SEPARATION

RELATED APPLICATIONS

[01] This application claims the benefit of priority of U.S. Provisional Patent Application Nos. 61/613,332 filed March 20, 2012 and 61/792,822 filed March 15, 2013, which are incorporated by reference herein.

BACKGROUND OF THE INVENTION

Field of the Invention

[02] The present invention relates to an improved steam cracking process and system.

Description of Related Art

[03] Steam cracking processes typically involve two main sections, the convection and pyrolysis section. The convection section of the steam pyrolysis cracking zone is used to heat the feed to the required reaction temperatures, often called the cross-over temperature, prior to entering the steam pyrolysis cracking unit, wherein the pyrolysis cracking reaction occurs. Steam pyrolysis cracking reactions typically convert a relatively heavy hydrocarbon feedstock, which may include of a wide range of hydrocarbon components, into lighter, and more desirable, hydrocarbons, including but not limited to ethylene, propylene, butadiene, mixed butenes and pyrolysis gasoline.

[04] Steam pyrolysis is a useful process that utilizes Le Chatelier's principle to create a more favorable reaction environment. The reactions that occur within a steam cracking process have more molecules on the product side of the equilibrium. Such reactions proceed to the more desirable product side when the reaction is performed under low pressure, as is stated by Le Chatelier's principle. The reaction normally occurs at atmospheric pressure; and running the cracking reaction at conditions lower then atmospheric pressures can be very uneconomical.

Other conventional processes utilize a catalyst instead of steam to lower the activation energy and therefore create more desired products. However, in steam pyrolysis processes the addition of a low molecular weight diluent, steam is utilized. The addition of the low molecular weight steam to the cracking reaction lowers the partial pressure of the reaction system and creates more favorable reaction conditions and therefore increased desired products are formed.

[05] Therefore it is an object of the present invention to provide improved steam cracking process and systems.

SUMMARY OF THE INVENTION

[06] The system and process herein provides an integrated vapor-liquid separation device in conjunction with a steam pyrolysis cracking unit operation. In certain aspects, a feed is charged to the inlet of a convection portion of a steam pyrolysis unit where the feed is heated to conditions effective for steam cracking. The convection section effluent is separated in a vapor- liquid separator and the separator vapor effluent is charged to the inlet steam cracking portion of the steam pyrolysis zone. The liquid effluent can be further processed, recycled within the system or a combination thereof. In additional aspects, a feed separated upstream of the convection portion of a steam pyrolysis unit using a flash vessel equipped with a vapor-liquid separator device described herein.

[07] Other aspects, embodiments, and advantages of the process of the present invention are discussed in detail below. Moreover, it is to be understood that both the foregoing information and the following detailed description are merely illustrative examples of various aspects and embodiments, and are intended to provide an overview or framework for understanding the nature and character of the claimed features and embodiments. The accompanying drawings are illustrative and are provided to further the understanding of the various aspects and embodiments of the process of the inventionA

BRIEF DESCRIPTION OF THE DRAWINGS

[08] The invention will be described in further detail below and with reference to the attached drawings where:

[09] FIG.1 is a process flow diagram of an embodiment of a steam cracking process with an integrated vapor-liquid separation zone between the convection and pyrolysis sections; and

[10] FIG. 2 is an embodiment of a steam cracking process with an integrated vapor-liquid separation zone upstream of the convection section and prior to the steam cracking process; and

[11] FIG. 3 is an embodiment of a steam cracking process with an integrated vapor liquid separation zone upstream of the convection section of the steam cracking process and integrated vapor-liquid separation within the steam cracking process;

[12] FIGs. 4A-4C are schematic illustrations in perspective, top and side views of a vapor- liquid separation device used in certain embodiments of a steam cracking unit operation and process described herein; and

[13] FIGs. 5A-5C are schematic illustrations in section, enlarged section and top section views of a vapor-liquid separation device in a flash vessel used in certain embodiments of a steam cracking unit operation and process described herein.

DEATILED DESCRIPTION OF THE INVENTION

[14] A process flow diagram for one embodiment of a steam cracking process with an integrated vapor-liquid separation is shown in FIG.1. The integrated system generally includes a convection section and a steam pyrolysis section, with a vapor-liquid separation zone between the convection and pyrolysis sections. [15] Steam pyrolysis zone 10 generally comprises a convection section 6 and a pyrolysis section 8 that can operate based on steam pyrolysis unit operations known in the art, i.e., charging the thermal cracking feed to the convection section in the presence of steam. In addition, as shown in FIG 1 a vapor-liquid separation section 7 is included between sections 6 and 8. Vapor-liquid separation section 7, through which the heated steam cracking feed from convection section 6 passes, can be a separation device based on physical or mechanical properties of vapors and liquids.

[16] In certain embodiments, vapor-liquid separation devices are illustrated by, and with reference to FIGs. 4A-4C and 5A-5C. A similar arrangement of a vapor-liquid separation device is also described in U.S. Patent Publication Number 2011/0247500 which is incorporated by reference in its entirety herein. In these devices vapor and liquid flow though in a cyclonic geometry whereby the device operates isothermally and at very low residence time (in certain embodiments less than 10 seconds), and with a relatively low pressure drop (in certain embodiments less than 0.5 bars). In general vapor is swirled in a circular pattern to create forces where heavier droplets and liquid are captured and channeled through to a liquid outlet, while the vapors are sent for further processing in the steam pyrolysis section 9.

[17] As shown in FIG. l steam pyrolysis zone 10 operates under parameters effective to crack feed 1, into the desired products. In certain embodiments, steam cracking is carried out using the following conditions: a temperature in the range of from 400°C to 900°C in the convection section and in the pyrolysis section; a steam-to-hydrocarbon ratio in the convection section in the range of from 0.3 : 1 to 2: 1; and a residence time in the convection section and in the pyrolysis section in the range of from 0.05 seconds to 2 seconds. [18] In another embodiment shown with respect to FIG. 2, a vapor-liquid separator 9 is included upstream of steam pyrolysis zone 10, through which feed 1 is charged. Vapor-liquid separator 9 shown in FIG. 2 can be a flash separation device including a separations device based on physical or mechanical separation of vapors and liquids, which is seen in FIGs. 4A-4C, or a combination including at least one of these types of devices (e.g. shown in FIGs. 5A-5C in which the inlet of a flash vessel includes a device based on physical or mechanical separation of vapors and liquids). The vapor phase effluent, stream la, of this separation section 9 is the feed to the steam pyrolysis zone 10, where in the convection section 6 the separated effluent is heating to temperatures effective to undergo steam cracking. The heated effluent is charged to the inlet of steam pyrolysis section 8, where steam can be added in effective quantities to crack the feed and produce a mixed product stream. The vaporization temperature and fluid velocity are varied to adjust the approximate temperature cutoff point, for instance in certain embodiments in the range of about 350°C to about 600°C for compatibility with residue blends and/or processing operations.

[19] A further embodiment is shown in FIG. 3, where a vapor-liquid separator 9 is included upstream of steam pyrolysis zone 10, through which feed 1 is charged to and is fractioned. The vapor phase effluent, stream la, of separation section 9, is the feed to the steam pyrolysis zone 10. In the convection section 6 the separated effluent is heating to temperatures effective to undergo steam cracking. The heated effluent is charged to the inlet of a vapor-liquid separation device 7 for further separation. The vapor phase effluent of the vapor-liquid separation device 7 is sent to the inlet of steam pyrolysis section 8 where steam is added in effective quantities to crack the feed and produce a mixed product stream. [20] In the embodiments of FIGs. 1-3, a quenching zone 11 is typically integrated downstream of the steam pyro lysis cracking zone 10 and includes an inlet in fluid communication with the outlet of steam pyrolysis cracking zone 10 for receiving mixed product stream 4. The mixed product is quickly quenched in quenching zone 11 to stop the pyrolysis reaction and a quenched effluent 5 exits.

[21] In certain embodiments, the vapor-liquid separation section 7 includes one or a plurality of vapor liquid separation devices 80 as shown in FIGs. 4A-4C. The vapor liquid separation device 80 is economical to operate and maintenance free since it does not require power or chemical supplies. In general, device 80 comprises three ports including an inlet port 82 for receiving a vapor4iquid mixture, a vapor outlet port 84 and a liquid outlet port 86 for discharging and the collection of the separated vapor and liquid, respectively. Device 80 operates based on a combination of phenomena including conversion of the linear velocity of the incoming mixture into a rotational velocity by the global flow pre-rotational section, a controlled centrifugal effect to pre-separate the vapor from liquid, and a cyclonic effect to promote separation of vapor from the liquid. To attain these effects, device 80 includes a pre-rotational section 88, a controlled cyclonic vertical section 90 and a liquid collector/settling section 92.

[22] As shown in FIG. 4B, the pre-rotational section 88 includes a controlled pre-rotational element between cross-section (SI) and cross-section (S2), and a connection element to the controlled cyclonic vertical section 90 and located between cross-section (S2) and cross-section (S3). The vapor liquid mixture coming from inlet 82 having a diameter (Dl) enters the apparatus tangentially at the cross-section (SI). The area of the entry section (SI) for the incoming flow is at least 10% of the area of the inlet 82 according to the following equation:

ST * ¹ _D 1 } _ ^~

(1) [23] The pre-rotational element 88 defines a curvilinear flow path, and is characterized by constant, decreasing or increasing cross-section from the inlet cross-section SI to the outlet cross-section S2. The ratio between outlet cross-section from controlled pre-rotational element (S2) and the inlet cross-section (SI) is in certain embodiments in the range of 0.7 < S2/S1 < 1.4.

[24] The rotational velocity of the mixture is dependent on the radius of curvature (Rl) of the center-line of the pre-rotational element 88 where the center-line is defined as a curvilinear line joining all the center points of successive cross-sectional surfaces of the pre-rotational element 88. In certain embodiments the radius of curvature (Rl) is in the range of 2< R1/D1<6 with opening angle in the range of 150° < aRl < 250°.

[25] The cross-sectional shape at the inlet section SI, although depicted as generally square, can be a rectangle, a rounded rectangle, a circle, an oval, or other rectilinear, curvilinear or a combination of the aforementioned shapes. In certain embodiments, the shape of the cross- section along the curvilinear path of the pre-rotational element 38 through which the fluid passes progressively changes, for instance, from a generally square shape to a rectangular shape. The progressively changing cross-section of element 88 into a rectangular shape advantageously maximizes the opening area, thus allowing the gas to separate from the liquid mixture at an early stage and to attain a uniform velocity profile and minimize shear stresses in the fluid flow.

[26] The fluid flow from the controlled pre-rotational element 88 from cross-section (S2) passes section (S3) through the connection element to the controlled cyclonic vertical section 90. The connection element includes an opening region that is open and connected to, or integral with, an inlet in the controlled cyclonic vertical section 90. The fluid flow enters the controlled cyclonic vertical section 90 at a high rotational velocity to generate the cyclonic effect. The ratio between connection element outlet cross-section (S3) and inlet cross-section (S2) in certain embodiments is in the range of 2 <S 3/S1 < 5.

[27] The mixture at a high rotational velocity enters the cyclonic vertical section 90. Kinetic energy is decreased and the vapor separates from the liquid under the cyclonic effect. Cyclones form in the upper level 90a and the lower level 90b of the cyclonic vertical section 90. In the upper level 90a, the mixture is characterized by a high concentration of vapor, while in the lower level 90b the mixture is characterized by a high concentration of liquid.

[28] In certain embodiments, the internal diameter D2 of the cyclonic vertical section 90 is within the range of 2 < D2/D1< 5 and can be constant along its height, the length (LU) of the upper portion 90a is in the range of 1.2 <LU/D2 < 3, and the length (LL) of the lower portion 90b is in the range of 2 < LL/D2 < 5.

[29] The end of the cyclonic vertical section 90 proximate vapor outlet 84 is connected to a partially open release riser and connected to the pyrolysis section of the steam pyrolysis unit. The diameter (DV) of the partially open release is in certain embodiments in the range of 0.05 < DV/D2 < 0.4.

[30] Accordingly, in certain embodiments, and depending on the properties of the incoming mixture, a large volume fraction of the vapor therein exits device 80 from the outlet 84 through the partially open release pipe with a diameter (DV). The liquid phase with a low or non-existent vapor concentration exits through a bottom portion of the cyclonic vertical section 90 having a cross-sectional area S4, and is collected in the liquid collector and settling pipe 92.

[31] The connection area between the cyclonic vertical section 90 and the liquid collector and settling pipe 92 has an angle in certain embodiment of 90°. In certain embodiments the internal diameter of the liquid collector and settling pipe 92 is in the range of 2 < D3/D1 < 4 and is constant across the pipe length, and the length (LH) of the liquid collector and settling pipe 92 is in the range of 1.2 < LH/D3 <5. The liquid with low vapor volume fraction is removed from the apparatus through pipe 86 having a diameter (DL), which in certain embodiments is in the range of 0.05 <DL/D3 < 0.4 and located at the bottom or proximate the bottom of the settling pipe. In certain embodiments, a vapor-liquid separation device is provided similar in operation and structure to device 80 without the liquid collector and settling pipe return portion. For instance, a vapor-liquid separation device 180 is used as inlet portion of a flash vessel 179, as shown in FIGs 5A-5C. In these embodiments the bottom of the vessel 179 serves as a collection and settling zone for the recovered liquid portion from device 180.

[32] In general a vapor phase is discharged through the top 194 of the flash vessel 179 and the liquid phase is recovered from the bottom 196 of the flash vessel 179. The vapor-liquid separation device 180 is economical to operate and maintenance free since it does not require power or chemical supplies. Device 180 comprises three ports including an inlet port 182 for receiving a vapor-liquid mixture, a vapor outlet port 184 for discharging separated vapor and a liquid outlet port 186 for discharging separated liquid. Device 180 operates based on a combination of phenomena including conversion of the linear velocity of the incoming mixture into a rotational velocity by the global flow pre-rotational section, a controlled centrifugal effect to pre-separate the vapor from liquid, and a cyclonic effect to promote separation of vapor from the liquid. To attain these effects, device 180 includes a pre-rotational section 188 and a controlled cyclonic vertical section 190 having an upper portion 190a and a lower portion 190b. The vapor portion having low liquid volume fraction is discharged through the vapor outlet port 184 having a diameter (DV). Upper portion 190a which is partially or totally open and has an internal diameter (DII) in certain embodiments in the range of 0.5<DV/DII<1.3. The liquid portion with low vapor volume fraction is discharged from liquid port 186 having an internal diameter (DL) in certain embodiments in the range of 0.1<DL/DII<1.1. The liquid portion is collected and discharged from the bottom of flash vessel 179.

[33] In order to enhance and to control phase separation, heating steam can be used in the vapor-liquid separation device 80 or 180, particularly when used as a standalone apparatus or is integrated within the inlet of a flash vessel.

[34] While the various members of the vapor-liquid separation devices are described separately and with separate portions, it will be understood by one of ordinary skill in the art that apparatus 80 or apparatus 180 can be formed as a monolithic structure, e.g., it can be cast or molded, or it can be assembled from separate parts, e.g., by welding or otherwise attaching separate components together which may or may not correspond precisely to the members and portions described herein.

[35] The vapor-liquid separation devices described herein can be designed to accommodate a certain flow rate and composition to achieve desired separation, e.g., at 540°C. In one example, for a total flow rate of 2002 mVday at 540°C and 2.6 bar, and a flow composition at the inlet of 7% liquid, 38% vapor and 55% steam with a density of 729.5 kg/m ³ , 7.62 kg/ m ³ and 0.6941 kg/m ³ , respectively, suitable dimensions for device 80 (in the absence of a flash vessel) includes Dl =5.25 cm ; SI =37.2 cm ² ; S1=S2=37.2 cm ² ; S3= 100 cm ² ; oRl =213°; Rl = 14.5 cm; D2= 20.3 cm; LU=27 cm; LL= 38 cm; LH= 34 cm; DL= 5.25 cm; DV= 1.6 cm; and D3= 20.3 cm. For the same flow rate and characteristics, a device 180 used in a flash vessel includes Dl= 5.25 cm; DV = 20.3 cm; DL= 6 cm; and DII= 20.3 cm. [36] It will be appreciated that although various dimensions are set forth as diameters, these values can also be equivalent effective diameters in embodiments in which the components parts are not cylindrical.

[37] The feedstock can be any feed conventionally used in feedstock to a steam cracking unit. In certain additional embodiments herein, a range of additional feeds can be charged to the steam cracking unit due to the advantageous effects of the vapor-liquid separation device(s) described herein.

[38] Residuals from the upstream and/or intermediate separator in the steam cracking process described herein can be further processed in a secondary operation, for instance a conventional unit operation including but not limited to solvent deasphalting, slurry hydroprocessing. Fluid Catalytic Cracking (FCC), coker processing, or a combination comprising one or more of the foregoing. One or more product or residual streams from these secondary operations can be recycled as complementary steam cracking feed and/or further upstream of the steam cracking unit described herein.

[39] The use of the vapor-liquid separator either between the convection and pyrolysis sections, or upstream of the convection section, provides an economical and effective means to separate the intermediate product or feed to enhance certain steam cracking operations. The vapor-liquid separation device is maintenance free since it does not have moving parts, or require power or chemical supplies.

[40] The method and system of the present invention have been described above and in the attached drawings; however, modifications will be apparent to those of ordinary skill in the art and the scope of protection for the invention is to be defined by the claims that follow.