Patent Application
20130172650
None.
Embodiments of the invention relate to olefin conversion at a first temperature followed by product recovery at a second temperature higher than the first temperature.
Fuel gas at refineries contains methane, hydrogen and light olefins, such as ethylene and propylene. The light olefins often provide more value if utilized for other purposes than burning as a constituent of the fuel gas. Exemplary prior applications include use of the propylene for feedstock in alkylation units to produce high-octane gasoline blend and use of the ethylene for making polymers.
However, these applications require separation of the ethylene and propylene that often each make up less than 20% of the fuel gas. Expensive cryogenic separations thus limit the value realized for the light olefins within the fuel gas. Further, some refineries due to distance from plastic manufacturing facilities lack a market for the ethylene.
Various catalysts exist for oligomerization of the light olefins into upgraded products. Previous techniques employed with these catalysts for the oligomerization rely on pure olefin feeds, solvent diluents and/or undesired operating conditions. The techniques fail to provide a viable solution for generating desired products using the fuel gas as feed and at limited pressure and temperature.
Therefore, a need exists for a method of upgrading light olefins into more valuable products.
For some embodiments, a method of upgrading light olefins includes passing a feed stream containing the olefins with each between two and five carbons into contact at a first temperature with an oligomerization catalyst to form oligomers of the olefins. The method further includes recovering the oligomers by heating the catalyst to a second temperature higher than the first temperature. The heating releases from the catalyst the oligomers adsorbed on the catalyst when the catalyst and the olefins are contacted at the first temperature.
According to some embodiments, a method of upgrading light olefins includes contacting an oligomerization catalyst formed of at least one of chromium and nickel on a solid support with a fuel gas containing greater than 15% by volume methane and less than 75% by volume of the olefins that are at least one of ethylene, propylene and butylenes. The contacting at a pressure below 1400 kilopascals and at a first temperature between 20° C. and 300° C. produces oligomers that are formed of the olefins and adsorbed on the catalyst. Heating the catalyst to a second temperature between 200° C. and 500° C. and at least 50° C. higher than the first temperature desorbs the oligomers that are then separated into gasoline and distillate range products.
In some embodiments, a system for upgrading light olefins includes a reactor containing an oligomerization catalyst and coupled to a feed of olefins selected from at least one of ethylene, propylene and butylenes. The reactor configuration cycles between an oligomerization and adsorption operation in which the olefins and the catalyst are in fluid communication for contact at a first temperature and a recovery operation. For the recovery operation, heating to a second temperature higher than the first temperature desorbs from the catalyst oligomers of the olefins.
A more complete understanding of the present invention and benefits thereof may be acquired by referring to the following description taken in conjunction with the accompanying drawings.
Turning now to the detailed description of preferred arrangements of the present invention, it should be understood that the inventive features and concepts may be manifested in other arrangements and that the scope of the invention is not limited to the embodiments described or illustrated.
Methods and systems relate to upgrading light olefins, such as ethylene, propylene and butylenes, diluted in a gas mixture, such as refinery fuel gas. The upgrading yields products in a gasoline, distillate, lube oil or wax range without requiring purification or compression of the gas mixture prior to feeding the gas mixture to a reactor. In operation, the mixture contacts a solid oligomerization catalyst, such as silica supported chromium, within the reactor. This contact occurs at a first temperature suitable to produce oligomers that are formed of the olefins and adsorb on the catalyst in liquid or solid phases. Next, heating the catalyst to a second temperature higher the first temperature desorbs the oligomers that are recovered and separated into the products.
Exemplary solid compositions suitable for the catalyst 104 used to oligomerize light olefins into oligomers for gasoline, distillate, lube oil and wax range products with between 5 and 30 carbons or 5 and 50 carbons include activated metals disposed on porous support materials. The catalysts 104 may include chromium, iron, cobalt, nickel and combinations thereof. Examples of the support materials for the catalyst 104 include silica and silica-alumina oxides.
In the oligomerization and adsorption step, a feed stream introduced through the inlet 101 contacts the catalyst 104, which is in an active state as depicted by unfilled circles in
The feed stream thus may include a mixture of gases with dilute ethylene. For example, the fuel gas suitable for the feed stream may contain greater than 15 percent by volume (vol. %) methane and less than 75 vol. % olefins. Exemplary concentrations within such feed streams range from 30 vol. % to 60 vol. % methane, 4 vol. % to 20 vol. % ethylene, 5 vol. % to 15 vol. % hydrogen, 0 vol. % to 15 vol. % propylene with remaining volume being other olefins with three or five carbons along with other gases.
The catalyst 104 and the feed stream contact at a first temperature during the oligomerization and adsorption step. For some embodiments, the first temperature ranges from 20° C. to 500° C. or from 20° C. to 300° C. Pressure in the reactor 100 for the oligomerization and adsorption step ranges in some embodiments from 100 kilopascals (kPa) to 7000 kPa or 100 kPa to 1400 kPa.
The oligomers of the olefins form as the feed stream contacts the catalyst 104. The oligomers deposit on surfaces of the catalyst 104 and are trapped in pores of the catalyst 104. Conditions in the reactor 100 throughout the oligomerization and adsorption step result in desirable products remaining in liquid and solid phases adsorbed on the catalyst 104. Given that selective oligomerization of the olefins occurs, non-olefin constituents of the feed stream do not react or get adsorbed and therefore pass through the reactor 100 and the outlet 102.
For some embodiments, the second temperature used in the recovery step exceeds the first temperature employed for the oligomerization and adsorption step by at least 50° C., at least 100° C. or at least 150° C. The second temperature in some embodiments ranges from 100° C. to 800° C. or from 200° C. to 500° C. While not limited to any particular theory, it is believed that the heating facilitates physical desorption of the oligomers from the catalyst 104 along with some cracking of the oligomers.
A carrier gas flowing through the inlet 101 sweeps the oligomers out of the reactor 100 as the product desorbs from the catalyst 104. While the carrier gas may be the same as the feed stream, some embodiments use a different composition for the carrier gas such that the feed stream or the olefins are stopped from passing into contact with the catalyst 104 during the recovery step. For example, steam may function as the carrier gas and also supply the heat needed to reach the second temperature.
In some embodiments, the heating of the catalyst 104 releases the oligomers from the catalyst and into a gas phase. The oligomers released into the gas phase may include C5-C21 hydrocarbons that remained in liquid and solid phases on the catalyst 104 during the passing of the feed stream into contact with the catalyst 104. Effluent from the reactor 100 that exits through the outlet 102 during the recovery step includes the carrier gas along with the oligomers. Separation of the effluent removes the carrier gas and fractionates the products into gasoline, distillate, lube oil and wax ranges for inclusion in respective blend pools.
The regeneration of the catalyst 104 occurs by flowing regeneration gases in sequence through the inlet 101 and into contact with the catalyst 104 inside the reactor 100. The regeneration gases include oxidants (e.g., oxygen or air) introduced to burn coke deposited on the catalyst 104 followed by reducing agents (e.g., carbon monoxide, hydrogen or light hydrocarbons) to reduce active metals of the catalyst 104 to lower oxidation states. In some embodiments, the regeneration of the catalyst 104 includes calcination of the catalyst 104 in air or oxygen atmosphere at 200° C. to 650° C., purging with an inert gas such as steam, nitrogen, argon or carbon dioxide at 200° C. to 500° C. and reduction of the catalyst 104 in carbon monoxide, ethylene, propylene, hydrogen or mixtures thereof at 200° C. to 500° C.
Each following example is provided by way of explanation of the invention, one of many embodiments of the invention, and the following examples should not be read to limit, or define, the scope of the invention.
Preparation of Catalyst A was done by dissolving 11.2 grams (g) Cr(NO3)3.9H2O in 43 milliliters (mL) deionized water to form a solution. Then, 40 g of zeolite (SiO2/Al2O3=80) was put into the solution to provide a support for the chromium. After mixing and wetting, an impregnated sample was dried at 110° C. in air for 24 hours and then calcined in air at 550° C. for 5 hours.
Preparation of Catalyst B was done by dissolving 3.1 g Ni(NO3)2.6H2O in 42 mL deionized water to form a solution. Then, 40 g of silica beads (surface area=370 meters square per gram (m2/g), pore volume=1.08 mL/g) was put into the solution to provide a support for the nickel. After mixing and wetting, an impregnated sample was dried at 110° C. in air for 24 hours and then calcined in air at 550° C. for 16 hours.
Preparation of Catalyst C was done by dissolving 9.5 g Ni(NO3)2.6H2O in 39 mL deionized water to form a solution. Then, 40 g of silica beads (surface area=370 m2/g, pore volume=1.08 mL/g) was put into the solution to provide a support for the nickel. After mixing and wetting, an impregnated sample was dried at 110° C. in air for 24 hours and then calcined in air at 550° C. for 16 hours.
A stainless steel tubular reactor (1.27 centimeter inner diameter) was loaded with 8 g of the Catalyst A. The reactor was heated up to 500° C. and purged with nitrogen for 30 minutes (min). The catalyst was then reduced in carbon monoxide at 350° C. for 60 min. After cooling down to 150° C. in carbon monoxide flow, the reactor was pressurized up to 345 kilopascals for an oligomerization and adsorption operation with 67% ethylene and 33% nitrogen at a flow rate of 300 ml/min for 20 min. Ethylene flow was then stopped. In a subsequent recovery operation, the reactor temperature was increased to 490° C.
An effluent gas condenser collected 7.6 g liquid by completion of the recovery operation. The liquid yield was 35.8%. Simulated distillation indicated that the liquid was composed of 55.5 weight percent (wt. %) C5-C11, 34.8 wt. % C12-C21 and 8.6 wt. % C22+ hydrocarbons.
As in Example 4, the reactor was loaded with the Catalyst A, which was then reduced. The reactor at 150° C. was pressurized up to 345 kilopascals for an oligomerization and adsorption operation with 33% ethylene and 67% nitrogen at a flow rate of 300 ml/min for 60 min. Ethylene flow was then stopped. In a subsequent recovery operation, the reactor temperature was increased to 350° C.
The effluent gas condenser collected 2.2 g liquid by completion of the recovery operation. The liquid yield was 27.4%. Simulated distillation indicated that the liquid was composed of 54.3 wt. % C5-C11, 43.0 wt. % C12-C21 and 2.2 wt. % C22+ hydrocarbons.
The Catalyst B was loaded into the reactor and reduced as in Example 4. During an oligomerization and adsorption operation with the reactor at 150° C., 75% ethylene and 25% nitrogen flowed at a rate of 200 ml/min for 70 min. Ethylene flow was then stopped. In a subsequent recovery operation, the reactor temperature was increased to 500° C.
Upon completion of the recovery operation, the effluent gas condenser collected 7.2 g wax. The wax yield was 54.9%. Simulated distillation indicated that the wax was composed of 8.1 wt. % C5-C11, 23.0 wt. % C12-C21 and 68.9 wt. % C22+ hydrocarbons.
The Catalyst C was loaded into the reactor and reduced as in Example 4. During an oligomerization and adsorption operation with the reactor at 150° C., 75% ethylene and 25% nitrogen flowed at a rate of 200 ml/min for 80 min. Ethylene flow was then stopped. In a subsequent recovery operation, the reactor temperature was increased to 500° C.
The effluent gas condenser collected 6.4 g wax by completion of the recovery operation. The wax yield was 42.7%. Simulated distillation indicated that the wax was composed of 16.0 wt. % C5-C11, 26.9 wt. % C12-C21 and 57.1 wt. % C22+ hydrocarbons.
In closing, it should be noted that the discussion of any reference is not an admission that it is prior art to the present invention, especially any reference that may have a publication date after the priority date of this application. At the same time, each and every claim below is hereby incorporated into this detailed description or specification as additional embodiments of the present invention.
Although the systems and processes described herein have been described in detail, it should be understood that various changes, substitutions, and alterations can be made without departing from the spirit and scope of the invention as defined by the following claims. Those skilled in the art may be able to study the preferred embodiments and identify other ways to practice the invention that are not exactly as described herein. It is the intent of the inventors that variations and equivalents of the invention are within the scope of the claims whiles the description, abstract and drawings are not to be used to limit the scope of the invention. The invention is specifically intended to be as broad as the claims below and their equivalents.
This application is a non-provisional application which claims the benefit of and priority to U.S. Provisional Application Ser. No. 61/583,073 filed Jan. 4, 2012, entitled “Upgrading Light Olefins,” which is hereby incorporated by reference in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| 61583073 | Jan 2012 | US |
