How hydrodesulfurization of crude oil, the method of hydrodesulfurization crackerandoj naphtha(options)

 

Usage: oil refining and petrochemical industry. Essence: are hydrodesulfurization flow of crude oil, which absorbs a very small amount of olefins. The method is a two-stage process, where N2S removed between stages of the pipeline to prevent the formation of recombinant mercaptans. In another aspect of the invention are hydrodesulfurization crackerandoj naphtha as described above. Technical result: to achieve high levels of desulphurization with less loss of olefins. 3 N. and 6 C.p. f-crystals, 1 tab., 2 Il.

The present invention relates to a method of desulphurization catalytically crackerandoj the full range naphtha boiling through the reaction of hydrogen with available raw organic sulfur compounds in the presence of catalysts of hydrodesulfurization. In particular, the present invention can use the stage catalytic distillation, which reduce the sulfur content to very low levels, makes more efficient use of hydrogen and causes less hydrogenation of olefins in the case of naphtha stream full diapause flows characterized by their boiling ranges, which determine the composition. Processing flows also affects the composition. For example, products, processes or catalytic cracking or thermal cracking contain a high concentration of olefinic substances, as well as saturated compounds (alkanes) and polyunsaturated substances (diolefins). In addition, these components can be any of the various isomers of these compounds.

On the composition of the raw naphtha derived from petroleum cube, or fractions of naphtha straight race, primarily influenced by the source of crude oil. Nafta sources of paraffin oil contains more saturated linear or cyclic compounds. The General rule is that a large part sweet (low-sulfur) crude oil and naphtha is paraffin. Naphthenic crude oil contains more unsaturated, cyclic and polycyclic compounds. Crude oil with higher sulphur content tend to be naphthenic. Recycling of different fractions of naphtha straight race may slightly vary depending on their composition due to a source of raw materials.

Subjected to reforming naphtha or the product of the reforming process typically requires no further obrabotkata reforming nafta essentially no sulfur due to the rigidity of its pre-treatment process and the process itself.

Crakereanda naphtha produced in the catalytic cracking installation, has a relatively high octane number because it contains olefinic and aromatic compounds. In some cases, this fraction can make such a big contribution, which is half of the gasoline pool in processed together with a significant part octane.

Material catalytically crackerandoj naphtha boiling range of gasoline currently forms a significant part (~1/3) of the pool of gasoline product in the United States and he gives the greatest proportion of sulfur. Impurities of sulfur may require removal of typically the Hydrotreating to meet the product specifications or to ensure compliance with the regulations on the protection of the environment. Some consumers want the sulfur content in the final product would be below 50 wt.h/million

The most common method of removing sulfur compounds is hydrodesulfurization (HDS), when the oil distillate is passed over a solid catalyst in the form of particulates, comprising hydrogenating metal supported on a carrier of alumina. Raw materials include additional significant amounts of hydrogen.

The following equations illustrate the reactions in a typical installation of HDS:

img>RH+HCl

(3) 2RN+4H2RH+NH,

(4) ROOH+2H2RH+H20

Typical working conditions for HDS reactions are:

Temperature,°F 600-780

Pressure, psi wt. 600-3000

The rate of recirculation of H2, STD.a cube. ft/bbl 1500-3000

Replenishment of fresh N2, STD. cubic feet per barrel of 700-1000

After Hydrotreating the product can be divided into fractions or simply overtake, to highlight the sulfide and collect desulfurizing naphtha. The loss of olefins accidental hydrogenation is harmful because of the reduction of the octane number of naphtha and reduction in the pool of olefins for other applications.

In addition to supplying high-octane mixed components, crakereanda nafta is often used as a source of olefins in other processes such as esterification. Conditions for Hydrotreating a naphtha fraction to remove sulfur will also satiate a certain amount of olefinic compounds in the faction, lowering the octane number and causing the loss of a source of olefins.

Have been made various proposals in order to remove sulfur, at the same time keeping more olefins. Because olefins MESI tend to concentrate in high-boiling fraction, the most common solution was a pre-fractionation prior to Hydrotreating. Preliminary fractionation gives a naphtha boiling range of the light naphtha which boils in the range from C5up to 250° F and naphtha boiling range of heavy naphtha which boils in the range from about 250-475°F.

Prevailing light or a low-boiling sulfur compounds are mercaptans, while more severe or high-boiling compounds are tifany and other heterocyclic compounds. Division one fractionation will not remove the mercaptans. However, in the past mercaptans were removed oxidative ways, including alkaline leaching. The combination of oxidative removal of mercaptans, followed by fractionation and Hydrotreating heavier fractions is described in U.S. patent 5320742. Under oxidative removal of mercaptans mercaptans converted into the corresponding disulfides.

U.S. patent 5597476 describes the two-stage method, in which the naphtha fed to the first distillation column reactor, which operates as panchanathan column or hexanolactone column, and a lighter material, containing the most su the comfort with diolefine with the formation of sulfides, which are removed in nedogona with more high boiling sulfur compounds. Ndogoni expose hydrodesulfurization in the second distillation column reactor, where the sulfur compounds are converted in N2S and removed.

The use of two or more consecutive treatments catalytic hydrodesulfurization implemented for processing of crude oil in order to remove organic sulfur compounds, however, in these prior processes, the product has a large number of “recombinant” brimstone." Under recombinant grey understand the new organic sulfur compounds, primarily mercaptans, which are formed in the reverse reaction of N2S from the preceding hydrodesulfurization or hydrodesulfurization in subsequent processes hydrodesulfurization with olefins contained in raw materials. H2S can recombine with the formation of mercaptans, thus increasing the amount of sulfur in the product. In addition, the presence of H2S can cause a greater saturation of olefins, leading to loss of octane number and flow rate of hydrogen.

Product serial processes multilayer desulphurization of course has a lower content serials, because of the sulfur, the resulting recombination.

In this way the efficiency of subsequent processing was increased by the Department of H2S from the processed raw material before the raw material supply for the subsequent hydrodesulfurization.

The advantage of the present invention is that the flow of the full range naphtha boiling put hydrodesulfurization, while there is a high percentage of olefins on the content in the feedstock by sequential hydrodesulfurization with the removal of H2S after each stage of hydrodesulfurization. It is believed that H2S was not removed between treatments hydrodesulfurization at successive stages of hydrodesulfurization in the prior art, but rather the earlier practice was to remove the H2S after the final hydrodesulfurization.

SUMMARY of the INVENTION

In the broad context of the present invention relates to a method of hydrodesulfurization oil feedstock containing organic sulfur compounds and preferably olefins, at least two successive treatments of the raw materials by contact with hydrogen in the presence of a catalyst hydrogensulfate removal of the N2S of the raw material after each of the specified handle.

In one embodiment, the implementation in practice of the present invention the full range naphtha boiling subjected to a two-stage process for removal of organic sulfur compounds by hydrodesulfurization. In the first stage, the full range naphtha boiling subjected to desulfurization in a distillation column reactor, which acts as a Stripping column, discharging to the upper shoulder straps hydrodesulfurizing light naphtha with formed in the reactor H2S. Significant proportion of H2S removed from top of shoulder strap receiver/separator. The heavier fraction is subjected to hydrodesulfurization and removed in the form of ledogorov. Ndogoni and upper shoulder straps then served in the column for desorption of H2S, where the remainder of N2S is separated from desulfurizing naphtha. Ndogoni of columns for the separation of N2S then fed to the second reactor (or standard reactor with a single pass or second distillation column reactor). Removal of N2S serves two purposes. It prevents the formation of recombinant organic sulfur compounds and allows the use of less stringent conditions for the same sulfur removal, the same is the means of distillation column, which also contains the catalyst, so that the column for simultaneous reaction and distillation. In a preferred embodiment, the catalyst is prepared in the form of patterns for distillation and it serves as a catalyst and as a structure for distillation.

BRIEF DESCRIPTION of DRAWINGS

Fig.1 is a process flow diagram in simplified form, using two reactor hydrodesulfurization with straight design, which are arranged one behind the other, and where N2S is removed between the two reactors.

Fig.2 is a process flow diagram in simplified form, using two reactor hydrodesulfurization, which are arranged one behind the other, and the first is a catalytic distillation reactor having two zones of hydrodesulfurization, one for the lighter fraction and one for the more high-boiling, which are processed separately, then combined in the Stripping column for removal of H2S before serving in the installation of hydrodesulfurization with direct aisle.

DETAILED DESCRIPTION

Raw materials for the process include sulfur-containing petroleum fraction, such fraction from catalytic cracking fluidized bed (FCCU), the cat is the boiling range of naphtha products from a catalytic cracking installation, because they contain the desired olefins and undesirable sulfur compounds. The naphtha fraction straight race contains very little of the olefinic material, and if the source of crude oil is not “sour”, very little sulfur.

The sulfur content in the fractions subjected to catalytic cracking, will depend on the sulfur content in the feedstock to the cracking installation, as well as from the boiling range of the selected fraction, used as raw material for the process. Lighter fractions will have a lower sulfur content than the high-boiling fraction. Head naphtha fraction contains most of the high octane olefins, but a relatively small amount of sulfur. Sulfur compounds in the head of the faction, mainly represent the mercaptans and typical compounds are methyl mercaptan (TKip.43° F), ethyl mercaptan (TKip.99°F), n-propylmercaptan (TKip.154° F), isopropylparaben (TKip.135-140°F), isobutylparaben (TKip.190°F), tert-butylmercaptan (TKip.147°F), n-butylmercaptan (TKip.208°F), second-butylmercaptan (TKip.203°F), isoamylalcohol (TKip.250°F), n-arylmercury (BP. 259°F),-methylbutyrate (TKip/sub>304° F), 2-mercaptohexyl (TKip.284° F) and 3-mercaptohexyl (TKip.135° F). Typical sulfur compounds found in more high-boiling fraction, include heavier mercaptans, tifany, sulfides and disulfides.

The reaction of organic sulfur compounds in the recycle stream with hydrogen over the catalyst with the formation of H2's usually called hydrodesulfurization. Hydrotreating is a broader term that includes the saturation of olefins and aromatics and reaction of organic compounds of nitrogen with the formation of ammonium. However, hydrodesulfurization it turns on and sometimes it is simply referred to as Hydrotreating.

Catalysts that are useful for the reaction of hydrodesulfurization include metals of group VIII such as cobalt, Nickel, palladium, alone or in combination with other metals such as molybdenum or tungsten, on a suitable carrier, which may be an alumina, silica - alumina, Titania - Zirconia or similar. Usually metals are present as oxides of the metals deposited on the extrudates or spheres, and as such, they generally are not useful as a framework for distillation.

D. the art. Metals of group VIII give increased secondary activity. The catalysts containing metals of group VIB, such as molybdenum and group VIII such as cobalt or Nickel are preferred. Catalysts suitable for the reaction of hydrodesulfurization include cobalt-molybdenum, Nickel-molybdenum and Nickel-tungsten. Generally, metals are present in the form of metal oxides deposited on a neutral substrate, such as alumina, silica - alumina or similar. The metals are reduced to sulfide or the use of, or prior to use, the influence of streams containing sulfur.

Properties typical catalyst hydrodesulfurization shown in the table below.

Typically the catalyst is in the form of extrudates having a diameter of 1/8, 1/16 or 1/32 inch and L/D of 1.5 to 10.

The catalyst can also be in the form of spheres having the same diameter. In the case of the correct form, they form too compact mass, and preferably get them in the form of patterns for catalytic distillation. Structure for catalytic distillation must be able to work as a catalyst and medium for Massape is 6, 5431890 and 5266546, which are incorporated here by reference.

Using system reactive distillation (catalytic distillation) reduces decontamination and gives longer cycles than installing hydrogenation with a fixed layer, and it is preferable for the first reactor. The distillation column reactor favorably used for the reaction more severe or more high-boiling sulfur compounds. The pressure of the upper support straps from approximately 0 to 250 psi wt. with the appropriate temperature in the reaction zone of the distillation equal to between 400 and 700° F. you Can use the partial pressure of hydrogen of 0.1 to 70 psi abs. In one preferred embodiment, use of the partial pressure of hydrogen from 0/1 to 10 lb/sq. in. abs. Generally, the best results are obtained by the partial pressure of hydrogen in the range from 0.5 to 50 lb/sq. in. abs.

The second reactor may be a vapor-phase reactor with a single downward pass, since most of the sulfur was removed. Since H2S and more difficult sulphur compounds have already been removed, the reactor can operate under milder conditions, for example at a pressure of about 200 lbs/sq. which the distillation column, for hydrodesulfurization require a lower total pressure in the range of from 25 to less than 300 pounds per square inch gage. and the partial pressure of hydrogen of less than 150 pounds per square inch, preferably can be used up to 0.1 pound per square inch, preferably from about 15 to 50 pounds per square inch. The temperature in the reaction zone of the distillation is in the range from 400 to 750° F. the Hydrogen to the second distillation column reactor serves in the range from one to ten standard cubic feet (SCF) per pound of feedstock. Rated average velocity of the fluid (liquid volume of feedstock per volume of catalyst) in the second column are in the range 2-5.

Typical conditions in the reaction zone of the distillation (the second and following columns) distillation column reactor to hydrodesulfurization naphtha are:

The temperature of 450-700° F

The total pressure of the 75-300 psi wt.

The partial pressure of H26-75 lb/sq. in. abs.

Average hourly space velocity of naphtha Approximately 1-5

Speed H210-1000 STD. cubic feet/barrel

The operation of the distillation column reactor leads to the formation of both liquid and vapor phase in the reaction zone of the distillation. A significant part of the pair represents the giving can be achieved only with additional consideration.

Without limiting the scope of the invention, it is assumed that the mechanism that gives the efficiency of hydrogenation in the distillation column reactor is a condensation of a part of the vapors in the reaction system, which absorb a sufficient amount of hydrogen in the condensed liquid to obtain the necessary close contact between the hydrogen and the sulfur compounds in the presence of a catalyst, leading to their hydrogenation. In particular, the sulfur compounds are concentrated in the liquid, while the olefins and N2S concentrate in the vapor phase, giving high conversion of sulfur compounds with low conversion of compounds of olefins.

The result of the way in the distillation column reactor is the possibility of using lower partial pressures of hydrogen (and thus a lower total pressure). As in many cases, distillation, inside the distillation column reactor there is a temperature gradient. In the lower part of the column contains more high-boiling material and, thus, it is at a higher temperature than in the upper part of the column. The fraction, boiling at a lower temperature, which contains more easily removable sulfur compounds, is niche hydrocracking or saturation necessary olefinic compounds. More high-boiling part is exposed to higher temperatures in the lower part of the distillation column reactor to reveal a sulfur-containing cyclic compounds and gidrirovanii sulphur.

Between the two reactors is the column for the separation of N2S, which effectively removes the entire product H2S of the first column. This prevents contact of N2S and olefins with the catalyst and the formation of recombinant organic sulfur compounds, and enables the use of less severe conditions in the second reactor with the same removal of sulfur, at the same time preventing the hydrogenation of olefins.

In Fig.1 shows a simplified process flow diagram of a variant of implementation of the invention. Naphtha is fed to the first reactor with a fixed bed and a single passage 10 through the pipeline 1, a hydrogen fed into the reactor 10 through line 2. The reactor 10 contains a layer 11 of a corresponding catalyst hydrodesulfurization. In the first reactor 10 part of the organic sulfur compounds react with hydrogen with the formation of H2S. Conditions in the first reactor are mild by the standards of hydrodesulfurization. For example, the temperature of the náchod fluid (LHSV) is in the range from 5 to 10 volumes of naphtha by volume of the catalyst. The degree of desulphurization thus somewhat smaller than normal, about 95%.

Coming from the first reactor 10 flows into the first Stripping column 20, where N2S and the excess hydrogen is separated in the upper shoulder straps through the pipeline 4. Condensable materials in the upper shoulder straps are condensed in the condenser 21 and are separated from the H2S and hydrogen in the separator 22. The excess hydrogen and H2S is removed through pipe 12. The condensed material is returned to the Stripping column as phlegmy through pipe 13.

Ndogoni of Stripping column 20 serves in the second reactor with a fixed bed and a single passage 20 through the pipe 5 with the addition of hydrogen fed to the reactor 20 through the pipeline 2. The reactor 20 contains a second layer 21 of the respective catalyst hydrodesulfurization. Conditions in the second reactor is adjusted, to provide the desired degree of desulfurization. The exit stream from the second reactor 20 serves the second Stripping column 40, where the excess hydrogen and N2S, formed in the second reactor 20, is separated together with the upper shoulder straps through the pipeline 8. Again condensable materials in the upper shoulder straps are condensed in to the pipe 14 in the form of phlegmy. The excess hydrogen and N2S remove the pipe 14. The final product is removed in the form of ledogorov pipeline 9. Since H2S remove between the reactor, the second reactor can be used milder conditions, and, thus, the olefins are not exposed to conditions of hydrogenation.

Consider now Fig.2. It shows the second variant of the invention, where the first reactor is a distillation column reactor 10 containing two layers 11a and 11b of the catalyst hydrodesulfurization in the form of structures for catalytic distillation. Naphtha is served between layers through the pipeline 1, and the hydrogen is fed below the layers through the pipeline 2. Because the catalytic distillation column can be operated at lower pressures, you will be satisfied a smaller amount of olefins. In addition, the catalytic distillation column is more effective in the hydrogenation of heavy sulfur compounds, such as tifany and benzothiophene. Light naphtha is taken as the top straps through the pipe 4 together with the excess hydrogen and the greater part of H2S, formed in layers. Condensable material condense in the condenser 50 and is collected in the category of liquids are returned to the distillation column reactor 10 in the form of phlegmy through pipe 13. The remaining portion of the liquid upper straps are served in the upper part of Stripping column 20. Ndogoni from the distillation column reactor 10 also serves in the Stripping column 20, but in the lower part, via line 3.

A Stripping column, separates the N2S in the upper shoulder straps through the pipeline 15. Condensable materials in the upper shoulder straps condense in the condenser 21 and collected in the separator 22, where they are separated from the excess hydrogen and N2S. the Excess hydrogen and N2S is removed from the separator through the pipe 16, while the liquid is returned to the Stripping column as phlegmy through the pipeline 23. The final product is removed in the form of ledogorov pipeline 9.

The side zipper is withdrawn from the Stripping column 20 through pipe 5 and fed into the reactor 30 single pass fixed bed containing layer 31 of a suitable catalyst hydrodesulfurization, where the lighter organic sulfur compounds react with hydrogen, which is fed through the pipeline 6. The exit stream from the reactor 20 is served by pipeline 32 in the evaporative drum 40, where the hydrogen and H2S is distilled off from the exit stream and served in the upper part of Stripping column 20 through the pipeline 42. The liquid from the evaporative drum product.

EXAMPLE 1

Crakereanda the full range naphtha boiling, with the following characteristics, first treated in a catalytic distillation column containing 11032 g commercial cobalt/molybdenum catalyst Criterion DC-130, placed in the form of a catalytic structure as described in U.S. patent 5730843 located with a nominal diameter of 3" in two sections 50 foot columns from 15.1 feet of catalyst below the point of entry of raw materials and 18.7 feet of catalyst above the point of entry of raw materials. Hydrocarbons lead between two layers of catalyst.

Description of raw materials

Total sulfur 2086 mg/l

Total nitrogen 64 mg/l

Bromine number 52

Density 0,8005 g/cm3@ 15,66°C

ASTM D-2887 Distillation

5% 160°F

10% 174

20% 205

30% 231

40% 258

50% 283

60% 320

70% 338

80% 382

90% 419

95% 442

Catalytic distillation column operates at a pressure of the upper shoulder strap 230 psi wt., giving the temperature of the catalyst layer 570°F. Catalytic distillation column reactor, working alone, makes the removal of sulfur 96.7% of the loss of the bromine number (loss olefins) 46,47%. Data commercial single-stage apparatus for Hydrotreating fixed bed show that approximately 85% loss olefinic only the upper shoulder straps and then processed in a traditional reactor purification of fixed bed and a single pass of the second stage, containing the same catalyst under the following conditions:

Average hourly feed rate of the oil 8

The rate of hydrogen to 113.4 STD. cubic feet/gallon

The average temperature of 470°F

A pressure of 200 pounds per square inch gage.

The total degree of desulphurization, equal 97,2%, so the loss of olefins, equal only to 43.4%. Perhaps in very mild conditions. This clearly shows the selectivity of the two-stage process of the present invention in comparison with the one-stage process.

EXAMPLE 2

Raw materials, as described in example 1, processed in the distillation column reactor of example 1. Only the top shoulder straps separated from the N2S and excess hydrogen and processed under the following conditions in the reactor purification to achieve naphtha containing 27 wt.h/million:

Average hourly feed rate 8

The feed rate of hydrogen 104 STD. cubic feet/barrel

The average temperature of 510° F

The pressure of 275 pounds per square inch gage.

Total saturation of the olefins 51,5%

Full conversion of S equal 98,96%. The saturation of the olefins is 51,5%.

Data from the commercial one-step installation with a fixed layer show that we should expect a loss of about 92% of the olefins with the same level of desulfurization.

ment of the column in example 1, containing commercial cobalt/molybdenum catalyst Criterion DC-130, as described.

Description of raw materials

Total sulfur 1554 mg/l

Total nitrogen 132 mg/l

Bromine number 30,5

Density 0,8288 g/cm3@ 15,66°C

ASTM D-2887 Distillation

5% 195°F

10% 229

20% 265

30% 288

40% 322

50% 336

60% 362

70% 384

80% 399

90% 412

95% 428

Catalytic distillation column reactor operates at a pressure of the upper shoulder strap 195 psi wt., giving the temperature of the catalyst layer 590°F. Catalytic distillation column reactor, working alone, makes the removal of sulfur 98,98% loss of olefins 66,15%. However, the total sulfur content equal to 24 wt.h/million

United top zipper and nedohin is separated from the N2S and excess hydrogen and processed under the following conditions in the reactor purification to achieve naphtha, containing only 7 h/million by weight:

Average hourly feed rate of the oil 12

The rate of hydrogen 88 STD. cubic feet/gallon

The average temerature 510°F

Pressure 230 psi wt.

Total saturation of the olefins 67,4% conversion of sulfur to 99.7%

Data commercial single-stage apparatus for Hydrotreating fixed bed show that the loss would occur olefins approximately 95% is Ursachi of crude oil, containing organic sulfur compounds, at least two successive treatments of the raw materials by contact with added fresh hydrogen on each of these sequential treatments in the presence of a catalyst of hydrodesulfurization for the conversion of organic sulphur compounds in the H2S, where N2S removed from the raw material after each of the specified handle.

2. The method according to p. 1, where two treatments are consistent.

3. How hydrodesulfurization flow crackerandoj naphtha, which includes stages a) feeding hydrogen and naphtha stream containing organic sulfur compounds and olefins in a first reaction zone containing a suitable catalyst hydrodesulfurization, under conditions suitable for reaction of organic sulfur compounds with hydrogen with the formation of H2S; (b) the filing of the exit stream from the specified first reaction zone to a distillation zone where some of the listed H2S removed from the first stream with reduced content of N2S; (c) the filing of the specified first stream with reduced content of N2S and fresh hydrogen in a second reaction zone containing a suitable catalyst hydrodesulfurization, under conditions suitable for Uhodyashego stream from the specified second reaction zone of the distillation stage b), where the part of the said H2S is removed to obtain a second stream with a reduced content of N2S, have further reduced the content of organic sulfur compounds, compared with the specified naphtha stream and a first stream with a reduced content of N2S.

4. The method according to p. 3, where this first reaction zone includes a catalyst hydrodesulfurization in this form to provide simultaneous reaction and distillation of the reaction mixture indicated the flow of naphtha and products hydrodesulfurization.

5. The method according to p. 4, including the supply stream from the specified second reaction zone of the distillation stage (b), where some of the listed H2S is removed by formation of the second stream with reduced content of N2S, have further reduced the content of organic sulfur compounds, compared with the specified naphtha stream and a first stream with a reduced content of N2S.

6. The method according to p. 3, where the conditions are such as not to contribute to the saturation of the olefins contained in the specified nafta.

7. The method according to p. 3, where the content of organic sulfur compounds from the second stream with reduced content of N2S is less than 50 wt. h/million

8. SP is holding organic sulfur compounds and olefins, in the distillation column reactor containing a catalyst desulfurization; (b) simultaneously in the specified distillation column reactor, provide (1) the contact specified crackerandoj naphtha and the specified hydrogen with the specified catalyst hydrodesulfurization under conditions of hydrodesulfurization, whereby a portion of these organic sulfur compounds react with the specified hydrogen with the formation of H2S, and these conditions are such that these olefins remain unsaturated; and (2) separation of the specified naphtha into a light fraction boiling below about 250°F, and a heavy fraction boiling above about 250°F; (c) remove the specified light fraction in the form of upper straps from the specified distillation column reactor together with H2S and unreacted hydrogen; (d) the deletion of specified heavy fraction in the form of ledogorov from this distillation column reactor; (e) the consolidation of specified heavy fraction and the light fraction to obtain the first combined fractions and subtracting from the H2S; (f) the filing of the first combined fractions after removal of the N2S in the reaction zone of a fixed bed and a single pass containing the catalyst GidroMash to obtain a second combined fractions; (g) removing the N2S from the specified second combined fractions from the stage (f); and (h) obtaining the product stream, which contains much less organic sulfur compounds than the specified thread crackerandoj naphtha.

9. The method according to p. 8, where the second pooled fraction from stage (g) combine with first United faction and remove the H2S.



 

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