PROCESS FOR DESULFURIZATION OF PETROLEUM DISTILLATES

Abstract: The desulfurization of petroleum distillates can be carried out by cyclic low-temperature adsorption of oxidized sulfur compounds with activated carbon followed by regeneration of the activated carbon using an organic solvent. The activated carbon used in the process is commercially available and its surface area that ranges from approximately 500 to 2000 m<2>/g having a substantial portion of its pores in the range between 10 to 100 Angstroms.

Description: PROCESS FOR DESULFURIZATION OF PETROLEUM DISTILLATES CROSS REFERENCE TO RELATED APPLICATIONS This application claims the benefit of United States Provisional Application No 60/170,416, filed December 13, 1999, which is herein incorporated by reference in its entirety FIELD OF THE INVENTION The present invention relates to a novel process for the removal of sulfur compounds from petroleum distillates by selective adsorption on activated carbon which can be used in petroleum refining for the desulfuπzation of gasoline, naphtha, kerosene, diesel fuel, fuel oil and other products BACKGROUND OF THE INVENTION The production of sulfur-free petroleum distillates is becoming more and more important due to environmental concerns In particular, diesel fuel is now regulated all over North America to a maximum sulfur level of 500 ppm (Federal Register, Vol 64, No 92, May 13, 1999) for highway diesel engines In Europe and Japan sulfur levels down to 50 ppm or even lower have been proposed Currently, catalytic hydrodesulfuπzation is the technology that is practiced in refineries to reduce diesel sulfur to 500 ppm The high pressures and temperatures associated with hydrodesulfuπzation and modifications thereof not only significantly increase the cost, they also have the potential to alter desirable characteristics of distillate fuels Therefore, there is both a strong economic and technical incentive to develop cost effective techniques for sulfur reduction using very mild conditions (e g , 20°C to 75°C temperature and ambient to very low pressures) U S Pat No 5,454,933 teaches a process that uses activated carbon together with catalysts composed of Group VI and Group VIM metals as a polishing desulfuπzation agent for distillates previously subjected to hydrodesulfuπzation U S Patent No 2,877,176 teaches the use of alkali-doped activated carbon for adsorption of sulfur from distillate fuels followed by washing the carbon with a hot hydrocarbon However, a complete process for economic sulfur removal by an adsorbent using negligible amounts of activated carbon (impregnating a catalyst within the carbon to create its activation) and other reagents which results in reduced emissions into the environment is not disclosed or described in the prior art BRIEF SUMMARY OF THE INVENTION The present invention relates to a process for desulfunzation of petroleum distillates, in particular diesel fuel separated by distillation into a low sulfur and a high sulfur fraction, using cyclic low temperature adsorption of the high sulfur diesel fraction on commercially available activated carbon (catalytically impregnated carbon) followed by a solvent stripping step, a regeneration (solvent-washing) step and a carbon drying step in a closed loop zero emission system The desulfuπzed diesel fuel is then blended with the low-sulfur diesel fraction from the primary crude separation (distillation) step to yield the final desulfuπzed diesel product and a high-sulfur by product It is an object of the present invention to reduce total sulfur levels in petroleum distillates to less than approximately 500 ppm BRIEF DESCRIPTION OF THE DRAWINGS Fig 1 is a diagrammatic flowchart of the overall process' concept as provided in accordance with the teachings of the present invention Specifically Fig 1 shows the initial process whereby diesel fuel is split into low-sulfur and high-sulfur fractions Fig 2 is a detailed flowchart of the overall desulfunzation process of the high- sulfur fraction as provided in accordance with the teaching of the present invention DETAILED DESCRIPTION OF THE INVENTION In one embodiment of the present invention FIG 1 crude oil 1 is first subjected to distillation 2 to achieve the various fractions 3, 4, 5 of which diesel 3 is one Diesel typically ranges from approximately C10 to C o hydrocarbons Approximately 30% of the diesel fraction from Cio to C13 contains much less sulfur than the heavier fraction (d to C 2 o) The high-sulfur 4 fraction is then subjected to the process shown in FIG 2 The high-sulfur diesel fraction or diesel feed 21 mixes with the high-sulfur bottom recycle 41 as shown in FIG 2 The combined stream 22 enters the sulfur adsorber 43 either co-currently or counter-currently The sulfur adsorber 43 consists of a moving-bed of high surface area (between approximately 500 to 1500 m 2 /g) porous (with most pores in the 10 to 100 Angstrom range) carbon The diesel fuel is desulfuπzed and leaves the adsorber 43 as low-sulfur diesel product 23 to be blended with the low sulfur diesel fraction 3 from FIG 1 The moving carbon stream 25 enters a solvent stripper 44 into which a solvent vapor laden nitrogen stream 27 enters and essentially solvent-free nitrogen stream 28 leaves The carbon 26 (with oil) moves out of the solvent stripper 44 as stream 26 and enters the oil desorber 45 where it is contacted with liquid solvent and leaving with the desorbed oil as stream 30 The solvent and oil mixture 30 goes to a solvent still 46 and is separated into a high-sulfur bottom stream 42 and a solvent overhead stream 35 that is recycled back to the oil desorber as stream 29 The high-sulfur bottom recycle stream 41 can be recycled to the mix with the diesel as stream 22 to increase the sulfur content of the feed to the sulfur adsorber 43 and reduce the amount of oil carried away in the high-sulfur bottom stream 42 The regenerated carbon leaves the oil desorber as stream 31 and since it contains solvent it enters a solvent desorber 47 The solvent is stripped from the carbon by nitrogen stream 28 and the nitrogen solvent mixture 27 is recirculated back to the solvent stripper 44 The dry regenerated carbon leaves the solvent desorber as stream 24 and is recycled back to the sulfur adsorber 43 The entire process takes place at pressures ranging from approximately 1-5 atmospheres Typical temperatures of operation are provided below Sulfur adsorber 43 25 - 50°C Solvent stripper 46 25 - 50°C Oil desorber 45 50 - 100°C Solvent desorber 47 50 - 1 10°C Solvents used in conjunction with the teachings of the present invention include organic solvents with boiling points below the boiling point of the petroleum distillate to be desulfuπzed In one embodiment of the present invention the petroleum distillate is diesel fuel having an initial boiling point of approximately 150°C Toluene is the preferred solvent for desulfuπzing diesel fuel Other acceptable solvents include, but are not limited to, benzene, chlorinated hydrocarbons, hexane and cyclopentane However, environmental and toxicity concerns may limit the choice of industrially acceptable solvents Solvents are selected based upon their ability to remove aromatic components of oxidized sulfur The entire process takes place in a closed loop with no emissions. The high- sulfur bottom may carry traces of solvent away and this is made up as stream 48. The modification of crude distillation to split the diesel into two indicated fractions 3 and 4 from FIG 1 results in a nearly 30 % savings in desulfunzation because a 30 % smaller stream 4 is to be desulfurized. Furthermore, the extremely mild conditions of the desulfunzation process present a very cost-effective alternative to hydrodesulfurization. While the following non-limiting examples utilize diesel fuel as the source of sulfur containing distillates, the present invention can be applied to other distillates. Moreover, the moving-bed is described as the preferred configuration in FIG 2; however, cyclic fixed-beds, stirred tanks can also be used. The following non-limiting examples will provide the reader, and persons of ordinary skill in the art, a better appreciation and understanding of the present invention. EXAMPLES Diesel Fuels Used The diesel fuels used were gas oil 0.2% S from Saybolt (Diesel #1 ), L-0, 2-62 premium from Lukoil (Diesel #2), and L-0, 5-62 from Lukoil (Diesel #3). The properties of these fuels as provided by the supplier are shown in Table 1. Materials Used The following commercially available carbon sources were used as adsorbents: A. Carbo-Tech GMBH, Activekohle, Typ D52/4NOx B. Calgon Mixed BPL 6 χ 16 and PCB 6 χ 16 C. Barneby and Sutcliffe, Type Gl, 8 χ 16, Lot #1 -31 -1T D. Strem, 06-0050, Lot #135211 -S E. Calgon, Sample #3092-4-3 (high catalytic activity carbon) F. Calgon, BPL 6 χ 16 G. Calgon, F-400 H. Calgon, Cal 12^40 I. Calgon, CPG 12x40 Sulfur Measurement Instrument Horiba Sulfur-in-Oil Analyzer SLFA-20. Petroleum Distillate Samples Used Diesel #1 was analyzed 10 times using the Honba analyzer The average sulfur content was 1353 ppm with a standard deviation of 18 ppm The Diesel #2 was analyzed 10 times using the Honba analyzer The average sulfur content was 1969 ppm with a standard deviation of 12 ppm Diesel #3 was analyzed 10 times using the Honba analyzer The average sulfur content was 2847 ppm with a standard deviation of 26 ppm Example 1 A quantity of 531 5g of Diesel #3 measurement of 2850-ppm sulfur was vacuum (at 28" Hg vacuum) distilled to yield 6 fractions The weight distribution and sulfur content are provided below Fraction # Weight % Sulfur (ppm) Distilled at (°C) 1 0 34 57 collected from vapor by condensation at -2 2 9 97 465 172 3 10 47 719 186 4 10 54 1021 197 5 6 91 1304 240 6 (as measured) 60 33 4201 Residual Diesel 6 (by subtraction) 61 82 Table 1 Properties of Diesel Fuels Experimental Designation Diesel #1 Diesel #2 Diesel #3 Name Gasoil 0 2%S L-0,2-26 Premium L-0,5-62 Supplier Saybolt Lukoil Lukoil Density (kg/L) 0 829 0 860 0 838 Sulfur content (wt%) 0 13 0 19 0 50 Cloud point (C) -9 -3 -6 Cold filter -20 -12 -14 Plugging point (C) Flash point (C) 61 65 65 Fractional Makeup 1 BP (C) 165 6 NA NA 50% recovered (C) 252 5 279 277 95% recovered (C) 342 0 NA NA 96% recovered (C) NM 360 354 FBP (C) 354 5 NA NA Example 2 Example 1 was repeated using 467 12 g of Diesel #3 that measured at 2850 ppm sulfur The weight distribution and sulfur contents are provided below Fraction # Weight % Sulfur (ppm) Distilled at (C) 1 0 49 230 collected from vapor by condensation at -2C 2 10 14 548 170 3 1 1 27 805 183 4 1 1 32 1 103 195 5 4 21 1405 240 6 (as measured) 61 69 4262 Residual Diesel 6 (by subtraction) 62 57 — — Example 3 The residual diesel fractions (#6) from Examples 1 and 2 were combined and subjected to further vacuum distillation into four fractions The weight distribution and sulfur contents are provided below Fraction # Weight % Sulfur (ppm) Distilled at (C) 1 9 09 2004 207 2 8 98 2310 21 1 3 3 94 2475 217 4 75 33 4780 Residual Diesel 4 (by subtraction) 77 99 Example 4 Example 1 was repeated using 261 44 g of Diesel #1 that measured 1353 ppm sulfur The weight distributions and sulfur contents are provided below Fraction # Weight % Sulfur (ppm) Distilled at (C) 1 0 45 NM collected from vapor by condensation at -2C 2 19 88 582 164 3 24 17 828 193 4 20 88 1 150 212 5 2 43 1418 223 6 29 19 2574 Residual Diesel Example 5 Example 1 was repeated using 470 1 1 g of Diesel #1 that measured 1357 ppm sulfur Seven fractions were collected The weight distributions and sulfur contents are provided below Fraction # Weight % Sulfur (ppm) Distilled at (C) 1 0 83 379 collected from vapor by condensation at -2C 2 10 2 518 143 3 10 63 723 152 4 1 1 97 795 167 5 9 79 846 181 6 4 15 860 194 7 51 65 1987 Residual Diesel Example 6 Example 1 was repeated using 818 69 g of Diesel #3 that measured 2850 ppm sulfur The weight distributions and sulfur contents are provided below Fraction # Weight % Sulfur (ppm) Distilled at (C) 1 0 85 NM 2 10 94 489 184 3 8 29 622 197 4 9 64 982 203 5 3 77 1123 207 6 66 50 3884 Residual Diesel Example 7 A quantity of 41 72 g of residual diesel (3884 ppm sulfur) from Example 6 was placed in each of 5 different beakers Ten grams of carbons A, B, C, D and E were mixed into the 5 beakers respectively The sulfur levels in the free oil was measured and the measurements are shown below Sulfur remaining (ppm) After After Carbon 4 3 h 24 1 h A ~ 3904 B -- 3071 C - 3065 D - 3134 E 3572 3357 Example 8 Unadsorbed residual diesel was decanted from carbons B, C, D, and E of Example 7 and subjected to carbon addition in the same ratio as Example 7 The results of sulfur remaining are shown below Sulfur remaining (ppm) Decanted Carbon Residual Diesel Added Carbon (g) (g) After 2 5 h After 23 h B 23 96 5 70 2699 2552 C 22 27 5 37 NM 2553 D 23 39 5 65 NM 2586 E 28 09 6 78 NM 2792 Example 9 Fractions 1 through 5 from Example 6 were combined in a way to yield Batch #1 and Batch #2 with a sulfur measurement of 768 ppm and 694 ppm, respectively Carbon B was added to each batch in the same oil to carbon ratio as Example 7 The results of the sulfur remaining are shown below Sulfur remaining (ppm) After 18 h After 41 h Batch 598 603 #1 Batch 480 487 #2 Example 10 A large sample of Diesel #1 was distilled as in Example 1 to produce 5 fractions and 1584 g of residual diesel Fractions 1 and 2 were combined to yield 440 g, fractions 3, 4, and 5 were combined to yield 1018 g The residual diesel measured 1992 ppm sulfur The 1584 g of residual diesel was placed in a 4L beaker and approximately 396 g of Carbon B was added After 72 hours, the sulfur content was reduced to 1330 ppm The resulting diesel was filtered to yield 1313 g of oil with 271 g of oil retained on the carbon To the 1313 g of diesel, approximately 326 g of fresh Carbon B was added and the slurry which was left standing for 72 hours The sulfur content was reduced to 980 ppm The resulting slurry was filtered and 1096 g of oil was recovered To this oil, 271 g of Carbon F was added and left standing for an additional 24 hours The sulfur content was reduced to 797 ppm This slurry was filtered and 880 g of oil was recovered To this, 222 g of Carbon C was added and left standing for another 24 hours The sulfur content was reduced to 635 ppm The resulting slurry was filtered and yielded 689 g of oil To this, 70 g of Carbon C and 102 g of Carbon D was added The sulfur reduced to 531 ppm This final slurry was filtered to yield 554 g of oil Example 1 1 The combined fractions 3-5 from Example 10 (1018 g) measured 773 ppm sulfur The combination was placed in a beaker and 252 g of Carbon F was added After 24 hours the sulfur content had reduced to 612 ppm The slurry was filtered and 829 g of oil was recovered To this slurry 206 g of Carbon F was added After 24 hours the sulfur content had been reduced to 515 ppm The slurry was filtered and 688 g of oil was recovered To this 171 g of Carbon D was added After 24 hours the sulfur content had been reduced to 488 ppm The slurry was filtered and 570 g of oil was recovered Example 12 The combined fractions 1 and 2 from Example 10 (440 g) measured 449 ppm sulfur This combination was mixed with desulfunzed oils from Examples 10 and 11 in the same ratio as the original proportions Thus 554 g of oil from Example 10 was combined with 378 g of oil from Example 11 and 151 g of combined fractions 1 and 2 to yield desulfunzed diesel The sulfur content of the desulfunzed diesel measured at 480 ppm Example 13 Saybolt independently analyzed the desulfunzed diesel from Example 12 Properties of the original Diesel #1 and desulfunzed Diesel #1 are compared in Table 2 which illustrates that other than the reduced sulfur content there were no other significant change in properties Table 2 Comparison of Properties of Diesel #1 and Desulfunzed Diesel #1 Result Desulfunzed Diesel Test Method Unit Diesel #1 from Example 13 Specific gravity at 15C ASTM D 4052 kg/L 0 8289 0 8147 Sulfur ASTM D 2622 mass % 0 13 0 054 Flash point ASTM D 93 °C 61 0 64 0 Cloud point ASTM D 2500 °C -9 -15 Cold filter plugging point IP 309 °C -20 -15 Distillation IBP °C 164 5 174 0 10 v/v recovered °C 195 0 200 0 20 v/v recovered °C 210 0 213 5 30 v/v recovered °C 225 5 228 5 40 v/v recovered °C 239 0 241 5 50 v/v recovered °C 252 5 254 5 60 v/v recovered °C 266 5 267 5 70 v/v recovered °C 281 0 281 5 80 v/v recovered °C 295 5 299 0 90 v/v recovered °C 323 5 322 5 95 v/v recovered °C 342 0 342 0 FBP °C 354 0 351 Residue v/v% 1 0 2 0 Loss v/v% < 0 5 0 5 Example 14 A quantity of 182 4 g of Diesel #2 (sulfur - 1973 ppm) was mixed with 45 61 of Carbon D and the mixture was left standing for 24 hours The sulfur content was reduced to 1339 ppm The slurry was filtered to yield 155 g of oil To this, 38 7 g of Carbon D was added The sulfur content was further reduced to 1034 ppm The slurry was filtered to yield 132 3 g of oil To this 33g Carbon D was added The sulfur content was reduced to 845 ppm The slurry was filtered to yield 113 g oil To this 28 g carbon D was added The sulfur content was reduced to 704 ppm The slurry was filtered to yield 95 g oil To this 23 8 g carbon was added The sulfur content was reduced to 585 ppm The slurry was filtered to yield 77 g oil To this 19 g carbon was added The sulfur content was reduced to 498 ppm The slurry was filtered to yield 67 g of desulfunzed diesel measuring 498 ppm sulfur Example 15 A quantity of 72 g of spent carbon (wiih oil) [from Example 10, Carbon C added to797 ppm sulfur oil] containing an estimated 33 g oil was subjected to Soxhlet extraction using toluene The toluene (with oil extracted) was distilled to separate the oil that measured 31 5 g and had 1261 ppm sulfur The carbon was dried with nitrogen gas at 120°C The regenerated carbon was tested for desulfunzation efficiency. Forty-one g of regenerated carbon was mixed with 171 g of Diesel #3 containing 2835 ppm sulfur The sulfur content was reduced to 1949 ppm in 24 hours. The regenerated carbon was thus more efficient than the original carbon. Example 16 A quantity of 50 mL of Diesel #3 containing 2850 ppm sulfur was mixed with 10 g of Carbon G at 22°C and the sulfur content was monitored as a function of time. The results are shown below Time (h) Sulfur remaining (PPm) 0.25 2594 0.5 2488 1 2292 2 2219 4 2227 Example 17 Same as Example 16 except, 20 g of Carbon G was used The results are shown below Time (h) Sulfur remaining (ppm) 0 25 2033 0 5 1996 1 2002 2 1909 Example 18 Same as Example 16 except 50 g Diesel #3 and 30 g of Carbon G was used The results are shown below Time (h) Sulfur remaining (ppm) 0 25 1555 0 5 1754 1 0 1747 2 0 1822 4 0 1720 Example 19 Same as Example 18 except 30 g of Carbon F was used The results are shown below Time (h) Sulfur remaining (ppm) 0 08 2384 0 33 2298 0 75 2037 1 0 1997 1 25 1835 3 1731 Example 20 Same as Example 18 except sulfur was measured quickly. The results are shown below: Time (min) Si ilfur remaining (ppm) 2 2408 12 2113 24 1882 Example 21 Same as Example 18 except 20 g of Carbon H was used. The results are shown below: Time (min) Sulfur remaining (ppm) 5 2387 17 2223 30 2169 60 2084 130 1974 180 1976 285 1912 Example 22 Same as Example 18 except 20 g of Carbon I was used. The results are shown below: Time (min) Sulfur remaining (ppm) 5 2371 15 2259 40 2148 60 2002 105 1965 210 1929 Example 23 Same as Example 18 except 30 g of Carbon I was used The results are shown below Time (mm) Sulfur remaining (ppm) 5 2158 30 1880 60 1742 130 1685 180 1660 240 1652 Example 24 Same as Example 18 except 30 g of Carbon H was used The results are shown below Time (mm) Sulfur remaining (PPm) 5 2120 30 1780 60 1751 120 1686 180 1643 240 1658 Example 25 A quantity of 50 g of Diesel #3 (2850 ppm sulfur) was mixed with approximately 20 g of Carbon G After 15 minutes of contact with stirring, the slurry was filtered with a recovery of 33 g of diesel Its sulfur value had dropped to approximately 2201 ppm and 17 g of Diesel #3 remained attached to the wet carbon externally (in between granules) and inside the pores The original Diesel #3 color was yellow and the diesel recovered was yellow Fifty (50) g of hexane was poured through the wet carbon and 41 g of hexane wash came through the carbon with 9 g remaining on the carbon The hexane wash was clear, not yellow, and contained approximately 422 ppm sulfur Fifty (50) g of toluene was then poured through the wet carbon that had been treated with hexane as above Forty-three (43) g of toluene wash came through the carbon with 7 g remaining on the carbor The solvent wash was yellow and contained 291 ppm sulfur This example illustrates that a more polar and aromatic solvent such as toluene as opposed to hexane recovers chromagenic species from the carbon that actually give the diesel the yellow color, where as hexane is not able to recover these species Example 26 Example 25 was repeated except Carbon F was substituted for Carbon G The diesel recovered from the carbon weighed 36 g It had 2374 ppm sulfur and its color was yellow The hexane wash weighed 41 g, it was colorless and had 266 ppm sulfur The toluene wash weighed 45 g, it was light yellow and it had 218 ppm sulfur Example 27 An upflow packed-column was prepared containing about 2200-cc (1238g) of carbon G The column was a 2 5-ιnch x 36-ιnch high stainless steel tube External controlled heat was supplied to the column if necessary to control the bed temperature The diesel flow to the column was set at 17 2 cc/min A number of diesel fuel samples were tested A diesel fuel from a gas station containing 483 ppm sulfur was flowed up through the column at 30°C Adsorption caused the temperature to rise to 68°C as the diesel flowed up Once the adsorption wave went through, the temperature dropped back to 30°C Four samples of desulfunzed diesel were collected in 200 cc batches are shown below Sulfu r (ppm) Batch 1 60 Batch 2 79 Batch 3 129 Batch 4 117 Thus, the sulfur was reduced from 483 ppm to 60-129 ppm for the first 800 ml of fuel that passed through the column, over about 45 minutes Example 28 An upflow column was packed in a similar manner as Example 27 A diesel fuel from a gas station was spiked with dibenzothiophene and thianaphthene to achieve a diesel with a sulfur content of 2863 ppm This fuel was flowed up at 17 2 cc/min up through the column in a similar manner as Example 27 Adsorption again caused the temperature to rise to 68°C and then fall back to 30°C as the wave passed through the column Ten samples were collected in 230 cc batches The sulfur contents of these batches and of the column drain collected are shown below Sulfu r (ppm) Batch 1 100 Batch 2 347 Batch 3 580 Batch 4 903 Batch 5 1145 Batch 6 1390 Batch 7 1630 Batch 8 1762 Batch 9 1930 Batch 10 1958 Column Drain 2731 This example demonstrates that the first four batches (690 cc) when combined would have a sulfur content of less that 500 ppm and the last six batches (1610 cc) when combined with a portion of the column drain would have a sulfur content of less than 2000 ppm starting from a diesel containing 2863 ppm sulfur Example 29 First four batches from Example 28 were combined and designated as Sample B The last six batches from Example 28 were combined with 610 ml of column drain and designated as Sample C Each combination and the feed diesel (designated as Sample A) were sent to Saybolt for measurement of sulfur and other diesel specs These results are shown in Table 3 These results show that the sulfur reduction was as measured in Example 28 The Cetane index of the product improved, indicating removal of aromatics The other specs did not change significantly Table 3 Comparison of Properties of Feed Diesel (Sample A) and Two Product Diesels (Samples B&C) of Example 28 Example 30 The sulfided column from Example 27 was regenerated with toluene upflow (13 cc/min) for two hours at 75°C The sulfur content in the toluene product and column toluene dram indicated a sulfur recovery from the column of 73% Following the toluene wash, column was purged with nitrogen for two hours at 100°C Example 31 The partially regenerated column of Example 30 was tested for recovery of desulfunzation efficiency A diesel sample (Diesel #2, Table 1 ) containing 1998 ppm sulfur was flowed up through the column at conditions similar to Example 27 Seven 200 cc batches and the column drain were collected and their sulfur content was measured as follows Sulfur (ppm) Batch 1 462 Batch 2 558 Batch 3 726 Batch 4 881 Batch 5 962 Batch 6 1084 Batch 7 1152 Column Drain 1676 Thus, the sulfur content was reduced from 1998 ppm to as low as 462 ppm, indicating partial regeneration of the column with toluene Example 32 The column from Example 31 was regenerated again as in Example 30 with toluene followed by a nitrogen purge Measurement of sulfur in the toluene effluent and column drain indicated an 86% recovery of the sulfur from the column Example 33 The partially regenerated column of Example 32 was tested using a 526 ppm sulfur-containing diesel feed at conditions similar to Example 27 The first 250-ml effluent contained 413-ppm sulfur and the column drain contained 506-ppm sulfur Examples 31 and 33 indicate that following regenerations, sulfur removal limit is around 500 ppm This suggested a modification to the regeneration procedure Example 34 The column from Example 33 was regenerated as in Example 30 with toluene, however, the nitrogen purge was conducted at a higher temperature of 115°C Example 35 The partially regenerated column of Example 34 was again tested using the 526-ppm sulfur containing diesel feed at conditions similar to Example 27 The first 280 ml and the next 125 ml sample effluents showed only 300 ppm sulfur as opposed to 413 ppm in Example 33 and the column drain showed 440 ppm as opposed to 506 ppm sulfur in Example 33 This suggests that the 15°C higher N 2 purge temperature improved the regeneration efficiency of the column Example 36 The column of Example 35 was regenerated as in Example 34 The partially regenerated column was tested using a 534-ppm sulfur containing diesel feed, in a manner similar to Example 27, except that the column was maintained at 70°C as opposed to 30°C in Example 27. A total of 12 samples of the product and the column drain were collected from the effluent as shown below. Amount (g) Sulfur (ppm) Sample 1 178 276 Sample 2 184 294 Sample 3 171 255 Sample 4 173 299 Sample 5 178 316 Sample 6 178 325 Sample 7 177 350 Sample 8 174 357 Sample 9 175 356 Sample 10 186 346 Sample 11 191 338 Sample 12 179 392 Column Drain 795 480 This example shows that the desulfurization efficiency improves at 70°C since sulfur is consistently removed to less than 350 ppm from 534 ppm for the first seven collections. Example 37 The column from Example 36 was again regenerated as in Example 35 and subjected to diesel feed containing 485 ppm sulfur in a manner similar to Example 27, except that the temperature was 63°C and flow was reduced from 17.2 ml/min to 6.3 ml/min. A total of 12 samples of the product and the column drain were collected from the effluent as shown below. Amount (g) Sulfur (ppm) Sample 1 129 249 Sample 2 1 17 277 Sample 3 116 261 Sample 4 121 260 Sample 5 123 263 Sample 6 123 278 Sample 7 120 288 Sample 8 131 322 Sample 9 123 293 Sample 10 120 317 Sample 11 121 284 Sample 12 128 354 Column Drain 711 468 This example shows that a marginal increase in desulfunzation efficiency occurs when the flow is lowered from 17 2 ml/min to 6 2 ml/min The sulfur is reduced from 485 ppm to below 350 ppm in 11 of the first 12 column effluents The present invention provides a simple, mild, highly effective and inexpensive desulfunzation process which utilizes readily available, durable and inexpensive activated carbons (catalyst impregnated carbons) The desulfunzation process performed in accordance with the teachings of the present invention provide the following technical advantages over processes presently known in the art 1 The initial separation of the crude petroleum distillates into low and high- sulfur fractions limits the volume of distillates to be processed, thus significantly reducing costs 2 Final oxidized sulfur content in the petroleum distillate product can be regulated by a non-miscible solvent that selectively removes oxidized sulfur aromatic compounds and controlling the number of times the distillate is recycled through fresh regenerated carbon 3 The desulfunzation process is mild and effective 4 Selective regeneration of the carbon can be accomplished by using different solvents 5 Diesel fuel quality is not adversely effected 6 A very high-sulfur, low volume bottom product is produced by repeated exposure to the fresh regenerated carbon, thus increasing fuel yields and decreasing waste It will be apparent to one of ordinary skill in the art that many changes and modifications can be made in the invention without departing from the spirit or scope of the appended claims

Claims: What is claimed is 1 A process for removing sulfur compounds from petroleum compounds comprising separating said petroleum compounds into a first low-sulfur fraction and a first high-sulfur fraction, reacting said first high-sulfur fraction with at least one oxidizing agent, contacting said first high-sulfur fraction with at least one activated carbon capable of adsorbing said sulfur compounds thereby forming a second low-sulfur fraction and a second high-sulfur fraction, recycling said at least one activated carbon with at least one solvent and at least one gas, and recovering said petroleum compounds having said sulfur compounds removed therefrom 2 The process of claim 1 wherein the selection of said at least one solvent is based upon the selectivity of said solvent in removing aromatic sulfur components 3 The process of claim 2 further comprising contacting said second high-sulfur fractions with said at least one activated carbon, and recycling said second high-sulfur fractions repeatedly through said at least one activated carbon until said sulfur content level in said petroleum compound is less than approximately 500 ppm 4 The process of claim 1 wherein said solvents are selected from the group consisting of toluene, benezene, chlorinated hydrocarbons, hexane, and cyclopentane 5 The process of claim 1 wherein said gas is nitrogen 6 The process of claim 1 further comprising maintaining said process at a temperature of at least 20°C 7 The process of claim 1 further comprising maintaining said process at a temperature within the range of approximately 20°C to 150°C 8 The process of claim 1 further comprising maintaining said process at a pressu irree within the range of approximately 1 to 5 atmospheres 9 The process of claim 1 wherein said petroleum compound is selected from the group consisting of gasoline, naphtha, kerosene, diesel fuel, fuel oil, and crude oil 10 The process of claim 1 wherein said oxidizing agents are selected from the group consisting of air, oxygen, and hydrogen peroxide 11 The process of claim 1 wherein said activated carbons are arranged in a configuration selected from the group consisting of moving-beds, fixed-beds, cyclic fixed-beds, and stirred tanks 12 The process of claim 1 wherein said activated carbons have a surface area of at least 500 m /g 13 The process of claim 1 wherein said activated carbons have a surface area of approximately between 500 to 2000 m /g 14 The process of claim 1 wherein said activated carbons have a pore size ranging between 10 to 100 Angstroms 15 A process for removing sulfur compounds from petroleum compounds comprising separating said petroleum compounds into a first low-sulfur fraction and a first high-sulfur fraction, reacting said first high-sulfur fraction with oxidizing agents, contacting said first high-sulfur fraction with activated carbons capable of adsorbing said sulfur compounds thereby forming a second low-sulfur fraction and a second high-sulfur fraction, eluting said adsorbed sulfur compounds from said activated carbons, removing said adsorbed sulfur compounds from said solvents, and applying a gas to said activated carbons to regenerate said activated carbons 16 The process of claim 15 further comprising contacting said elutant having adsorbed sulfur compounds with said activated carbons 17. A system for removing sulfur compounds from petroleum compounds comprising: a distiller, wherein said petroleum compounds are separated into a first low- sulfur fraction and a first high-sulfur fraction; at least one carbon loop; and at least one solvent loop. 18. The system of claim 17 wherein said at least one carbon loop further comprises at least one activated carbon capable of adsorbing sulfur compounds thereby forming a second low-sulfur fraction and a second high-sulfur fraction. 19. The system of claim 17 wherein said solvent loop further comprises at least one solvent that elutes adsorbed sulfur compounds from said activated carbons.

Inventors: GANGWAL SANTOSH K, WISMANN WILLIAM, GANGWAL, SANTOSH, K., WISMANN, WILLIAM
Applicants: DS2 TECH INC, GANGWAL SANTOSH K, WISMANN WILLIAM, DS2 TECH, INC., GANGWAL, SANTOSH, K., WISMANN, WILLIAM
Application year: 2000
Main classification: C10G53
IPC codes: C10G25, C10G53