SA01220321B1 - Process for desulfurization of petroleum feeds - Google Patents

Abstract

Abstract: The hydrodesulfurization process has been discussed for a stream of distilled cracked naphtha in which very few valuable olefins are saturated. The process is a two-stage process as H2S separates the two phases to prevent the formation of recombinant mercaptans. Where H2S is separated between the stages, milder stages can be used in the second stage of the polishing reactor to achieve the same desulfurization rates with less olefin loss.

Description

A process for desulfurization from petroleum feeds Full description Background of the invention The present invention is concerned with a process for desulfurization from a full boiling point of fluid catalytic cracked naphtha by hydrogen reaction With organic sulfur compounds present in feed in the presence of hydrogenation catalysts - sulfur separation catalysts. Fifthly, the invention ALL can use catalytic distillation steps that reduce desulfurization to very low rates ¢ enable more efficient use of hydrogen and cause less olefin hydrogenation for the full boiling rate range of stream flowing from naphtha Gall Yee petroleum distillate streams containing a variety of organic chemical constituents dale . organic chemical, the currents are determined by its boiling rate, which determines the composition. The treatment of Lad currents affects the installation. for example; The products from either catalytic distillation or thermal cracking processes contain high concentrations of olefinic materials in addition to saturated alkanes and polyunsaturated substances (diolefins). Additional; These components can represent any of the various isomers in the compounds.The composition of the untreated naphtha as it comes from the crude distillation apparatus, or the straight-running naphtha, is influenced primarily by the crude source. Crude paraffinic sources include more saturated cyclic or straight-chain compounds.As a general Yo base, the more sweetened crude compounds (lower in sulfur content) and naphtha compounds are paraffinic.Crude naphtha compounds contain more unsaturated, cyclic and polycyclic compounds.Raw materials Those with higher sulfur content tend to be LE by Yovy treatment

Different straight-running naphtha compounds can vary slightly depending on their composition as a result of the raw source. Reconstituted or reconstituted naphtha generally does not require any further processing except perhaps distillation or solvent extraction in order to separate the valuable aromatic product. © Reconstituted naphtha compounds do not primarily contain any sulfur impurities due to the risk of pre-treatment of the treatment process and the process itself. Distilled naphtha as it comes from the catalytic distillation unit contains a relatively high octane number as a result of the olefinic and aromatic compounds included in it + and in some cases; This product can contribute as much as half of the gasoline 0 in the distillation basin together with a distinct fraction of octane. One-third of the assembly produced from gasoline in the United States of America and provides the bulk of the sulfur. sulfur impurities can require separation; usually by hydrotreating; To meet product specifications or to ensure Vo's compliance with environmental regulations. Some users prefer that the percentage of sulfur in the final product be less than 00 g / m of weight 0 The most common method for separating sulfur compounds is by hydrogenation - sulfur separation HDS (hydrdesulfurization) in which distillates Petroleum petroleum passes over a solid aerosol catalyst that includes hydrogenation metal fixed 0 over an alumina base. Extra abundant amounts of hydrogen are included in the feed. The following equations describe the reactions in a typical HDS unit: Typical operating conditions for 11705 reactions are as follows: - yovy

¢ After hydrotreating is complete, the product can be fractionated or flashed easily to release the hydrogen sulfide and now collect the sulfur-free naphtha. Loss of olefins by accidental hydrogenation is determined by reducing the octane rating of the naphtha and reducing the olefins pool for other uses.

° In addition to providing high-octane tuning components, octane; The distillates of naphtha, Lie, are used as sources of olefins in other processes, for example, etherification. The conditions for the hydrotreatment of the naphtha product for desulfurization will also saturate some of the olefinic compounds in the octane-reducing product and cause losses in the olefins source to be extracted.

Ve, various proposals have been made to separate sulfur while preserving the most demanding olefins 0 since the olefins in the distilled naphtha are mainly in the low-boiling product of those naphtha products and the sulfur-containing impurities tend to concentrate in the product Je boiling The most common solution is pre-distilled prior to the hydrogenation treatment. Pre-distillation produces light-boiling naphtha which boils in the range of products consisting of *0 carbon atoms of approximately 1170 C and heavy-boiled naphtha which boils in the range of approximately 71 1om-1raa compounds The predominant light or less boiling sulfur is mercaptans, while the heavier or less boiling compounds are thiophenes or other mixed cycling compounds. Separation by distillation only will not separate the mercaptans. Previously, the mercaptans were separated by oxidation processes involving washing with caustics. Compatibility of oxidative separation of the mercaptans followed by distillation and hydrotreatment of the heavier product has been discussed in US Patent No. 7. at the oxidative separation of the mercaptans; The mercaptanes convert to the corresponding disulfides. Yo US Patent No. 804997476 discusses a two-stage process in which naphtha is fed into a first distillation column reactor that functions as a depentanizer or hexane separator since the lighter material contains the majority of olefins and mercaptans (Yovy)

mercaptans that boil in the scope of the first distillation reaction, as the mercaptans interact with diolefins to form sulfides, which separate at the bottom in parallel with any higher-boiling sulfur compounds. The bottom products were subjected to hydrogenation - sulfur separation in a second distillation column reactor where the sulfur compounds were converted to 8:11 and separated. ° The use of two or more catalytic hydrogenation treatments - sequential sulfur separation is practiced for the treatment of petroleum feeds to separate organic sulfur compounds ‎organic sulfur ¢ In any case, in those previous treatments there is a distinct amount of "recombinant sulfur" in the product. Recombinant sulfur means new organic sulfur compounds; particularly the mercaptans; Formed by the reverse reaction of 11:8 of Adee hydrogenation - - pre-sulphurization or hydrogenation - desulphurization in hydrogenation processes 0 in the feed. 1128 The following sulfur separation olefins can be incorporated by means of olefins

H, S which increases the amount of sulfur in the product. Also + the presence of mercaptans to form mercaptans and consume octane can cause more 5-olefins to saturate to lose octane. Of course it has a lower sulfur content than the feed containing a lower treatment ¢ but each subsequent treatment has a lower efficacy than would be expected due to the recombinant sulfur. in the current process; The effectiveness of the post-treatment is increased by separating 1155 of the treated feed before the feed passes into the subsequent hydrogenation - desulfurization. 7 Among the advantages of the present invention is that the naphtha stream with a full boiling rate is graded - the sulfur is separated while the olefin content remains at a higher percentage than the original feed by hydrogenation - sequential sulfur separation with a separation of 11:8 after each hydrogenation - Jai sulfur HpS is not believed to separate hydrogenation-desulfurization in serial hydrogenation-desulfurization processes in the former field; But rather practice. The previous one separates 11:5 after hydrogenation - the final sulfur separation Yo 1 lah:

The general ha oll of the invention In the broader context, the present invention is represented in a process of hydrogenation - sulfur separation hydrodesulfurization of petroleum feed containing petroleum organic sulfur compounds and with preference to olefins through at least two consecutive treatments © to feed through Contact with hydrogen in the presence of a hydrogenation catalyst - Separation of sulfur to convert part of the organic sulfur compounds to 11:5 Cus. The improvements are 11:9 separation of the feed after each treatment. In an embodiment of the present invention; Full-boiling range Bal is subjected to a two-step process to separate the organic sulfur by hydrogenation - Jad 0 sulfur. In the first step - full-boiled naphtha, the sulfur is separated in the distillation column reactor, which acts as a separation unit. The superproduct of light hydrogenated and sulfur-free naphtha is taken in parallel with the 11:5 product in the reactor. The distinctive part of the 11:8 separates from the upper output assembly/separation unit. The heavier product is treated with hydrogenation and sulfur separation and is separated as bottom products. Bottom products and top products and then fed into a separation unit 11:5 10 as the rest of the HS is separated from the sulfur-free naphtha. The benthic products from the HS separator are then fed into a second reactor (either a standard single-pass reactor or a second distillation column reactor). Chapter 11:5 is employed for two purposes. It prevents the formation of recombinant organic sulfur compounds and allows less dangerous conditions to separate the same sulfur while preventing the hydrogenation of olefins. and preferably; The organic sulfur content of the stream, Jaa 0, is less than or c/m by weight. as used here; The term “distillation column reactor” means a distillation column that also contains a catalyst so that the reaction and distillation are simultaneously in the column. in a preferred embodiment; The catalyst is a pany in the form of a distillation structure and serves as both a catalyst and a distillation structure. YO A brief explanation of the drawings - Figure No. 1 is a flow diagram in graphic form using two hydrogenation reactors - straight-pass double-pass sulfur separation in sequence and includes a 14.9 separation between the two reactors. Yovy

- Figure No. 1 is a flow diagram in graphic form using two hydrogenation reactors - separating sulfur in series; The first is a catalytic distillation reactor which has two scales hydrogenation-sulfur separation; one for the product of the lightest and one for the heaviest; It is treated separately and then combined in a separator for 9:11 separation before going to a straight-pass hydrogenation-separating sulfur unit. Detailed description Feeding in the process includes output from petroleum containing sulfur, especially from the fluid bed catalytic distillation unit (FCCU) that boils in the boiling range of gasoline (a product composed of carbon atoms up to 471 Degree Fahrenheit). fan of the olefinic material, and unless the raw source is “acid”, very little sulfur. The sulfur content in the catalytic distillates will depend on the 1 sulfur content in the feed to the distillation unit in addition to the boiling rate of the selected product used As a feedstock for the process Lighter products will have lower sulfur contents than higher boiling ones The front end of naphtha contains most of the high octane olefins but relatively little sulfur The sulfur components in the front end are mainly mercaptans Typically, these compounds are 0 :- methyl mercaptan (boiling point Y=degree Fahrenheit) ¢ ethyl mercaptan (boiling point 1 M0) normal propyl mercaptan n-propyl mercaptan (boiling point 1.4 m) ¢ iso-propyl mercaptan (boiling point ov,Y m Te ¢) » iso-butyl mercaptan ( Boiling point AYA m tert-butyl mercaptan (boiling point 9, ? m) “N-butyl mercaptan Yo (boiling point 997.8 +) 0 sec-butyl mercaptan GUS yo (boiling point 5 um)” iso-amyl mercaptan (boiling point 171 m + amyl (sale) mercaptan n-amyl mercaptan (glyp point 11.1 ¢) ' Yovy

Alpha-methylbutyl mercaptan (glycine grade 11.1 ¢) ' alpha-ethylbutyl mercaptan (glycine grade Veo ¢) 'n-hexyl mercaptan (boiling point 190.1 C) “¢ -1 mercapto hexane -2 (boiling point 00607 C); and -0 mercapto hexane © -3 (boiling point oV, Y ¢(. Typical sulfur compounds found in the highest boiling product include heavier mercaptans « thiophenes » - sulfides and disulfides. The reaction of organic sulfur compounds in The distillation stream with hydrogen over the catalyst to form 11:5 is typically called hydrogenation - hydrodesulfurization 0. Hydrodesulfurization is the broadest term which includes the saturation of olefins and aromatic compounds and the reaction of organic nitrogen compounds to form ammonia 0 at any rate. However, hydrogenation-desulfurization includes Lally easily referred to as hydrotreating catalysts that are useful for the hydrogenation-desulfurization reaction include Group VIII metals eg cobalt ¢ nickel nickel; palladium ¢ alone or in combination with other metals for example molybdenum or tungsten on a suitable support which may represent alumina; Silica - alumina - titania - zirconia ¢ or the like. Sale Metals are available in the form of oxides of metals supported over extrusions or pellets and as they are, Ye will not be considered useful for distillation structures. Catalysts may additionally contain components from the fifth and sixth b metals of the periodic table, or mixtures thereof. Group VIII metal provides increased total activity medium. Catalysts containing a metal of the sixth group B over J, for example molybdenum, and the eighth group, for example, cobalt or nickel, are preferred. Suitable catalysts for the hydrogenation-sulfurization reaction include cobalt — molybdenum a gia gall » nickel - molybdenum » and nickel - tungsten. Metals are generally found in the form of oxides supported on top of the Yovy base

neutral eg alumina; silica - alumina; or something like that . Metals are reduced to sulfides either upon use or before use by exposure to sulfur-containing currents.

Characteristics of a typical hydrogenation-desulfurization catalyst are shown in Table 1 below.

° Table No. 1, metal, weight 7

The catalyst is typically in extruded form containing a diameter of 1/01 CAN or 1/77 of an inch and an L/D ratio of 1.0 to 10.

The catalyst also can be in the form of pellets contained on the same diameters. In the regular form it forms a very compact mass and preferably in the form of a catalytic distillation structure, Aig.

0 Catalytic distillation must be able to be employed as a catalyst and as a mass transfer medium. structures

Catalytic distillations useful for this purpose are discussed in US Patents Nos. 1 9771779 + 471044 and 7547© which are incorporated by attribution.

The use of the distillation reaction system (catalytic distillation) reduces inertia and provides for longer operation than in fixed bed hydrogenation units and is considered preferable for the first reactor. column reactor

0 Distillation is uniquely used for the reaction of sulfur compounds with heavier or higher boiling points. The upper pressure Lad is kept close to 0-0 psig YO with a corresponding temperature in the distillation reaction range of 4.4 10°C - 0.7271°C. Partial pressures of hydrogenation equal to 0 = Veo psia can be used. In one of my favorite incarnations; The partial pressure of hydrogen is equal to yovy

01 0) is used. General partial pressures of hydrogen in the range of 0, + +0 psia provide ideal results. The second reactor can become a single-pass gas phase bottom flow reactor because the majority of the sulfur compounds have been separated. Because 11:8 and more of the hard Sse© sulfur has already been separated – the reactor can be operated under more moderate conditions; For example, at approximately 7010 2810 pressure; The temperature of the SYN reactor and the instantaneous spatial velocity of the liquid are .03 when a second distillation column is used; The lower total pressure in the range from Yo to less than 01 psig "requires for hydrogenation - sulfur separation and partial pressure of hydrogen Ve equals less than 1500 psi and preferably as low as even 0.1 psi can Use with preference approximately 0-11 psi The temperature in the distillation reaction range is in the range of 054 “M. Hydrogen in the Jolie second distillation column is fed in the range of 11-01 standard cubic feet) (SCF/lb of feed). The normal instantaneous spatial velocities of the liquid (volume of liquid in the feed/unit volume of catalyst) in the second column are in the range 0-Y No. Typical conditions in the second reaction range (second and subsequent columns ) for the distillation and hydrogenation column reactor - naphtha sulfur separation is as follows: - Operation in the distillation column reactor produces both the liquid phase and the vapor phase within the scope of the distillation reaction. The considered part of the vapor is hydrogen, while a part is a vapor hydrocarbon of petroleum product The actual separation can only 0 be taken into secondary consideration

AR

Without limiting the intent of the present invention; It is suggested that the mechanism proposed to produce the efficiency of the hydrogenation in the distillation column reactor represents the condensation of part of the vapors in the reaction system; Which retains enough hydrogen in the condensed liquid to obtain the required contact between and as a . hydrogenation hydrogen and sulfur compounds in the presence of the catalyst to produce hydrogenation concentrated in 11:8 olefins in particular; The sulfur species are concentrated in the liquid while the olefins are 0 in the vapor, allowing for a high conversion of sulfur compounds with a low conversion of the olefin species. The result of running the process in the distillation column reactor is that lower pH partial pressures (and thus lower total pressures) can be achieved. used. As in any distillation; There is a temperature gradient within the distillation column reactor. The temperature at the lower end of the column contains 0 material with a higher boiling point and thus is at a higher temperature than the upper end of the column. lowest boiling point; which contains more sulfur compounds left separable; exposure to lower temperatures at the top of the column which provides for greater selectivity; that required. The higher part olefin lower hydrogen distillation or saturation of olefinic compounds Cua in the boiling point is exposed to higher temperatures at the lower end of the distillation column reactor Ve . For open distillation of cyclic sulfur-containing compounds and hydrogenation of sulfur between the two reactors there is a 11:5 separator unit that effectively separates all 11:5 product from the first column. This prevents contact between 1155 and the olefins with the catalyst and the resulting formation of recombinant compounds and allows for less hazardous conditions in the second organic sulfur reactor. In order to separate the sulfur itself while preventing the hydrogenation of the olefins YS, a graphic flow diagram of one of the embodiments of the invention 1 was shown, with reference now to Figure No. 01, via line 01 fed into the first fixed-bed single-pass reactor naphtha Gad. The current contains 01 via the flow line * . reactor 01 and hydrogen fed into reactor 1 flow; Part of 01 of hydrogenation catalyst - suitable sulfur separation. In the first reactor 11 on the layer of organic sulfur compounds it reacts with hydrogen to form 11:5 . Conditions in the first Yo reactor are mediated by hydrogenation-sulphurization measurements. For example; the temperature psig 61-050 is in the range from 7897.8*C - 0.5107C; The pressure is in the range of yovy

Hand and the instantaneous spatial velocity of the liquid (11157) is in the range from *H-10 [LAE] catalyst volume. The degree of sulfur separation is therefore somewhat lower than usual; Approximately 7906. The flow from the first reactor 01 is fed into the first separation column Yo as the HS and excess hydrogen is separated out in the overhead products by the flowline; . The condensable © materials in the overproducts are condensed in the condenser YY and separated from 11:5 and the hydrogen in the separator YY . The excess of hydrogen and 11:5 are separated by flow line 11 . The condensate is returned to the separator as returns via the flow line AY Bottom outgrowths from the separator 71 are fed into a second single-pass fixed bed reactor 0 via the flow line © where complementary hydrogen is fed into the reactor Yo by

0 flow line 1 . The Yo reactor contains a second layer, YY, of hydrogenation catalyst - suitable sulfur separation. Conditions in the second reactor are set to provide the required degree of sulfur separation. The flow from the second reactor 71 is fed into the second separator 0; whereupon the surplus of hydrogen and 11:8 produced in the second reactor 71 is separated out with the overhead products via flow line A . second ; The condensables in the upper products are condensed in capacitor 411

V0 is separated from the hydrogen and AHS separator 47 and returned to the second separator through a flow line 14 in the form of reflux. The excess of hydrogen and 1125 dal by flow line 14 . The final product is separated as a bottom product by flow line 9. Whereas, HS separates reactors; The milder conditions can be used in the second reactor, thus the olefins will not be subjected to hydrogenation conditions.

a Referring now to figure No. Y, a second embodiment of the present invention has been shown as the first reactor is a distillation column reactor 01 containing two layers 11a and 11b in a hydrogenation catalyst - sulfur separation in the form of catalytic distillation constructs. Naphtha is fed between the layers via flow line 1 and hydrogen is fed through flow line 7. Because the catalytic distillation column can be operated at lower pressures, fewer olefins will saturate. Land;

Yo, the catalytic distillation column is more effective when hydrogenating heavy sulfur compounds, for example, thiophenes and benzthiophenes. Catalytic Distillation Separation of naphtha into a mild bubbling product is achieved in as little as 2171.1 m;

1 lah

VY

And a heavy product that boils above a degree of approximately 1070 m. Light naphtha is taken as an overproduct of . Produced in HS layers by flow line; In parallel with the increase of hydrogen and the majority of, as the vapors; 01 and gather in the separator © 0 condensable substance condensed in the condenser, part of the liquid. 11 has 11.5 and more hydrogen; Separated by line No. Lay as reflux via flow line No. 01 The condensate is refluxed in the distillation column reactor © . 010 The remainder of the liquid overhead is fed into the upper part of the separating column. 0, but in 71 is also fed into the separating column, Yo, bottom products from the distillation column reactor, 3. The lower range, through the flow line, the number of materials. 11 The upper products through the flow line number AHS separation column are separated where YY and collected in the separation device 71 condensable in the upper products condensed in the condenser 0 separated from the excess of hydrogen and 11:5 . The excess of hydrogen and 11:5 separate from, while the liquid returns to the separator in the form of reflux via 11 through the flow line. 9 flow line 77 . The final product is separated as bottom products via the flow line via the flow line © and is fed to the reactor 01 The bypass stream is taken from the separator of the hydrogenation catalyst - sulfur separation 1 containing layer 71 stabilized layers single-pass 1 The lighter organic sulfur reacts with hydrogen is appropriate since the organic sulfur compounds are fed through the flow line 01 from the reactor. 1 Gaal which is fed by line towards the £0 flashing barrel as hydrogen and 11:8 flashes from the flow and the YY flow is carried out by means of the 7 flowline; . The liquid from the 71 barrel is fed into the upper part of the separator

Cua £1 by flow line 01 flash is fed into the middle section of the separator Ye . That 11:58 residue is separated from the product 1 thl No.: distilled with a full boiling rate that includes the following characteristics first treated in naphtha naphtha grams of cobalt/molybdenum catalyst criterion D 11.77 catalytic distillation column Containing commercially placed in catalyst structures as DC-130 cobalt/molybdenum catalyst 01 1-Yes Yo Discussed in US Patent No. 0770849 Regulated in Qatar Usual? inches in two bands of yovy

V¢ is inserted between the hydrocarbon feet of the catalyst above the feed point. Hydrocarbon feed 00 columns of the two catalytic layers. PZ to provide psig 7700. The catalytic distillation column operates at an upper pressure equal to Ulla. The catalytic layer heat equals 7444 “C. Operated catalytic distillation column 0 (olefins sulfur separation as 757,147 losses in bromine number (loss in olefins 795.7 0 785) Data from a commercial single-stage fixed-bed hydrogenation processor shows that approximately 757,147 sulfur losses are produced at the same rate of sulfur separation . bromine # olefin 1 lah

E11 Only the upper products from the catalytic distillation column separate (HLS and excess from mie) and then treated in a conventional two-stage single-pass fixed bed polishing reactor containing the same catalyst under the following conditions: 17 dtr A rate is obtained A combined sulfur fraction of 97.7 7 with a loss of only 747.4 in olefins. The SY two-stage refinement reactor can also be operated under very mild conditions. This clearly shows that the selectivity of the two-stage process as operated according to the present invention is comparable to that of the single-stage process. example number? The feed as described in Example 1 is processed in a distillation column reactor according to Example 0 1. Only the superproducts are separated 5:11 and excess hydrogen and treated under the following conditions 0 | In the polishing reactor to achieve naphtha containing Nia YV by weight. The hydrogen rate hydrogen dtp with Co set ch of total saturation 8 is 798.97 . The olefin saturation is 751.8. Data from a commercial single-phase stabilized bed unit show that approximately 797 olefins are expected to be lost at the same rate as sulfur separation. yovy

Example No. 0 Naphtha distilled containing the following characteristics is treated in a catalytic distillation column according to Example No. 1 containing criterion catalyst DC VF em cobalt / molybdenum DC-130 cobalt/molybdenum catalyst commercial as a description. The catalytic distillation column is operated at an upper pressure of 140 psig, providing a constant bed temperature of 1077 °C. A catalytic distillation column operated alone yielded 794,948 chapters in sulfur with 765.15 losses in olefins anyway; The total sulfur percentage is approximately YE c/m by weight 0 : Lalah 1

For the combined top and bottom products, 11.8 and the excess hydrogen are separated and treated under the following conditions in the polishing reactor to achieve naphtha containing only 1 g/m of weight 0 FIT saturation of the combined olefins 54 at the transformation of Sulfur 189,Y ssh Data from a commercial single-stage fixed bed hydrogenation processor show that a loss of ~6 olefin is expected at the same sulfur separation rate. Yovy

Claims (1)

YA Protection Elements 1-1 Process for hydrotreatment - separation of sulfur hydrodesulfurization _ of a stream of distilled ¥ cracked naphtha comprising the following steps: = (i y feeding hydrogen and a stream of naphtha containing Compounds: organic sulfur and Jelia olefins Distillation column containing Js Hydrogenation - hydrodesulfurization catalyst ¢ § b) at the same time concurrently in the said distillation column reactor; (1) v Contacting the aforementioned distilled naphtha and hydrogen dl hydrogen 2553 A with a hydrogenation catalyst - sulfur separation treatment in 4 hydrogenation conditions - hydrodesulfurization treatment Thus, part of the aforementioned organic sulfur compounds reacts with hydrogen 4 to form (HLS). The conditions mentioned are such that the mentioned olefins remain unsaturated VY; and (1) 0 Separation of said naphtha into a low-boiling product of less than approximately 1.271.1 M; and a heavy-boiling product above approximately Ca YY (V0) c) removing the said light product as overproducts from the aforementioned distillation column reactor 0 in parallel with 1155 and unreacted hydrogen; 1 d) Separation of removing said heavy product as bottom products from said distillation column reactor; VA e) Combining the aforementioned heavy product and the light product to form a first combined product and separating 4 11.8 from it; 0 and) feeding part of the first combined product after 11:58 separation to a fixed layer reaction zone yy single pass containing a hydrogenation catalyst and sulfurization catalyst vy as part of the organic sulfur compounds The remaining organic sulfur reacts with hydrogen to yield 1125 and yield a second combined product; ve g) disconnect HS removing from the second merged output mentioned in step f); And ‎Yovy (z Yo) Extracting, recovering the product stream that actually contains less v1 organic sulfur compounds than the aforementioned distilled naphtha stream. 1 7- The process according to Claim No. 1, where That the second combined output in step g) combines 7 with the first combined output and pu class 1158 . -Y 1 Process according to claim 01; Whereas, the content of Cay yr SH organic sulfur in the second stream reductant 1128 is less than *0 g/m by weight. 1 +- process according to claim 1; Cus that the hydrogenation catalyst - hydrodesulfurization catalyst v mentioned includes a metal of group VIII JVI = o 1 process according to claim no.; ; Whereas, the mentioned hydrodesulfurization catalyst | includes a metal of group V 7. 1 +- the lip process of claim No. ©; Whereas, the mentioned hydrogenation catalyst - hydrodesulfurization catalyst — ¥ includes metal of group 7b VIB. 1 #- the ly operation of claim no.; ; © or 6; Whereas, the said Jaci sulfur hydrodesulfurization catalyst includes the .oxide 1 +- process pursuant to claim No. 4; © or 6; Cum that hydrogenation catalyst - hydrodesulfurization catalyst mentioned above includes sulfide .1 4- Process for hydrogenation - hydrodesulfurization catalyst treatment of distilled ¥ stream of naphtha comprising the steps add) :— (Iv hydrogen feed hydrogen and a stream of naphtha containing sulfur compounds; organic sulfur and olefins in the distillation column reactor containing a catalyst are hydrogenation - hydrodesulfurization catalyst ¢ 1b at the same time in said distillation column reactor ¢ 7 ) \ (contacting naphtha Gigi) distilled | Mentioned 5 and the aforementioned hydrogen and hydrogen gene with M Hs _ hydrogenation - treatment of sulfur separation under hydrogenation conditions - treatment of sulfur separation 1 lah a Hydrodesulfurization catalyst 4 Thus, part of the aforementioned organic sulfur compounds reacts with hydrogen to form 11:5 ¢ and (Y) yy Separation of said naphtha into a low-boiling product of less than approximately 1711°C; yy and heavy product boiling over approximately Ca VY c) Separation of said light product as overhead from said distillation column reactor in parallel with HS | 14 and unreacted hydrogen ¢ vo d) Separation of said heavy product as bottom products from said distillation column reactor; 11 e) Combine the said heavy product and the light product to form a first combined product and separate HS from it; 1 f) Feeding part of the first combined product after separating the HS to a single layer stabilizer reaction zone yA passage containing a hydrogenation catalyst and treating the hydrodesulfurization catalyst 14 as part of the remaining organic sulfur compounds Reacts with 70 -_ hydrogen to produce 1155 and yields a second fused product; vy g) detach HS from the second merged product mentioned in step f); And yy h) Extract the product stream that actually contains less organic sulfur compounds yy than the mentioned distilled naphtha stream. -01 10 Process in accordance with claim 4; Whereas, the content of organic sulfur 0 in the second stream reduced HS is less than 50 g/m by weight. -11-1 Operation ly of claim No. 4; Whereas, the hydrogenation catalyst - hydrodesulfurization catalyst 0 mentioned includes metal of group VII All -11-0 the process according to claim No. 11; Cum that the hydrogenation catalyst - hydrodesulfurization catalyst declining includes metal 26181 of the fifth ©“ group 7. VY) process according to claim 17; Whereas, the mentioned hydrogenation catalyst - hydrodesulfurization catalyst ~~ ¥ includes metal of group © B VIB 1 lalah EN Whereas the hydrogenation catalyst - treatment 17 or 17 11 The process according to Claim No. 14-1. The aforementioned oxide includes hydrodesulfurization catalyst sulfur separation ¥ that the hydrogenation catalyst - treatment Cun VY or 11 101 of claim No. ly Process -1#© 01 Said sulfide includes hydrodesulfurization catalyst ¥ YoVvyY