6:1, approximately 4:1 to approximately 8:1, approximately 4:1 to approximately 7:1, or approximately 4:1 to approximately 6:1. Butane (and propane, as a butane stream or propane stream, where applicable) is not shown. The extraction pressure of solvent delamination units, such as high-lift solvent delamination units, is greater than the critical pressure of the solvent used in the solvent delamination unit.

[0048] System 100 may be configured such that the high-lift solvent delamination unit 520 can produce two products from the conversion of the high-lift solvent delamination unit feed stream, both of which are provided to other units for further processing. An asphaltene lean heavy delamination oil stream 125 may be produced as a light product. As previously mentioned, the asphaltene lean heavy delamination oil stream 125 is combined with the vacuum column light stream 102 to form the hydrocracking feed stream 113. An asphaltene rich pitch stream 126 may also be formed as a bottom product. The asphaltene rich pitch stream 126 is directed toward the bitumen injection unit 540 for conversion.

[0049] In the configuration of system 100, multiple flows can be combined to form the bitumen injection unit feed flow 144. The remainder of the vacuum residue flow 103C (third portion) is combined with the asphaltene-rich pitch flow 126 from the high-lift solvent delamination unit 520 and the second portion 111B of the hydrocracking bleed flow. Furthermore, the low-viscosity diesel flow 142 introduced into system 100 can also be combined with three other flows to form the bitumen injection unit feed flow 144. The blend ratio of the remainder of the vacuum residue flow 103C and the asphaltene-rich pitch flow 126 is such that 103C (mixture of vacuum residues) is greater than 40%, the asphaltene-rich pitch flow 126 (pitch) is less than 30%, and the remainder is a diesel cutter to maintain the viscosity of the bitumen injection unit feed at less than approximately 1200 centistokes (cSt).

[0050] System 100 is configured such that a bitumen injection unit feed stream 144 is introduced into a bitumen injection unit 540 and converted into bitumen and asphalt products. The bitumen injection unit is an air injection unit in which a hydrocarbon mixture (bitumen injection unit feed stream 144) is heated to a temperature range of approximately 300°C to approximately 500°C and air is blown in at a pressure of approximately 1 bar to approximately 2 bar. The resulting bitumen and asphalt may be road-grade products. The bitumen and asphalt products can exit the bitumen injection unit 540 and system 100 via a bitumen and asphalt stream 145. Parallel solvent debris residue oil upgrading complex that does not contain bitumen formation

[0051] Figure 2 shows a system that is a parallel solvent delamination residue upgrading complex. System 200 is a residue upgrading complex that does not involve bitumen formation. This means that the high-lift solvent delamination unit and the low-lift solvent delamination unit have parallel inputs of reduced-pressure residue originating from a single source.

[0052] System 200 has several feed streams and product streams. The input stream 201 is introduced into the depressurization tower 600 and contains hydrocarbons with a TBP above 370°C. The hydrogen feed stream 215 is introduced into the hydrocracking unit 610 but consists of hydrogen. The light end stream 216 exits the hydrocracking unit 510 and contains light gases and excess hydrogen derived from the operation of the hydrocracking unit. The combined distillate and naphtha product stream 217 exits the hydrocracking unit 610 and contains fuel or petrochemical feedstock. The light deburring oil product stream 236 exits the low-lift solvent deburring unit 630 and contains light deburring oil, which is a lubricating oil base oil feedstock that can be used to produce bright oil. The solidified pitch stream 245 exits the pitch pelletizing unit 640 and contains pelletized or flakeled pitch that can be used as solid fuel.

[0053] In system 200, the input flow 201 is introduced into system 200 via the vacuum tower 600. In one or more embodiments, the configuration of system 200 enables the generation of two products from the vacuum tower 600: a vacuum tower light flow 202, which is a combined flow of distillate flow 202A and vacuum light oil flow 202B containing hydrocarbons that boil at a TBP of less than 560°C, and a vacuum residue flow 203 containing hydrocarbons that boil at a TBP of 560°C or higher.

[0054] Distillate flow 202A contains hydrocarbons that boil at a TBP of less than approximately 370°C, and reduced-pressure diesel flow 202B contains hydrocarbons that boil at a TBP between approximately 370°C and approximately 560°C.

[0055] System 200 is configured such that the reduced-pressure residue flow 203 exiting the reduced-pressure tower 600 is proportionally divided into two parallel flows. The first portion 203A of the reduced-pressure residue flow is led to a high-lift solvent de-abrasion unit 620 for processing. The first portion 203A of the reduced-pressure residue flow may be about 70% to about 90% by weight of the reduced-pressure residue flow 203 sent to the high-lift solvent de-abrasion unit, for example, about 75% to about 85% by weight. The second portion 203B of the reduced-pressure residue flow is led to a low-lift solvent de-abrasion unit 630 for processing. The second portion 203B of the reduced-pressure residue flow may be about 10% to about 30% by weight of the reduced-pressure residue flow 203 sent to the low-lift solvent de-abrasion unit, for example, about 15% to about 25% by weight.

[0056] System 200 is configured such that a second portion 203B of the reduced-pressure residue flow can be sent to a low-lift solvent delamination unit 630. The low-lift solvent delamination unit 630 is configured to combine the second portion of the reduced-pressure residue feed flow with a propane flow (as a solvent, not shown) to separate the second portion of the reduced-pressure residue feed flow into two products. The solvent:reduced-pressure residue feed ratio may be about 8:1 in one or more embodiments.

[0057] System 200 is configured such that the low-lift solvent deflaking unit 630 can generate two product flows: a light deflaking oil product flow 236 that exits System 200 as a product, and a heavy oil flow 237 that can exit from the bottom as an excavation flow. The generated light deflaking oil is a lubricating oil base oil feedstock.

[0058] The system 200 is configured such that a light flow 202 from the vacuum tower can be directed toward the hydrocracking unit 610. The asphaltene lean heavy de-abraded oil flow 225 from the high-lift solvent de-abrading unit 620 can be combined with the light flow 202 from the vacuum tower to form a hydrocracking feed flow 213. Furthermore, a hydrogen feed flow 215 consisting of hydrogen is introduced into the hydrocracking unit 610. The hydrocracking unit includes a fixed-bed catalyst, which will be described later.

[0059] In one or more embodiments, the system 200 is configured such that the hydrocracking unit 610 can convert the combined distillates, diesel fuel, and asphalten lean heavy detrecced oil under hydrocracking conditions and in the presence of excess hydrogen and a catalyst into distillates, naphtha, light end, and elimination materials.

[0060] The hydrocracking unit 610 may also be configured to separate the products into several product streams. The system 200 may be configured and operated so that the right-end products and excesses, and the distillate and naphtha products, exit the hydrocracking unit 610 and system 200 as a combined distillate and naphtha product stream 217 for further processing. The hydrocracking unit 610 may be further configured so that the right-end products and excess hydrogen exit the hydrocracking unit 610 and system 200 as a right-end stream 216 for further processing. The hydrocracking unit 610 may be further configured so that the waste material from the hydrocracking unit 610 exits the unit as a hydrocracking bleed stream 211, which is a system recycling stream.

[0061] In one or more embodiments, the system 200 may be configured such that the hydrocracking unit 610 is a catalytic cracking unit. The catalytic cracking unit may be a conventional riser fluid contact unit or a high catalyst / oil ratio downer design.

[0062] System 200 is configured so that the hydrocracking bleed stream 211 can be delivered to the high-lift solvent delamination unit 620.

[0063] In the configuration of system 200, multiple flows can be combined to form a high-lift solvent delamination unit supply flow 224. In system 200, a first portion 203A of the reduced-pressure residue flow can be combined with both the hydrocracking bleed flow 211 and the heavy oil flow 237 from the low-lift solvent delamination unit 630 to form the high-lift solvent delamination unit supply flow 224. System 200 can be combined so that the high-lift solvent delamination unit can be supplied with a mixture of reduced-pressure residue, asphaltized heavy oil, and recycled material from the hydrocracking unit.

[0064] The high-lift solvent delamination unit can be considered a “last resort unit” in system 200 for recycling useful fluid products back into system 200 and other units. That is, the bottom product from this unit is sent for conversion in the pitch pelletization process. System 200 may be configured so that the high-lift solvent delamination unit feed stream 224 can be introduced into the high-lift solvent delamination unit 620. System 200 may also be configured so that the high-lift solvent delamination unit 620 can process a mixture of vacuum residue, unconverted oil, and heavy oil in the presence of a butane solvent to produce asphaltene-rich and asphaltene-lean products. The solvent (butane):oil (vacuum residue, unconverted oil, and heavy oil) ratio may be in the range of about 5:1 in one or more embodiments.

[0065] System 200 may be configured such that a high-lift solvent delamination unit 620 can produce two products from the conversion of the high-lift solvent delamination unit feed stream, both of which are provided to other units for further processing. An asphaltene lean heavy delamination oil stream 225 may be produced as a light product. As previously mentioned, the asphaltene lean heavy delamination oil stream 225 is combined with the vacuum column light stream 202 to form a hydrocracking feed stream 213. An asphaltene rich pitch stream 226 may be produced as a column bottom product. The asphaltene rich pitch stream 226 is directed toward a pitch pelletization unit 640 for conversion.

[0066] System 200 may be configured such that an asphaltene-rich pitch stream 226 is introduced into a pitch pelletizing unit 640 and converted into pelletized or flake pitch. The solidified pitch may be a solid fuel that can be used, for example, in a boiler or partial oxidation unit. For example, the solidified pitch may be used as fuel in a boiler to generate steam, and the steam may be used in the facility to drive a steam turbine generator for power generation. The solidified pitch may be partially oxidized to synthesis gas, which may be used as fuel in a gas turbine to generate, for example, electricity or steam, or to produce hydrogen. The pelletized or flake pitch may be delivered from the pitch pelletizing unit 640 and System 200 via a solidified pitch stream 245. Solvent decomposition and decomposition raw material residue upgrade complex including bitumen generation

[0067] Figure 3 shows a system that is a solvent delamination residue upgrading complex including bitumen generation. System 300 is a residue upgrading complex including bitumen generation. In System 300, the high-lift solvent delamination unit and the bitumen injection unit have parallel inputs of reduced-pressure residue originating from a single source.

[0068] System 300 differs in part from Systems 100 and 200 because it can be a stepped flow system (meaning the solvent delamination units are in series). The reduced-pressure residue is first sent to the high-lift solvent delamination unit, and then a portion of the delamination oil is sent to the low-lift solvent delamination unit. In System 300, there is a fixed-bed residue treatment (hydrocracking reactor 750) upstream of the hydrocracking unit 710. Therefore, the quality of the delamination oil may be lower in System 300 compared to Systems 100 or 200, and the series-flow solvent delamination units can function (because the quality of the delamination oil in the conversion units is lower).

[0069] System 300 has several feed streams and product streams. The input stream 301 is introduced into the depressurization tower 700 and contains hydrocarbons with a TBP above 370°C. The hydrogenation feed stream 355 is introduced into the hydrogenation reactor 750 and consists of hydrogen. The hydrogen feed stream 315 is introduced into the hydrocracking unit 710 and consists of hydrogen. The low-viscosity diesel stream 342 is combined with the other streams to become the bitumen injection unit feed stream 344. The low-viscosity diesel stream 342 is a diesel stream with a target viscosity in the range of approximately 800-1200 cSt. The hydrogenated light end stream 356 exits the hydrogenation reactor 750 and contains light end products. The light end stream 316 exits the hydrocracking unit 710 and contains light gases and excess hydrogen from the operation of the hydrocracking unit. The combined distillate and naphtha product stream 317 exits the hydrocracking unit 710 and contains fuel or petrochemical feedstock. The light deburring oil product stream 336 exits the low-lift solvent deburring unit 730 and contains deburring oil which may be a lubricating oil base oil feedstock that can be used, for example, to produce bright oil. The bitumen and asphalt stream 345 exits the bitumen injection unit 740 and may contain road-grade asphalt.

[0070] In system 300, the input flow 301 is introduced into system 300 via the vacuum tower 700. In one or more embodiments, the configuration of system 300 enables the generation of two products from the vacuum tower 700: a vacuum tower light flow 302, which is a combined flow of distillate flow 302A and vacuum light oil flow 302B of hydrocarbons that boil at temperatures below 560°C, and a vacuum residue flow 303 containing hydrocarbons that boil at temperatures above 560°C.

[0071] Distillate flow 302A contains hydrocarbons that boil at a TBP of less than approximately 370°C, and reduced-pressure diesel flow 302B contains hydrocarbons that boil at a TBP between approximately 370°C and approximately 560°C.

[0072] System 300 is configured such that the reduced-pressure residue flow 303 exiting the reduced-pressure tower 700 is proportionally divided into two parallel flows. The first portion 303A of the reduced-pressure residue flow is led to a high-lift solvent de-abrasion unit 720 for processing. The first portion of the reduced-pressure residue flow may be about 50% to about 80% by weight of the reduced-pressure residue flow 303, for example, about 50% to about 70% by weight, or about 50% to about 60% by weight. The second portion 303B of the reduced-pressure residue flow is led to a bitumen injection unit 740 for processing. The second portion of the reduced-pressure residue flow may be about 20% to about 50% by weight of the reduced-pressure residue flow 303, for example, about 30% to about 50% by weight, or about 40% to about 50% by weight. The second portion 303B of the reduced-pressure residue stream is introduced into the bitumen injection unit supply stream 344, which is then introduced into the bitumen injection unit 740.

[0073] The system 300 is configured such that the asphaltene lean heavy delamination oil stream 325 from the high-lift solvent delamination unit 720 is divided into two parts. The second part 325B of the asphaltene lean heavy delamination oil stream is combined with the heavy oil stream 337 from the low-lift solvent delamination unit 730 to form a hydrogenation feed stream 353. Furthermore, a hydrogenation feed stream 355 consisting of hydrogen is introduced into the hydrogenation reactor 750.

[0074] As mentioned, in the configuration of system 300, the hydrogenation feed stream 353 can be processed in the hydrogenation reactor 750. The combined lift of the low-lift solvent delamination unit and the high-lift solvent delamination unit is greater than 75%, for example, 80%, 85%, 90%, or 95%. The lift of the high-lift delamination unit alone is approximately 60% or more, for example, 65%, 70%, 75%, 80%, 85%, or 90%. The hydrogenation feed stream 353 may have a high Conradson carbon value. The hydrogenation feed stream 353 may contain organometallic contaminants. For example, the metal content in the delamination oil may be greater than parts per million (ppm), and the Conradson residual carbon (value) in the feed may be greater than 8 ppm. These contaminants can be reduced by utilizing excess hydrogen and catalyst in the hydrogenation reactor through hydrogenation.

[0075] In one or more embodiments, the system 300 is configured such that the hydrogenation reactor 750 hydrogenates the combined asphaltene lean heavy deslag oil and heavy oil, converting it into heavy hydrogenation effluent and light end. The composition of the heavy hydrogenation effluent may include 85% or more of the residual influent heavy feed (as a substance that boils at about 370°C), with the metal and Conradson carbon ratio removed and the feed hydrogenated to a lower sulfur content (e.g., 90% or more desulfurization). One or more product streams may be present from the hydrogenation reactor 750. The system 300 is further configured such that the hydrogenated light end stream 356 exits the hydrogenation reactor 750 and the system 300 for further processing. The hydrogenation reactor 750 produces the light end product. The effluent from the hydrogenation reactor is led to the hydrogenation unit 710 for further treatment as the effluent hydrogenation feed stream 313.

[0076] The system 300 is configured such that the light stream 302 from the depressurized tower can be directed toward the hydrocracking unit 710. The hydrocracking feed stream 313 from the hydrotreatment reactor 750 can be combined with the light stream 302 from the depressurized tower in the hydrocracking unit 710. Furthermore, a hydrogen feed stream 315 consisting of hydrogen is introduced into the hydrocracking unit 710. The hydrocracking unit includes a fixed-bed catalyst, which will be described later.

[0077] In one or more embodiments, the system 100 is configured such that the hydrocracking unit 510 can convert the combined distillates, diesel fuel, and asphalten lean heavy detrecced oil under hydrocracking conditions and in the presence of excess hydrogen and a catalyst into distillates, naphtha, light end, and elimination materials. In one or more embodiments, the operating temperature of the hydrocracking unit is in the range of about 360°C to 420°C. The operating pressure of the hydrocracking unit is in the range of about 70 absolute bar (bara) to 170 bara (partial pressure of hydrogen).

[0078] The hydrocracking unit 710 may also be configured to separate the products into several product streams. The system 300 may be configured and operated so that the right-end products and excesses, and the distillate and naphtha products, exit the hydrocracking unit 710 and system 300 as a combined distillate and naphtha product stream 317 for further processing. The hydrocracking unit 710 may be further configured so that the right-end products and excess hydrogen exit the hydrocracking unit 710 and system 300 as a right-end stream 316 for further processing. The hydrocracking unit 710 may be further configured so that the waste material from the hydrocracking unit 710 exits the unit as a hydrocracking bleed stream 311, which is a system recycling stream.

[0079] In one or more embodiments, the system 300 may be configured such that the hydrocracking unit 710 can be replaced by a catalytic cracking unit. The catalytic cracking unit may be a conventional riser fluid catalytic unit or a high catalyst / oil ratio downer design.

[0080] System 300 is configured such that a hydrocracking bleed stream 311 containing unconverted oil (or unconverted oil stream) is split into two streams. A first portion 311A ​​of the hydrocracking bleed stream, for example about 80% to 100% by weight, may be sent to a high-lift solvent delamination unit 720. Before being introduced to the high-lift solvent delamination unit 720, the first portion 311A ​​of the hydrocracking bleed stream may be combined with other streams to form a high-lift solvent delamination unit feed stream 324. A second portion 311B of the hydrocracking bleed stream, for example more than 0% to about 20% by weight, may be sent to a bitumen injection unit 740 for further processing. Before being introduced to the bitumen injection unit 740, the second portion 311B of the hydrocracking bleed stream may be combined with other streams to form a bitumen injection unit feed stream 344.

[0081] In the configuration of system 300, multiple flows are combined to form a high-lift solvent deaeration unit supply flow 224. In system 300, a first portion 303A of the reduced-pressure residue flow may be combined with a first portion 311A ​​of the hydrocracking bleed flow to form a high-lift solvent deaeration unit supply flow 324. System 300 may be configured to supply the high-lift solvent deaeration unit with a combined mixture of reduced-pressure residue and recycled material from the hydrocracking unit.

[0082] The high-lift solvent delamination unit can be considered a “last resort unit” in system 300 for recycling useful fluid products back into system 300 and other units. That is, the bottom products from this unit are sent for conversion in the bitumen injection process. System 300 may be configured such that the high-lift solvent delamination unit feed stream 324 can be introduced into the high-lift solvent delamination unit 720. System 300 may be configured such that the high-lift solvent delamination unit 720 can be treated with a mixture of vacuum residue and unconverted oil in the presence of a butane solvent to produce asphaltene lean products and asphaltene rich products. The solvent (butane):oil (vacuum residue and unconverted oil) ratio may be in the range of about 5:1 in one or more embodiments.

[0083] System 300 may be combined such that a high-lift solvent delamination unit 720 can produce two products from the conversion of the high-lift solvent delamination unit feed stream, both of which are provided to other units for further processing. An asphaltene lean heavy delamination oil stream 325 may be produced as a light product. The asphaltene lean heavy delamination oil stream 325 may be divided into a first portion 325A and a second portion 325B. The first portion of the asphaltene lean heavy delamination oil stream may be about 50% to about 80% by weight of the asphaltene lean heavy delamination oil stream, for example, about 50% to about 70% by weight, or about 50% to about 60% by weight. The second portion 325B of the asphaltene lean heavy deblecking oil flow may be about 20% to about 50% by weight, for example, about 30% to about 50% by weight, or about 40% to about 50% by weight. The division between the first and second portions may vary within these ranges, taking into account the desired amount of lubricating oil produced. The first portion 325A of the asphaltene lean heavy deblecking oil flow may be directed to a low-lift solvent deblecking unit 730 for conversion. The second portion 325B of the asphaltene lean heavy deblecking oil flow may be combined with the heavy oil flow 337 to form a hydrogenation feed flow 353. An asphaltene-rich pitch flow 326 may also be formed as a bottom product. The asphaltene-rich pitch flow 326 may be directed toward a bitumen injection unit 740 for conversion.

[0084] As described above, in the configuration of system 300, a first portion 325A of the asphaltene lean heavy delamination oil stream may be introduced into a low-lift solvent delamination unit 730. The low-lift solvent delamination unit 730 is configured to combine a second portion of the reduced-pressure residue feed stream with a propane stream (as a solvent, not shown), and then separate the second portion of the reduced-pressure residue feed stream into two products. The solvent:reduced-pressure residue feed ratio may be about 8:1 in one or more embodiments.

[0085] System 300 is configured such that the low-lift solvent deflaking unit 730 can generate two product flows: a light deflaking oil product flow 336 that exits System 300 as a product, and a heavy oil flow 337 that can exit from the bottom as an excavation flow. The generated light deflaking oil is a lubricating oil base oil feedstock.

[0086] In the configuration of system 300, multiple flows can be combined to form the bitumen injection unit supply flow 344. A second portion 303B of the reduced-pressure residue flow is combined with the asphaltene-rich pitch flow 326 from the high-lift solvent delamination unit 720 and a second portion 311B of the hydrocracking bleed flow. Furthermore, a low-viscosity diesel supply flow is also introduced into system 300 and can be combined with the other three flows to form the bitumen injection unit supply flow 344.

[0087] System 300 is configured such that the bitumen injection unit supply flow 344 is introduced into the bitumen injection unit 740 and converted into bitumen and asphalt products. The bitumen and asphalt may be road grade products. The bitumen and asphalt products can exit the bitumen injection unit 740 and system 300 via the bitumen and asphalt flow 345. Process methods for using the system

[0088] In one or more embodiments, the process may include the step of introducing a feed into a system such as the system shown in Figures 1 to 3. The process may also include the step of operating the system such that fractional distillation, solvent step delamination, hydrocracking, hydrotreatment, bitumen blowing, pitch pelletization, or a combination thereof, produces one or more system products from the introduced feed.

[0089] System products that may be generated from one or more embodiments of the process include, but are not limited to, high-value fuels and feedstocks including diesel, gasoline, and naphtha; lubricating oil base oil feedstocks; and olefins including, but are not limited to, ethylene, propylene, and butene. The products generated by the system will be described further.

[0090] The process can be used for multiple bottom-of-stack upgrading projects in semi-conversion or hydroskimming refineries.

[0091] The process includes introducing a feed into a system of one or more embodiments. The feed may be straight-run vacuum residue, decomposition feed, or both straight-run and decomposition feed. The feed is introduced into a vacuum tower.

[0092] When cracked feedstock is introduced, the process can produce lubricating oil base feedstock in a limited manner, but it can also produce high-value fuels and core building block petrochemical products. To produce lubricating oil base feedstock, the amount of cracked feedstock components in the feedstock should be 15% or less, for example, less than 15%, 10% or less, or 5% or less.

[0093] The process of operating the system includes a step of fractional distillation of the input flow. The fractional distillation step includes a step of separating the feed introduced by boiling point in a vacuum column. The vacuum column may be a vacuum distillation column.

[0094] For example, the fractional distillation process includes operating the system to produce distillate, diesel fuel, and vacuum residue. The distillate may boil at a temperature of about 370°C or less. The diesel fuel may boil between about 370°C and 560°C. The vacuum residue may boil at a temperature of over 560°C. The fractional distillation process may also include combining the fractionated distillate and diesel fuel products into a single internal flow, such as a distillate and vacuum diesel fuel flow (vacuum tower diesel flow).

[0095] The process of operating the system may include sending the fractionated product (vacuum residue) to both the solvent deaeration unit and the hydrocracking unit. If a bitumen injection unit is included in the system, the process of operating the system may include sending the fractionated product (vacuum residue) to the bitumen injection unit.

[0096] In one or more embodiments, if the system includes a catalytic cracking unit instead of a hydrocracking unit, the steps of operating the system may include sending the fractionated product to a solvent de-abrasion unit and a catalytic cracking unit.

[0097] The solvent deblecking step may, in one or more embodiments, include operating the system so that a combined internal flow of reduced-pressure residue and unconverted oil (excluded flow from the hydrocracking unit) is deblecked in a high-lift solvent deblecking unit. The combined internal flow may further include heavy oil, such as bottom products from a low-lift solvent deblecking unit. High-lift solvent deblecking produces two products: asphaltene-lean heavy deblecked oil and asphaltene-rich pitch.

[0098] The solvent delamination step may include the step of operating the system so that the reduced-pressure residue is sent to a low-lift solvent delamination unit and delaminated.

[0099] The solvent debluffing step may include a step of operating the system so that asphaltene lean heavy debluffing oil is sent to a low-lift solvent debluffing unit for further debluffing.

[0100] Low-lift solvent-stage deflaking can produce two products: light deflaking oil and heavy oil flow (which may contain asphaltenes). The light deflaking oil is a system product that can be a useful lubricating oil base oil feedstock.

[0101] In one or more embodiments, the process of operating the system may include the process of producing naphtha and unconverted oil from the hydrocracking unit. The system may be operated under “naphtha mode,” in which case naphtha and unconverted oil are produced from the hydrocracking unit, and the light end production may be as high as 15-20% of the feed to the hydrocracking unit.

[0102] In one or more embodiments, a system is configured in which a catalytic cracking unit is used instead of a hydrocracking unit. In one or more embodiments, the process may include the steps of introducing a reduced-pressure residue stream into a catalytic cracking unit and operating the system so that the reduced-pressure residue stream is catalytically cracked. In one or more embodiments, the reduced-pressure residue stream may include reduced-pressure residue and asphaltene lean heavy deburring oil. System operation may produce several products from the catalytic cracking unit. The products are the same type of boiling products as those from the hydrocracking unit, except that the products from the catalytic cracking unit are more olefinic and aromatic compared to those from the hydrocracking unit. Therefore, the products from the catalytic cracking unit can be used for purposes other than those from the hydrocracking unit.

[0103] In one or more embodiments, the process may include the steps of introducing a hydrogenation feed stream into a hydrogenation reactor and operating the system so that the hydrogenation feed stream is hydrogenated. In one or more embodiments, the hydrogenation stream may include asphaltene lean heavy deflaking oil and heavy oil streams from low-lift solvent deflaking units. The hydrogen stream is led into the hydrogenation reactor. System operation may produce two products from the hydrogenation reactor. The products may include a light-end product, which is a system product, and a hydrogenated light-end product.

[0104] In one or more embodiments, the process may include the steps of introducing a bitumen injection unit feed stream into a bitumen injection unit and operating the system so that the bitumen injection unit feed stream is processed in the bitumen injection unit. The bitumen injection unit feed stream may consist of reduced-pressure residue, asphaltene-rich pitch, unconverted oil waste or recycled stream from a hydrocracking unit, and low-viscosity diesel fuel (having a viscosity in the range of about 800 to 1200 cSt). System operation may produce bitumen and asphalt from the bitumen injection unit. The bitumen and asphalt are system products, including road-grade asphalt. If a catalytic cracking unit is included instead of a hydrocracking unit, slurry oil from the catalytic cracking unit is introduced into the bitumen injection unit.

[0105] In one or more embodiments, the process may include the steps of introducing asphaltene-rich pitch into a pitch pelletizing unit and operating the system so that the asphaltene-rich pitch is processed in the pitch pelletizing unit. System operation may produce a solid fuel as a system product. The solid fuel includes pelletized or flakeped pitch.

[0106] Examples

[0107] Example 1 is described in Table 1. Table 1, together with, for example, Figure 1 (parallel solvent delamination residue oil upgrading complex including bitumen generation), shows a flow scheme that is an example of a high-level balance using one or more systems and processes according to the embodiment.

[0108] [Table 1-1]

[0109] Table 1, continued [Table 1-2]

[0110] In Table 1, "g / mL" is grams per milliliter, "wt%" is weight percentage (w / w), and "ppmw" is parts per million by weight. "cSt" is centistokes, and "dmm" is one-tenth of a millimeter (referring to the penetration depth into the surface of bitumen in the penetration test).

[0111] In Example 1, when the input flow 101 (Figure 1, feed) is 100 TPH, the asphalt flow 145 (Figure 1, bitumen residue lift) is 28.2 (approximately 28 wt%), and the generated product (other than asphalt or bitumen) is 71.78 (72 wt%) of the total feed (from the input flow). Furthermore, the total 28.7 TPH of the bitumen injection unit feed flow 144 (Figure 1) includes approximately 53 wt% reduced pressure residue (15.3 TPH), approximately 31 wt% pitch (8.89 TPH), approximately 2 wt% unconverted oil (0.46 TPH), and approximately 14 wt% diesel fuel (4 TPH).

[0112] In Example 1 (Figure 1), a distillate flow 102A that boils at less than approximately 370°C and a reduced-pressure light oil flow 102B that boils at approximately 370°C to approximately 560°C are combined to form a reduced-pressure light oil flow 102.

[0113] In Example 1, the first portion 103A of the reduced-pressure residue flow is 50% by weight of the total weight (100% by weight) of the reduced-pressure residue flow 103, the second portion 103B of the reduced-pressure residue flow is 12% by weight, and the remainder 103C of the reduced-pressure residue flow is 38% by weight; the first portion 111A of the hydrocracking bleed flow is 81% by weight of the total weight (100% by weight) of the hydrocracking bleed flow 111, and the second portion 111B of the hydrocracking bleed flow is 19% by weight.

[0114] Favorable effects

[0115] The systems and processes of one or more embodiments of this disclosure have several attributes useful to the global oil refining industry. One or more embodiments of this disclosure may provide one or more of the following advantages:

[0116] In one or more embodiments, a mixture of reduced-pressure residue and pitch (generated in the solvent de-abrasion unit) is converted into a system product. For example, bitumen and asphalt containing road-grade asphalt may be produced.

[0117] In one or more embodiments, a cascade-type solvent delamination unit is used in operation in close connection with a hydrocracking unit. Such a configuration maximizes conversion. This means that if bitumen is also produced, 60% of the residue may be converted to a lighter product, and if bitumen is not produced, the conversion rate may reach 80% (in the case of pitch production). As used herein, “cascade-type” is a method in which the residue flows in a cascade manner from one solvent delamination unit to the next, each with a different lift, thereby removing heavier molecules from the cascade and including molecules to be processed or sent as the final product.

[0118] In one or more embodiments, the closely coupled operation of hydrocracking and solvent delamination enables the removal of heavy polynuclear aromatic compounds. The removal of heavy polynuclear aromatic compounds and subsequent recycling ensure a higher conversion of heavy feedstocks compared to treatment by the hydrocracking unit alone. "High conversion" means that the hydrocracking unit can convert more than 90% of the feedstock into products that boil at temperatures below 370°C; the nominal conversion rate in the hydrocracking unit may be greater than 90%, for example, 91%, 92%, 93%, 94%, 95%, 96%, 97%, or 98%.

[0119] In one or more embodiments, high-value fuels, lubricating oil base oil feedstocks, and petrochemical building blocks are produced as system products. While we do not wish to be bound by theory, if a conventional system different from the flow scheme (system) of one or more embodiments is used, the conventional system may produce high-value fuels but will be more expensive and not economically viable compared to the flow scheme of one or more embodiments.

[0120] In one or more embodiments, the process of operating the system includes the process of converting both straight-run vacuum residue or cracked raw materials (residual oil) to high-efficiency oil to produce both fuel and lubricating oil.

[0121] In one or more embodiments, the ability to remove heavy polynuclear aromatic compounds through a solvent delamination system enables high conversion of the hydrocracking unit and, if possible, the generation of bitumen.

[0122] definition

[0123] The term "flow" or "stream" may include various hydrocarbons such as linear, branched, or cyclic alkanes, alkenes, alkadienes, alkynes, and aromatic compounds, as well as other substances such as gases and impurities. A flow or stream may include combinations of aromatic and non-aromatic compounds.

[0124] The term "zone" may refer to an area containing one or more pieces of equipment or one or more subzones. Equipment includes one or more reactors or reaction vessels, heaters, exchangers, pipes, pumps, compressors, and controllers. Furthermore, equipment such as reactor dryers or vessels may further comprise one or more zones.

[0125] The term "true boiling point" refers to the boiling point of a substance as defined by ASTM D2892. ASTM D2892 is a test method for determining the boiling point of a substance for the production of standardized quality liquefied gas, distillates, and residues from which analytical data can be obtained, and for determining the yield of the above distillates by both mass and volume, thereby creating a temperature vs. distillate mass% graph using 15 theoretical stages in a column with a reflux ratio of 5:1.

[0126] The term "white oil" refers to hydrocarbon products having a true boiling point (endpoint) below approximately 370°C. This may include, but is not limited to, hydrocarbons in liquefied petroleum gas, as well as naphtha and distillates.

[0127] The term "distillate" refers to hydrocarbons having a true boiling point range of 150–370°C. This may include, but is not limited to, kerosene and diesel products.

[0128] The term "residual oil" refers to hydrocarbons that have a true boiling point above 370°C and are feedstocks for vacuum distillation columns.

[0129] The term "diesel fuel" refers to hydrocarbons having a true boiling point range of 370–560°C. This may include, but is not limited to, diesel fuel obtained as a side cut from a vacuum distillation column in a fractional distillation section.

[0130] The term "vacuum residue" (or "vacuum residue") refers to hydrocarbons that have a true boiling point above 560°C and are obtained as bottom flow after flushing lighter components from the fuel oil flow.

[0131] The term "pitch" refers to the asphaltene-rich flow from a high-lift solvent delamination unit.

[0132] The term "asphaltene" can refer to heavy polar fractions, but is the residue remaining after the resin and oil have been separated from the feed residue supplied to the solvent de-abrasion unit. One or more embodiments of Conradson carbon and metals (contaminants) are described below, along with the hydrogen / carbon ratio (H / C) and the concentrations of metals and other components. Asphaltene derived from vacuum residue is generally characterized by having 15–90% by weight of Conradson or Ramsbottom residual carbon and a hydrogen / carbon (H / C) atomic mass ratio of 0.5–1.5 (by mass). Asphaltene may contain vanadium in amounts of 50 ppm to over 5000 ppm and nickel in amounts of 20 ppm to over 2000 ppm. The sulfur concentration of asphaltene may be in the range of 110% to 350% by weight higher than the sulfur concentration in the vacuum residue oil supply oil to the de-abrasion unit. The nitrogen concentration in asphaltene can be 100% to 350% by weight higher than the nitrogen concentration in the residue oil supplied to the de-bagging unit.

[0133] The term "resin oil" refers to the aromatic polar fraction, an intermediate between asphaltene (pitch) and delamination oil, separated from the feed residue to the delamination unit. Resin may be denser or heavier than delamination oil, but lighter than asphaltene. Resin products may contain aromatic hydrocarbons with aliphatic substituted side chains, and may also contain metals such as nickel and vanadium.

[0134] The term "deburring oil" generally refers to the lowest density product generated in a deburring unit, containing saturated aliphatic hydrocarbons, alicyclic hydrocarbons, and some aromatic hydrocarbons. Deburring oil may contain less than 30% by weight of aromatic carbon and less than 10% of relatively low levels of non-sulfur heteroatoms, e.g., less than 10% by weight of heteroatoms. Deburring oil derived from vacuum residue can generally be characterized as having less than 1-12% by weight of Conradson or Ramsbottom residual carbon and a hydrogen / carbon (H / C) atomic mass ratio of 1.0-2 (by mass). Deburring oil may contain less than 100 ppm of vanadium, e.g., less than 5 ppm, less than 5 ppm, less than 2 ppm, or less than 2 ppm. Deburring oil may contain less than 100 ppm of nickel, e.g., less than 5 ppm, less than 5 ppm, less than 2 ppm, or less than 2 ppm. The sulfur and nitrogen concentrations in the deburred oil may be 90% by weight or less of the sulfur and nitrogen concentrations in the residual oil supplied to the deburred unit.

[0135] The term "heavy deburring oil" refers to a mixture of resin and deburring oil typically produced from a solvent deburring unit using a heavy solvent (butane or a heavier molecular weight hydrocarbon) when the lift (amount of deburring oil produced) exceeds 60% (based on the weight of the reduced-pressure residue feed).

[0136] The term "light deburring oil" refers to deburring oil typically produced from a solvent deburring unit using a light solvent (such as propane) when the lift (amount of deburring oil produced) is less than 40% (based on the weight of the feed to the solvent deburring unit).

[0137] The term "hydrocracking unit" refers to a fixed-bed catalytic process unit used to convert distillates, diesel fuel ranges, and defractions into white oil products that maximize either naphtha or ultra-low sulfur diesel. The hydrocracking process is carried out at a reaction temperature range of 360°C to 420°C and a reaction pressure range of 70 bara to 170 bara (hydrogen partial pressure). Conversion rates in the hydrocracking zone can range from 50 to 98%; the liquid space velocity is 0.5 to 3 / hour (hr). -1 ) may be. In one or more embodiments, the conversion rate is expected to be about 95% in a two-stage unit configuration. The catalyst in the hydrocracking unit is a heterogeneous fixed-bed catalyst comprising one or more group VIII metals and one or more group VIB metals. The group VIII metals are one or more selected from the group consisting of iron, cobalt, and nickel. The group VIB metals are one or more selected from the group consisting of molybdenum and tungsten. The group VIII metals may be present in an amount of about 2 to 20% by weight, and the group VIB metals may be present in an amount of about 1 to 25% by weight. Generally, these metals are contained on a carrier material such as silica, alumina, or a combination thereof. Additional acidity in the form of zeolite may be present for the hydrocracking catalyst or accelerator, such as a group XV oxide. The group XV oxide may be present for the residue conversion and hydrotreatment catalyst. In one or more embodiments, the hydrocracking unit is a two-stage hydrocracking configuration. This can be beneficial for conversion efficiency and supply quality.

[0138] The term "solvent delamination unit" refers to a liquid-liquid extraction unit utilizing a C3 / C4 / C5 solvent to produce a lighter cut of delamination oil and resin (if produced) from a heavy feed from which asphaltene has been removed in a pitch flow as a reduced-pressure residue or asphaltene-rich pitch flow. The solvent / oil ratio in the solvent delamination unit is 3:1 to 8:1, and the operation of the solvent delamination unit is under either the subcritical or supercritical pressure and temperature range of the solvent used. The lift (amount of delamination oil and resin produced, if produced) is in the range of 30% to 80% by weight of the (residue) feed; optimally less than 70% by weight.

[0139] The term "pitch pelletizing unit" refers to a unit in which pitch from a solvent delamination unit is pelletized or flakebed to produce a solid that can be used as fuel for combustion or gasification.

[0140] The term "vacuum distillation column" refers to a vacuum distillation column that processes atmospheric pressure residue (hydrocarbons that boil above 370°C from a crude oil distillation unit), which operates at a pressure below atmospheric pressure (typically in the range of approximately 25 millimeters of mercury (mmHg) to approximately 100 mmHg in the flash zone, with an operating temperature of approximately 300°C to approximately 500°C in the flash zone), and produces diesel fuel products (which boil below 560°C, with the residue boiling above 560°C).

[0141] Fluid coupling of the main liquid products is shown in one or more embodiments, while other flows (hydrocarbons and others according to the process flow scheme) are not shown in one or more embodiments, but their inclusion can be understood by those skilled in the art.

[0142] The term "major" may mean that the compound or group of compounds in the flow constitutes about 50% by weight, for example, about 80% by weight.

[0143] The term "substantially" may mean that the compound or group of compounds in the flow constitutes about 80 mol%, for example, about 90 mol%, or about 99 mol%.

[0144] As used herein and in the appended claims, the words “comprise,” “has,” and “include,” and their grammatical variations, are intended to have an open and non-restrictive meaning that does not exclude additional elements or processes.

[0145] "Optionally" means that the event or situation described thereafter may or may not occur. This description includes both cases in which the event or situation occurs and cases in which it does not occur.

[0146] When the words "approximately" or "about" are used, this term may mean that the value may vary by up to ±10%, up to 5%, up to 2%, up to 1%, up to 0.5%, up to 0.1%, or up to 0.01%.

[0147] A range can be expressed as an approximate range from one specific value to another specific value, including those values. When such a range is expressed, it should be understood that another one or more embodiments are from one specific value to another specific value, along with all specific values ​​and combinations thereof within that range.

[0148] Note that one or more of the following claims utilize the term “where” or “in which” as a transitional clause. Note that for the purposes of defining the Art, this term is introduced into the claim as an open-ended transitional clause used to introduce a description of a set of structural features and should be interpreted similarly to the more commonly used open-ended preamble term “comprising.” For the purposes of defining the Art, the transitional clause “consisting of” may be introduced into the claim as a closed preamble term limiting the scope of the claim to the described components or processes and any naturally occurring impurities. For the purposes of defining the Art, the transitional clause “consisting essentially of” may be introduced into the claim to limit the scope of one or more claims to the described elements, components, substances, or process steps, and any undescribed elements, components, substances, or process steps that do not substantially affect the novel features of the subject matter of the claim. Since the transitional phrases "consisting of" and "consisting essentially of" can be interpreted as a subset of open-ended transitional phrases such as "comprising" and "including," any use of an open-ended phrase to introduce a description of a set of elements, components, substances, or processes should also be interpreted as disclosing a description of the same set of elements, components, substances, or processes using the closed terms "consisting of" and "consisting essentially of." For example, a description of a composition "comprising" components A, B, and C should also be interpreted as disclosing a composition "consisting of" components A, B, and C, as well as a composition "consisting essentially of" components A, B, and C.Any quantitative values ​​expressed in this application may be interpreted as including open-ended embodiments corresponding to the transitional phrases “comprising” or “including,” and closed or partially closed embodiments corresponding to the transitional phrases “consisting of” and “consisting essentially of.” The words “comprise,” “has,” and “include,” and their grammatical variations, are intended to have an open and non-restrictive meaning that does not exclude additional elements or steps.

[0149] While one or more embodiments of this disclosure have been described with respect to a limited number of embodiments, those skilled in the art who benefit from this disclosure will understand that other embodiments can be devised that do not deviate from the scope of this disclosure. Therefore, the scope of this disclosure should be limited only by the appended claims.

Claims

1. A system that upgrades the input flow, Decompression tower and; A hydrocracking unit connected downstream of the above-mentioned depressurization tower and in fluid communication with the above-mentioned depressurization tower; A high-lift solvent delamination unit is connected downstream of the above-mentioned vacuum tower and is in fluid communication with the above-mentioned vacuum tower; A low-lift solvent delamination unit is connected downstream of the above-mentioned vacuum tower and is in fluid communication with the above-mentioned vacuum tower; It includes a bitumen injection unit connected downstream of the above-mentioned vacuum tower and the above-mentioned high-lift solvent delamination unit, and in fluid communication with the above-mentioned vacuum tower and the above-mentioned high-lift solvent delamination unit, The above-mentioned depressurization tower is configured to receive the input flow of straight-run atmospheric pressure residue or decomposition feed material, and to separate the input flow into a depressurization tower light flow and a depressurization residue flow. The above-mentioned hydrocracking unit is configured to receive the combined flow of the light flow and heavy detrace oil flow from the vacuum tower, as well as the hydrogen flow, and to deliver the distillate, naphtha products, and light end products. The above heavy de-abrasive oil flow is in fluid communication with the above hydrocracking unit and further with the above high-lift solvent de-abrasive unit. The high-lift solvent delamination unit is configured to receive the butane flow, the first portion of the reduced-pressure residue flow, the first portion of the hydrocracking bleed flow, and the heavy oil flow, and to deliver the asphaltene lean heavy delamination oil flow and the asphaltene rich pitch flow, and the unconverted oil flow is in fluid communication with the hydrocracking unit, the high-lift solvent delamination unit, and the bitumen injection unit. The low-lift solvent de-abrasion unit described above is configured to receive the propane flow and the second portion of the reduced-pressure residue flow, and to deliver the light de-abrasion oil and heavy oil flow, which are the raw materials for supplying the lubricating oil base oil. The above heavy oil flow is in fluid communication with the above high-lift solvent delamination unit. The bitumen injection unit described above is configured to receive the combined flow of the second portion of the hydrocracking bleed flow, the remainder of the reduced-pressure residue flow, and the low-viscosity diesel flow, and to deliver the bitumen and asphalt flow. The above low-viscosity diesel fuel flow is in fluid communication with the above bitumen injection unit. A system in which the above-mentioned reduced-pressure residue flow is in parallel with the above-mentioned high-lift solvent delamination unit, the above-mentioned low-lift solvent delamination unit, and the above-mentioned bitumen injection unit.

2. The system according to claim 1, wherein the first portion of the reduced pressure residue flow is in the range of 40% to 60% by weight of the reduced pressure residue flow, the second portion of the reduced pressure residue flow is in the range of 5% to 15% by weight of the reduced pressure residue flow, and the remainder of the reduced pressure residue flow is in the range of 25% to 45% by weight of the reduced pressure residue flow.

3. The system according to claim 1 or 2, wherein the first portion of the hydrocracking bleed flow is in the range of 80% to 100% by weight of the unconverted oil flow, and the second portion of the hydrocracking bleed flow is in the range of more than 0% to 20% by weight of the unconverted oil flow.

4. The system according to claim 1 or 2, wherein the light flow of the depressurized tower contains hydrocarbons that boil at a temperature of 560°C or less, and the depressurized residue flow contains hydrocarbons that boil at a temperature of over 560°C.

5. The combined flow of the above-mentioned reduced-pressure residue flow, the above-mentioned unconverted oil flow, and the above-mentioned heavy oil flow forms a combined reduced-pressure residue, unconverted oil, and heavy oil. The system according to claim 1 or 2, wherein the high-lift solvent delamination unit is further configured to receive butane in a 5:1 ratio, the combined reduced-pressure residue, unconverted oil, and heavy oil.

6. The system according to claim 1, wherein the low-lift solvent delamination unit is further configured to receive propane:reduced pressure residue in an 8:1 ratio.

7. The system according to claim 1 or 2, wherein the bitumen injection unit supply flow has a viscosity of 800 to 1200 centistokes.

8. A system that upgrades the input flow, The input flow of straight-run atmospheric pressure residue or decomposition feed material; Decompression tower and; A hydrocracking unit connected downstream of the above-mentioned depressurization tower and in fluid communication with the above-mentioned depressurization tower; A high-lift solvent delamination unit is connected downstream of the above-mentioned vacuum tower and is in fluid communication with the above-mentioned vacuum tower; A low-lift solvent delamination unit is connected downstream of the above-mentioned vacuum tower and is in fluid communication with the above-mentioned vacuum tower; It includes a pitch pelletizing unit connected downstream of the high-lift solvent delamination unit and in fluid communication with the high-lift solvent delamination unit, The above-mentioned depressurization tower is configured to receive the above-mentioned input flow and separate the above-mentioned input flow into a depressurization tower light flow and a depressurization residue flow. The above-mentioned hydrocracking unit is configured to receive the combined flow of the light flow and heavy detrace oil flow from the vacuum tower, as well as the hydrogen flow, and to deliver the distillate, naphtha products, and light end products. The above heavy de-abrasive oil flow is in fluid communication with the above hydrocracking unit and further with the above high-lift solvent de-abrasive unit. The above-mentioned high-lift solvent de-abrasion unit is configured to receive a combined flow of butane, the first portion of the above-mentioned reduced-pressure residue flow, the unconverted oil flow as a hydrocracking bleed flow, and the heavy oil flow, and to deliver an asphaltene lean heavy de-abrasion oil flow and an asphaltene rich pitch flow. The above unconverted oil flow is in fluid communication with the above hydrocracking unit and the above high-lift solvent delamination unit. The low-lift solvent de-abrasion unit described above is configured to receive the combined flow of the propane flow and the second portion of the reduced-pressure residue flow, and to deliver the light de-abrasion oil and heavy oil flow, which are the raw materials for supplying the lubricating oil base oil. The above heavy oil flow is in fluid communication with the above high-lift solvent delamination unit. The pitch pelletizing unit described above is configured to receive an asphaltene-rich pitch flow and to deliver solid fuel. The above asphaltene-rich pitch flow is in fluid communication with the above high-lift solvent delamination unit and the above pitch pelletization unit. A system in which the above-mentioned reduced-pressure residue flow is in parallel with the above-mentioned high-lift solvent delamination unit and the above-mentioned low-lift solvent delamination unit.

9. The system according to claim 8, wherein the first portion of the reduced pressure residue flow is 70% to 90% by weight of the reduced pressure residue flow, and the second portion of the reduced pressure residue flow is 10% to 30% by weight of the reduced pressure residue flow.

10. The system according to claim 8 or 9, wherein the light flow of the depressurized tower contains hydrocarbons that boil at a temperature of 560°C or less, and the depressurized residue flow contains hydrocarbons that boil at a temperature of over 560°C.

11. The combined flow of the above-mentioned reduced-pressure residue flow, the above-mentioned unconverted oil flow, and the above-mentioned heavy oil flow forms a combined reduced-pressure residue, unconverted oil, and heavy oil. The system according to claim 8 or 9, wherein the high-lift solvent delamination unit is further configured to receive butane in a 5:1 ratio: the combined reduced-pressure residue, unconverted oil, and heavy oil.

12. The system according to claim 8 or 9, wherein the low-lift solvent delamination unit is further configured to receive propane:reduced pressure residue in an 8:1 ratio.

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