Dewaxing with nickel-silicalite catalyst

Abstract: A process for dewaxing middle distillate petroleum products includes the steps of introducing a middle distillate petroleum fraction having a boiling point in the range of from about 160 o C to about 500 o C into a reaction zone and contacting the middle distillate petroleum fraction in the reaction zone at temperatures of from about 500 o F to about 700 o F and pressures of from about 300 psig to about 2000 psig with a nickel-containing silicalite catalyst.

Description: TECHNICAL FIELD The present invention relates to a process for dewaxing middle distillate petroleum streams such as diesel and kerosene utilizing a nickel impregnated silicalite catalyst. BACKGROUND OF THE INVENTION Many petroleum middle distillate streams, particularly middle distillate streams produced from medium or severe hydrocracking operations, require dewaxing to provide the desired properties. Dewaxing involves the conversion of higher molecular weight straight and branched chain paraffins to lower molecular weight compounds. Conventional dewaxing processes for middle distillate fractions require temperatures in excess of about 700°F, typically in the range of from about 710°F to about 750°F (376°C to 398°C). Heating a middle distillate stream to this temperature range consumes a considerable amount of energy and requires substantial investment in process equipment. Thus, it would be desirable to reduce the amount of energy consumed and the amount of process equipment required to effectively dewax a typical middle distillate stream. Document D1 provides a process for hydrodewaxing middle distillates with a catalyst devoid of Group VI B metal components and comprising nickel components supported on a mixture of one or more amorphous, inorganic, refractory oxide components and a crystalline, intermediate pore, nonzeolitic molecular sieve having cracking activity, preferably a mixture of alumina and silicalite. The process of the present invention provides a method of dewaxing a middle distillate stream at lower than conventional temperatures, down to as low as about 260°C (500°F). Preferably, the dewaxing process of the present invention is practiced in the range of from about 260°C (500°F) to about 371°C (700°F). Dewaxing at these temperatures is achieved by utilizing a nickel- impregnated silicalite catalyst. SUMMARY OF THE INVENTION The present invention provides a method for dewaxing middle distillate petroleum products such as diesel, kerosene and light cycle oil utilizing a nickel impregnated silicalite catalyst. The use of the catalyst permits the dewaxing operation to be conducted at lower temperatures than conventionally used to dewax middle distillate streams. The Si/Al ratio of the silicalite utilized in the process of the present invention is greater than 200 and the catalyst contains from about 0.1% to about 5% nickel. The use of the catalyst permits dewaxing at temperatures that allow the dewaxing process to be accomplished in one or more beds of a multiple bed reactor that may also be used for hydrodesulfurization. DETAILED DESCRIPTION The process of the present invention provides an improved method of dewaxing middle distillate petroleum fractions such as diesel, kerosene and light cycle oil (LCO). The term "middle distillate" as used herein refers to petroleum distillate fractions having boiling points in the range of from about 160°C to about 500°C. These fractions are also characterized as having flash points between about 30°C and about 80°C. The process utilizes a silicalite catalyst that has been impregnated with nickel to dewax middle distillate fractions at temperatures that are lower than those used in conventional processes. The catalysts employed in the process of the present invention can be described as crystalline microporous organosilicates that are prepared hydrothermally with a reaction mixture including tetraethylammonium cations, alkali metal cations, water and a reactive source of silica. In contrast to crystalline zeolite materials which are aluminosilicates comprising three dimensional SiO 4 and AlO 4 tetrahedra joined by shared oxygen atoms, the silicalite crystalline organosilicates utilized in the process of the present invention are prepared from reaction systems which are essentially free of aluminum-containing reagents. Any aluminum present in the silicalite crystalline organosilicates is the result of impurities contained in the materials used to prepare the silicalites. Preferably, the Si/Al ratio of the silicalite utilized in the process of the present invention is greater than 200, more preferably the Si/Al ratio is in the range of from about 250 to about 500. After preparation, the silicalite catalyst may be dispersed in a binder or support material such as alumina. The silicalite binder admixture may be formed into the desired shape by extrusion, pelletization or other techniques known to those skilled in the art. After the silicalite binder admixture has been formed, it is impregnated with nickel, preferably in the form of an aqueous solution of a nickel salt. Methods of impregnating the silicalite catalyst with nickel are known to those skilled in the art. One method involves forming solutions of a nickel containing compound such as nickel nitrate or nickel acetate and then contacting the silicalite catalyst with the solution. The catalyst is contacted with a sufficient amount of the solution to deposit appropriate amounts of nickel or nickel salts onto the silicalite catalyst. Preferably, the silicalite catalyst is contacted with a sufficient amount of the solution to impregnate the catalyst with from about 0.1 wt% to about 5 wt% nickel. More preferably, the catalyst is impregnated with from about 0.5 wt% to about 1.5 wt% nickel. After the catalyst has been impregnated with the desired amount of nickel, the catalyst may be calcined. The nickel impregnated or nickel-containing silicalite catalyst prepared in accordance with the foregoing may be advantageously utilized to dewax middle distillate petroleum products. In one embodiment of the process of the present invention, the nickel impregnated silicalite catalyst is prepared as a 0.16 cm (one-sixteenth inch) diameter extrudate and is characterized by a crystallite particle size in the range of from about 1 to 2 microns (µm). The catalyst has a Si/Al ratio of about 300 and contains about 1% nickel. The process of the present invention can be carried out using a variety of process equipment, including a reactor vessel which defines a reaction zone containing catalyst material. Either single or multiple catalyst beds may be employed in the reaction zone. The dewaxing process of the present invention may be conducted at pressures of from about 2.07 MPa (300 psig) to about 13.79 MPa (2000 psig), preferably from about 2.76 MPa (400 psig) to about 6.89 MPa (1000 psig). Liquid hourly space velocities may range from about 0.1 hr -1 to about 30 hr -1 , more preferably from about 1 hr -1 to about 8 hr -2 . Hydrogen may be injected as needed depending on the particular feedstock to the dewaxing reactor. Normally hydrogen will be injected at a rate in the range of from 53.45 to 356.3 m 3 /m 3 (300 to 2000 SCFB) (Standard Cubic Feet per Barrel) of feedstock. As noted above, the dewaxing process may be operated at temperatures ranging from about' 260°C (500°F) to about 565.6°C (1050°F) and more preferably in the range of from about 287.8°C (550°F) to about 371°C (700°F). In another embodiment of the invention, the nickel-impregnated silicalite catalyst is used in one or more beds of a multiple bed reactor that also contain a catalyst suitable for hydrodesulfurization. The combination of dewaxing and hydrodesulfurization in a single multiple bed reactor is possible because the nickel-impregnated silicalite catalyst is effective in dewaxing within the same temperature range that hydrodesulfurization is accomplished. The process of the present invention may be further illustrated by the following example which is not to be construed as limiting the scope of the invention as hereinafter claimed. EXAMPLE Approximately 36 milliliters of a silicate catalyst impregnated with approximately 1% nickel is introduced into a loboratory scale reactor. The catalyst has a particle size distribution of between 420 and 250 microns (40 and 60 mesh) Nitrogen is introduced into the reactor and temperature is increased to about 115°C at a rate of about 50°C per hour. The temperature is maintained at this level for a period of from about 3 to 4 hours and then increased to about 150°C. The reactor is then placed under hydrogen flow for about ten to fifteen hours after which the reactor temperature is increased to about 250°C. A feed stream comprising a mixture of 52% straight run distillate, 16% kerosene and 20% light cycle oil is introduced into the reactor at a rate of 3.00 milliters per minute, corresponding to a liquid hourly space velocity of 5.0 hr -1 . Hydrogen is fed to the reactor at a rate of 0.266 liters/min. and the reactor pressure is maintained between 2.96 and 3.1 MPa (430 and 450 psig). The reactor feed stream is characterized in Table 1 below: REACTOR FEED API Gravity 32.6 Color 1.5 Sulfur wt% 0.815 Flash Point 87.8°C (190°F) Pour Point -6.7°C (20°F) Cloud Point -3.3°C (26°F) Initial Boiling Point 196.7°C (386°F) Centane Index 48.6 H 2 /Distillate Ratio 89m 3 /m 3 (500 SCFB) (Standard Cubic Feet per Barrel). The test is conducted for 600 hours and the reactor effluent is periodically sampled and analyzed for pour point and cloud point. Reactor inlet and outlet temperatures along with the reactor effluent pour point and cloud point are set forth below: Test Duration (hours) Reactor Inlet Temp (°C) Outlet Pour Point (°F) °C Cloud Point (°F) °C 2 252 253 (0) -17.8 (18) -7.8 22 262 264 (20) -6.7 (22) -5.6 29 285 286 (10) -12.2 (13) -10.6 46 286 287 (10) -12.2 (17) -8.3 70 290 292 (10) -12.2 (17) -8.3 94 295 296 (5) -15 (12) -11.1 103 303 305 (10) -12.2 (15) -9.4 118 303 305 (10) -12.2 (16) -8.9 126 315 318 (5) -15 (11) -11.7 142 312 315 (10) -12.2 (15) -9.4 150 317 321 (10) -12.2 (14) -10 167 316 319 (5) -15 (16) -8.9 175 318 320 (5) -15 (16) -8.9 192 315 318 (15) -9.4 (22) -5.6 200 321 324 (10) -12.2 (15) -9.4 218 320 323 (10) -12.2 (16) -8.9 241 328 330 (10) -12.2 (13) -10.6 265 327 329 (10) -12.2 (14) -10 289 330 332 (10) -12.2 (14) -10 321 328 331 (10) -12.2 (11) -11.7 336 328 331 (10) -12.2 (13) -10.6 360 328 334 (10) -12.2 (16) -8.9 365 329 332 (10) -12.2 (12) -11.1 384 329 331 (15) -9.4 (16) -8.9 408 334 336 (10) -12.2 (15) -9.4 432 336 338 (5) -15 (15) -9.4 439 340 342 (5) -15 (10) -12.2 456 340 342 (5) -15 (14) -10 480 338 340 (10) -12.2 (16) -8.9 504 339 342 (10) -12.2 (17) -8.3 511 342 344 (10) -12.2 (12) -11.1 552 344 345 (10) -12.2 (15) -9.4 578 346 348 (10) -12.2 (16) -8.9 600 354 355 (0) -17.8 (8) -13.3 While the invention has been described in connection with the foregoing example, it will be appreciated by the those skilled in the art that the invention is subject to variations and modifications which fall within the scope of the appended claims and which are intended to be covered thereby.

Claims: A process for dewaxing middle distillate petroleum products comprising : introducing a middle distillate petroleum fraction having a boiling point in the range of from 160°C to 500°C into a reaction zone; and dewaxing the middle distillate petroleum fraction in the reaction zone at temperatures of from 260°C (500°F) to 565.6°C (1050°F) in the presence of nickel-containing silicalite catalyst wherein the amount of nickel is of from 0.1 to 5 wt%, characterized by a crystallite particle size in the range of from 0.1 to 2 (µm) microns. The process of Claim 1 wherein the middle distillate fraction is dewaxed at a temperature between 260°C (500°F) and 454.4°C (850°F). The process of Claim 2 wherein the middle distillate fraction is dewaxed at a temperature between 260°C (500°F) and 371°C (700°F) The process of any one of the preceding claims wherein the reaction zone is maintained at a pressure of from 2.04 Mpa (300 psig) to 13.79 Mpa (2000 psig). The process of any one of the preceding claims, wherein the middle distillate petroleum fraction is selected from the group consisting of diesel, kerosene, light cycle oil and mixtures thereof. The process of any one of the preceding claims wherein the reaction zone is operated at liquid hourly space velocities of from 0.1 hr -1 to 30 hr -1 . The process of any one of the preceding claims wherein the reaction zone comprises at least one catalyst bed in a multibed reactor, said at least one catalyst bed containing a catalyst suitable for hydrodesulfurization of middle distillate petroleum fractions. The process of any one of the preceding claims wherein hydrogen is introduced into the reaction zone at a rate of from 53.45 m 3 /m 3 (300 SCFB) to 356 m 3 /m 3 (2000 SCFB) based upon the flow of the middle distillate fraction. The process of Claim 3 wherein the pressure is from 0.34 (50) to 13.79 MPa (2000 psig) and the catalyst is a nickel containing silicalite catalyst comprising from 0.5% to 1.5% nickel. The process of Claim 9 wherein the middle distillate petroleum fraction is selected from the group consisting of diesel, kerosene and light cycle oil and mixtures thereof. The process of Claim 9 wherein the reaction zone further comprises a catalyst suitable for hydrodesulfurization of the middle distillate petroleum fraction. The process of Claim 9 wherein hydrogen is introduced into the reaction zone at a rate of from 53.45 m 3 /m 3 (300 SCFB) to 356 m 3 /m 3 (2000 SCFB) based upon the flow of the middle distillate fraction.

Inventors: BUTLER JAMES R, FORWARD CLEVE, BUTLER, JAMES R., FORWARD, CLEVE
Applicants: FINA TECHNOLOGY, FINA TECHNOLOGY, INC.
Application year: 1996
Main classification: C10G45
IPC codes: C10G25, B01J29, C10G65, C10G67, C10G45