Production of diesel fuel and plant to this end

FIELD: process engineering.

SUBSTANCE: invention relates to method of diesel fuel production. Particularly, it pertains to compression of makeup hydrogen flow in compressor to bleed hydrogen flow from said compressed makeup hydrogen flow. Hydrocarbons flow is subjected to hydro cracking in the presence of hydrogen flow and catalyst to get outlet hydro cracking products flow to be separated in liquid flow and vapour flow to be compressed to get hydrogen compressed flow. Liquid outlet flow is fractionated to obtain diesel fuel flow. Hydrogen flow is bled for hydraulic cleaning from said compressed hydrogen flow for hydraulic cleaning of diesel fuel flow in the presence of hydrogen flow and catalyst to get outlet hydro cracking products flow. Invention covers also the diesel fuel production plant.

EFFECT: perfected process.

10 cl, 2 dwg

 

This application claims the priority of applications for U.S. patent No. 13/076608, filed March 31, 2011, the U.S. No. 13/076631, filed March 31, 2011, the U.S. No. 13/324186, filed December 13, 2011, and U.S. No. 61/549978, filed on October 21, 2011

The technical field to which the invention relates.

The invention relates to the production of diesel fuel by hydrocracking.

The level of technology

Hydrocracking refers to the process in which the hydrocarbons are subjected to cracking in the presence of hydrogen and catalyst to reduce the molecular weight hydrocarbons. Depending on the desired performance of the hydrocracking zone may contain one or more layers of the same catalyst or different catalysts. Hydrocracking is a process used to kikirevenge hydrocarbon feedstocks such as vacuum gas oil (VGO), with diesel fuel, including kerosene and fuel for gasoline engines.

Generally to devices for carrying out the catalytic cracking process in the fluidized bed (FCC) or other process unit carry out the mild hydrocracking to improve the quality of crude oil, which can be directed in the downstream installation, and at the same time carry out the conversion of part of the raw materials to produce lighter products, still is as a diesel fuel. As global demand for fuel for diesel engines is increasing with respect to fuel for petrol engines, mild hydrocracking is considered in order to offset the yield of products in the preferred direction of diesel fuel in the reduction of yield of gasoline. Soft cracking can be carried out in less than hard mode, compared to the hydrocracking is carried out with a partial or full conversion of hydrocarbons, in order to match the production of diesel fuel with the possibilities of the installation for carrying out the cracking process in the fluidized bed of catalyst, which is used mainly to obtain naphtha. Hydrocracking with partial or complete conversion of the hydrocarbons used for the production of diesel fuel with less output neprevyshenie oil, which can be directed in the installation located downstream.

For environmental reasons and according to the newly introduced rules and regulations commodity diesel fuel must meet all lower limits on impurities such substances as sulfur and nitrogen. New regulations require essentially complete removal of sulfur from diesel fuel. For example, the requirement for diesel fuel with ultra-low sulfur content is usually a sulfur content less than 10 wt.is./million

Therefore, there is a continuing need for improved methods of production of diesel fuel from a source of hydrocarbon raw materials in larger quantities, than produced amount of gasoline. Such methods must ensure that the diesel fuel meets the strict requirements for this product.

The invention

In one embodiment of the invention includes a method for the production of diesel fuel from a stream of hydrocarbons, including compressed stream make-up hydrogen compressor to receive the compressed stream make-up hydrogen. From the specified compressed stream of make-up hydrogen select a stream of hydrogen for carrying out hydrocracking. The hydrocarbon stream is subjected to hydrocracking in the presence of a stream of hydrogen for hydrocracking, and hydrocracking catalyst and get the output stream of the products of hydrocracking. At least a portion of the exit stream of the products of hydrocracking is subjected to fractionation to obtain a flow of diesel fuel. The flow of diesel fuel is subjected to Hydrotreating in the presence of a stream of hydrogen for Hydrotreating and Hydrotreating catalyst to obtain the exit stream of the product Hydrotreating.

According to another embodiment of the method of the invention also includes a breakdown of the exhaust products is tov hydrocracking to vapor output stream of the products of hydrocracking, containing hydrogen, and a liquid exit stream of the products of hydrocracking. Vapor output stream of the products of hydrocracking is compressed to obtain a compressed stream containing hydrogen. The compressed hydrogen-rich stream selected hydrogen-rich stream to the Hydrotreating.

According to another alternative embodiment of the method of the invention also includes a breakdown of the exhaust products Hydrotreating to vapor exiting product stream Hydrotreating containing hydrogen, and a liquid exit stream products Hydrotreating. Vapor exiting product stream Hydrotreating containing hydrogen, is mixed with the specified output stream of the products of hydrocracking.

In another embodiment relating to the method of the invention includes a method for the production of diesel fuel from a stream of hydrocarbons, including compressed stream make-up hydrogen compressor to receive the compressed stream make-up hydrogen. Compressed stream make-up hydrogen is additionally compressed in the compressor recycle gas and get compressed stream of hydrogen. The compressed stream of hydrogen selected stream of hydrogen for hydrocracking. The flow of hydrocarbons is subjected to hydrocracking in the presence of a stream of hydrogen for hydrocracking, and hydrocracking catalyst to obtain the exit stream of product is hydrocracking. At least a portion of the exit stream of the products of hydrocracking is subjected to fractionation to obtain a flow of diesel fuel. The flow of diesel fuel is subjected to Hydrotreating in the presence of a stream of hydrogen for the Hydrotreating catalyst Hydrotreating, and get the output stream products Hydrotreating.

According to another embodiment relating to the method of the invention also includes a method for the production of diesel fuel from a stream of hydrocarbons, including compressed stream make-up hydrogen compressor to receive the compressed stream make-up hydrogen. The flow of hydrocarbons is subjected to hydrocracking in the presence of a stream of hydrogen for hydrocracking, and hydrocracking catalyst to obtain the exit stream of the products of hydrocracking. The specified output stream of the products of hydrocracking is separated into vapor output stream of the products of hydrocracking containing hydrogen, and a liquid exit stream of the products of hydrocracking. Vapor output stream of the products of hydrocracking and compressed stream make-up hydrogen is compressed to obtain a compressed stream containing hydrogen. The compressed stream is selected hydrogen-rich stream for carrying out hydrocracking and hydrogen-rich stream to the Hydrotreating. Liquid exiting product stream is subjected to hydrocracking fra is to work with getting the flow of diesel fuel. The resulting flow of diesel fuel is subjected to Hydrotreating in the presence of a stream of hydrogen for the Hydrotreating catalyst Hydrotreating and get the output stream products Hydrotreating.

In accordance with another alternative embodiment relating to the method of the invention also includes a method for the production of diesel fuel from a stream of hydrocarbons, including compressed stream make-up hydrogen compressor to receive the compressed make-up hydrogen flow. Received compressed feed stream of hydrogen is compressed in the compressor recycle gas by receiving a compressed stream of hydrogen. The compressed stream of hydrogen selected stream of hydrogen for hydrocracking. The flow of hydrocarbons is subjected to hydrocracking in the presence of a stream of hydrogen for hydrocracking, and hydrocracking catalyst and get the output stream of the products of hydrocracking. At least a portion of the exit stream of the products of hydrocracking is subjected to fractionation to obtain diesel fuel. The flow of diesel fuel is subjected to Hydrotreating in the presence of a stream of hydrogen for Hydrotreating and Hydrotreating catalyst to obtain the exit stream products Hydrotreating. Finally at least a portion of the exit stream products Hydrotreating containing hydrogen, is mixed at the ore with a part of the exit stream of the products of hydrocracking.

In the embodiment relating to the device, the invention includes a plant for production of diesel fuel containing a hydrocracking reactor, which communicates with one or more compressors that are installed on the pipeline make-up hydrogen, and the pipeline for hydrocarbon and is suitable for hydrocracking flow of hydrocarbons from obtaining hydrocarbons with lower boiling temperature; compressor recycle gas which is connected with the hydrocracking reactor and is designed to compress the vapor exhaust of the products of hydrocracking containing hydrogen, to obtain a compressed stream containing hydrogen, in the pipeline recycle hydrogen; and hydrotreater unit which communicates with the pipe for compressed hydrogen and the hydrocracking reactor and is suitable for Hydrotreating flow of diesel fuel to obtain diesel fuel with low sulfur content.

According to another embodiment of the installation of the invention, furthermore, includes a warm separator that communicates with the Hydrotreating reactor and is designed for separation of exhaust products Hydrotreating to vapor exiting product stream Hydrotreating containing hydrogen discharged through the pipeline to the top of gases and liquid exit stream products gidroochistki the exhaust pipe from the bottom residue, moreover, the compressor recycle gas is communicated with the specified pipe to the top of gases.

According to another embodiment relating to a device, the invention includes a plant for production of diesel fuel using the flow of make-up hydrogen, and one or more compressors that communicate with the pipeline to the make-up hydrogen and are designed to compress the flow of make-up hydrogen; this facility also contains a pipeline for hydrocarbon raw materials, designed for carrying the flow of hydrocarbons; hydrocracking reactor, which communicates with the pipe make-up hydrogen and pipelines for hydrocarbons and is used for hydrocracking flow of hydrocarbons carried out to obtain hydrocarbons with lower boiling temperature; compressor recycle gas which is connected with the hydrocracking reactor and designed to compress the vapor exhaust of the products of hydrocracking containing hydrogen, to obtain compressed, containing hydrogen flow in the pipeline for compressed hydrogen; column fractionation, which communicates with the hydrocracking reactor and carries out the fractionation of liquid exit stream of the products of hydrocracking with getting the flow of diesel fuel, TRANS is oteruelo pipeline for diesel fuel; the Hydrotreating reactor which is connected with the compressed hydrogen and piping for diesel fuel and used for Hydrotreating the flow of diesel fuel to obtain diesel fuel with low sulfur content.

According to another embodiment relating to a device, the invention includes a plant for production of diesel fuel containing a hydrocracking reactor, which communicates with the compressor mounted on the line make-up hydrogen, and the pipeline of hydrocarbons and is used for carrying out the hydrocracking flow of hydrocarbons carried out with the aim of obtaining hydrocarbons with lower boiling temperature; compressor recycle gas which is connected with the hydrocracking reactor and piping make-up hydrogen and designed for compressing a vaporous effluent stream of the products of hydrocracking containing hydrogen, and compressed flow of make-up hydrogen from receiving the compressed stream containing hydrogen, in the pipeline for compressed hydrogen; and, finally, the Hydrotreating reactor which is connected with the compressed hydrogen and a hydrocracking reactor and used for Hydrotreating the flow of diesel fuel to obtain diesel fuel with low sulfur content.

In accordance with an alternative waples the tion, related to the device, the invention includes a plant for production of diesel fuel using the pipeline make-up hydrogen, and one or more compressors, which are communicated with the specified pipeline for make-up hydrogen and are designed to compress the flow of make-up hydrogen; this complex also contains the pipeline for hydrocarbon raw materials, designed for carrying the flow of hydrocarbons; hydrocracking reactor, which communicates with the pipe make-up hydrogen and pipelines for hydrocarbons and is used for hydrocracking flow of hydrocarbons carried out to obtain hydrocarbons with lower boiling temperature; compressor recycle gas which is connected with the hydrocracking reactor and is designed to compress vapor the exit stream of the products of hydrocracking containing hydrogen, to obtain the compressed stream containing hydrogen, in the pipeline for compressed hydrogen; column fractionation, which communicates with the hydrocracking reactor and carries out the fractionation of liquid exit stream of the products of hydrocracking with getting the flow of diesel fuel to be transported by pipeline for diesel fuel; and Hydrotreating reactor which is connected with the pipe statehoodaa and piping for diesel fuel and used for Hydrotreating the flow of diesel fuel to obtain diesel fuel with low sulfur content.

According to another embodiment relating to a device, the invention includes a plant for production of diesel fuel containing a hydrocracking reactor, which communicates with one or more compressors that are installed on pipelines make-up hydrogen, and the pipeline of hydrocarbons and is used for carrying out the hydrocracking flow of hydrocarbons to obtain hydrocarbons with lower boiling temperature; compressor recycle gas which is connected with the pipeline make-up hydrogen and a hydrocracking reactor and is designed to compress the vapor exhaust of the products of hydrocracking containing hydrogen, receiving the compressed stream of hydrogen in the pipeline for compressed hydrogen; hydrotreater unit which is connected with the pipeline compressed hydrogen and a hydrocracking reactor and used for Hydrotreating the flow of diesel fuel to obtain diesel fuel with low sulphur content; the warm separator that communicates with the Hydrotreating reactor and serves to separate the exit stream products Hydrotreating to vapor exiting product stream Hydrotreating containing hydrogen discharged through the pipeline to the top of gases and liquid exit stream products Hydrotreating in the pipeline was used for SN is zu residues; when this compressor recycle gas communicates with the pipeline for top exhaust gases.

Brief description of drawings

Figure 1 - simplified process flow diagram for an embodiment of the present invention.

Figure 2 is a simplified process flow diagram for an alternative embodiment of the present invention.

Definition

The term "communication" means that the operation of the installation between the listed components of the installation is ensured by the material flow.

The term "message downstream" means that the operation of installing at least part of the material passing to the object can pass from the object to which it is reported the specified object.

The term "message upstream" means that the operation of installing at least part of the material passing from the subject, can be carried to the object with which it is reported the specified entity.

The term "column" means a distillation column or columns that are designed to separate from the processed material of one or more components with different volatility. If not otherwise specified, each column above includes a capacitor which is used for condensing and returning part of the exhaust on the top of the thread back up the column, and in the lower part of the column boiling ilnik for evaporation and a part is allotted to the bottom of the flow back into the lower part of the column. Raw materials are sent into the columns can be preheated. The pressure at the top of the column represents the pressure of the vapor discharged from the top of the column. Waste temperature is a target temperature of the bottom liquid. Pipelines for the upper thread and the piping to the bottom of the stream belong to the network of pipelines running from the column below in the direction of flow from the return phlegmy or return flow in the column on boiling.

Used herein, the term "true boiling point" (TBP) refers to a method of testing to determine the boiling point of the material, which corresponds to ASTM D-2892 for the production of liquefied natural gas, distillate fractions and a residue of standard quality, the results of which can be obtained analytical data, and define the output of the above fractions by mass and volume. The results of these tests get a graph of the temperature dependence subjected to distillation mass (in wt.%), based fifteen of theoretical plates in the column with multiplicity irrigation 5:1.

Used herein, the term "conversion" means the conversion of raw materials into material that boils at a temperature in the temperature range of the boiling point of diesel fuel or at lower temperatures. Border boiling fraction from the distillation range of diesel is about fuel is in the range of 343° to 399°C (650° to 750°F), using the method for determining the fraction of the true boiling points".

Here, the term "diesel boiling range fuel" means hydrocarbons boiling in the range from 132° to 399°C (270° to 750°F), and when determining this interval using the method of determining the fractional composition on "the true boiling points".

Detailed description of the invention

Reactors for carrying out mild hydrocracking work in enough hard mode and, therefore, provide an insufficient degree of conversion. Diesel fuel produced in the mild hydrocracking, is of insufficient quality to meet the existing technical requirements for fuels, in particular in relation to the sulphur content. In this regard, the diesel fuel produced by a soft cracking, can be processed in the plant for Hydrotreating, so that it can be added to the finished ready to use diesel fuel. In many cases it may be attractive to combine the installation for mild hydrocracking and installation for Hydrotreating to reduce capital and operating costs.

Traditional installation for carrying out the hydrocracking contains cold separator and cold evaporative capacity is. Often, but not always, the installation includes a hot separator and hot evaporative capacity. Traditional hydrocracking unit contains only a cold separator. Cold separator can be operated at lower temperatures to obtain optimum separation of the hydrogen that is to be used as a gas recycle, but it is thermally inefficient, because subjected to hydrobromide liquid stream for subsequent fractionation is necessary to re-heat to get diesel fuel with low sulfur content.

To avoid cooling and re-heating subjected hydrobromide liquid flow and that it did not affect the process of separating hydrogen and a Hydrotreating unit used in parallel with the hydrocracking unit with a common compressor recycle gas and a cold separator. After compression the flow of recirculating gas share for submission to each setting. Make-up gas may be added to the flow of recirculating gas is higher in the direction of flow from the compressor recycle gas. Make-up gas may be added upstream from the compressor recycle gas in order to use this compressor for compressing gas containing hydrogen is supplied to the hydrocracking reactor and react the R Hydrotreating.

Installation for Hydrotreating can use the hot separator to extract the hot liquid product, and then combining the vapor phase effluent stream products Hydrotreating with the output flow of the products of hydrocracking. Such a scheme is that the process allows for Hydrotreating and hydrocracking to work at the same pressure. In addition, the vapor leaving the flow of the products of hydrocracking may be directed to a cold separator for further separation of hydrogen from hydrocarbons to obtain the recirculating gas. For liquid product stream Hydrotreating withdrawn from the warm separator, there is no need for re-heating to such an extent as it has done before fractionation. In addition, the liquid product stream Hydrotreating contains primarily diesel fuel with low sulfur content, so the process of fractionation of diesel fuel with low sulfur content simpler.

The invention includes a breakdown of all the make-up gas and recycle gas between hydrocracking and hydrotreatment. Adding make-up gas in the hydrocracking unit is preferred because the feedstock for hydrocracking reactor will usually have a high content of CR is destinia coke, that will lead to a higher rate of deactivation of the catalyst and reduce its service life. The use of make-up gas to increase the partial pressure of hydrogen in the hydrocracking reactor will contribute to more effective hydrocracking.

Installation and method 8 for the production of diesel fuel include a compressor section 10, the installation of 12 hydrocracking, installation of 14 units with an area of 16 fractionation. Hydrocarbons first goes to the 12 hydrocracking, where it is transformed into hydrocarbons of lower boiling point, such as diesel fuel. Diesel fuel is subjected to fractionation on a plot of fractionation and sent to the installation of 14 Hydrotreating to obtain diesel fuel with lower sulphur content.

The flow of make-up hydrogen is transported through the pipeline 20 to the make-up hydrogen is sent to the unit consisting of one or more series-connected compressors 22 installed on the compressor section 10, intended to increase the pressure of the flow of make-up hydrogen and compressed feed stream in the pipe 26. Compressed feed stream passing through the pipe 26 to compressed make-up hydrogen may be combined with the vapor goes through the eye of the products of hydrocracking, containing hydrogen transported by pipeline 42, obtaining supplied to the compression of hydrogen flow in the pipe 28. Compressed stream make-up hydrogen may be added in gaseous output stream of the products of hydrocracking at some point upstream from the compressor 50 so that, with respect to the pipeline 26 for compressed make-up hydrogen compressor 50 recirculating gas will be above the stream from each reactor hydrobromide, such as the reactor 36 hydrocracking, or reactor 92 hydrobromide. Accordingly, the gap between the pipe 26 for compressed make-up hydrogen compressor 50 recirculating gas there is no reactor hydrobromide.

Supplied to the compression of a stream of hydrogen in the pipe 28, formed from the combined flows of compressed make-up hydrogen and vaporous upcoming products of hydrocracking, may be subjected to compression in the compressor 50 recirculating gas by receiving a compressed hydrogen-rich stream that can be transported by pipeline 52 for compressed hydrogen containing compressed gaseous output stream of the products of hydrocracking. The compressor 50 recirculating gas may be provided downstream from the reactor 36 hydrocracking, the pipeline 20 make-up hydrogen and one or more of compr is sorow 22.

In one embodiment, the compressed stream of make-up hydrogen may be added to the pipe 52 with the compressed hydrogen-rich recycle stream below along the flow path from the compressor 50 recirculating gas. However, the pressure of the compressed hydrogen stream in the pipe 52 may be too high for mixing with stream make-up hydrogen without the use of additional compressors installed on lines 20 make-up hydrogen. Accordingly, it may be advantageous to add the compressed stream make-up hydrogen in the gaseous output stream of the products of hydrocracking, passing through the pipe 42, upstream from the compressor 50 recirculating gas, despite the increase in performance of the compressor 50 recirculating gas due to the increase in the total number of noise material. Adding the compressed stream make-up hydrogen upstream from the compressor 50 recirculating gas, however, can negate the need for an additional compressor 22 on lines 20 make-up hydrogen.

Compressed hydrogen-rich stream is transported through a pipeline 52, may be divided into separate 54 into two streams. The first hydrogen-rich stream to the hydrocracking is directed to a separator 54 of the compressed hydrogen is Otok, transported by pipeline 52 compressed hydrogen, and sent to the first branch 30 of the pipeline. The second hydrogen-rich stream to the hydrocracking is directed to a separator 54 of the compressed hydrogen-rich stream that can be transported by pipeline 52 compressed hydrogen, and send the second branch 56 of the pipeline for hydrogen. The first branch 30 of the pipeline for hydrogen upstream communicates with the reactor 36 hydrocracking, and the second hydrogen-rich stream for Hydrotreating in the second branch 56 of the pipeline is reported upstream reactor 92 Hydrotreating.

Stream with hydrogen for Hydrotreating in the first branch 30 of the pipeline is taken from the compressed hydrogen-rich stream that can be transported by pipeline 52, may be combined with the stream of hydrocarbon material passing through the pipe 32, to obtain the flow of feedstock to hydrocracking in the pipeline 34.

Compressed stream make-up hydrogen is transported through the pipe 26 can also be combined with the compressed hydrogen-rich recycle stream downstream from the separator 54, and the make-up hydrogen will be directed to meet the needs in the hydrogen reactor 36 hydrocracking or reactor 92 hydrobromide, not filled with recirculating flow of hydrogen in the pipe 52. If a compressed stream modpython the first hydrogen pipeline 26 is combined with the compressed hydrogen-rich recycle stream above the hike flow from separator 54, the make-up gas can be directed in the installation of 14 Hydrotreating, and the installation of 12 hydrocracking.

The flow of hydrocarbons is introduced into the pipe 32, for example, through an intermediate surge tank. According to one aspect of the described method and installation, in particular, are effective for hydrobromide hydrocarbon feedstock. Examples of such hydrocarbons include hydrocarbon streams containing components boiling at temperatures above 288°C (550°F), such as atmospheric gas oils, vacuum gas oil (VGO), neasfaltirovanyj residues by vacuum distillation, and distillation at atmospheric pressure, the coking distillate, the distillate direct distillation, solutions deasphalting oils, distillates coking, pyrolysis oil, high boiling synthetic oils, cycle oils, hydrocracked oil feedstock purification, the distillate of the catalytic cracking and the like. This is going to hydrocarbons may contain sulfur in an amount of from 0.1 to 4 wt.%.

Suitable hydrocarbon feedstock is a VGO or other suitable hydrocarbon fraction containing at least 50 wt.% and, as a rule, at least 75 wt.% components boiling at temperatures above 399°C (750°F). Typical VGO usually has a boiling point in which intervale from 315°C (600°F) up to 565°C (1050°F).

Hydrocracking refers to the process in which there is a break bonds in molecules of hydrocarbons in the presence of hydrogen with a lower molecular weight hydrocarbons. The reactor 36 hydrocracking downstream communicates with one or more of the compressors 22 installed on the pipeline 20 make-up hydrogen line 32 for hydrocarbons. The flow of feedstock to hydrocracking in the pipe 34 may exchange heat with the output flow of the products of hydrocracking passing through the pipe 38, and then may be heated in the firing heater before entering the reactor 36 hydrocracking for carrying out the hydrocracking flow of hydrocarbons from the receipt of hydrocarbons having a lower boiling point.

The reactor 36 hydrocracking may contain one or more cameras, a large number of layers of catalyst in each cell and various combinations of catalyst Hydrotreating and hydrocracking catalyst in one or more chambers. In some aspects, the hydrocracking reaction provides a General conversion of hydrocarbons, at least 20% vol. and, typically, more than 60% vol. obtaining products boiling at temperatures below the boiling point of the fractions of diesel fuel. The reactor 36 hydrocracking can work with partial conversion, making up more than 50 is b.%, or with deep conversion of at least part of 90% vol. raw materials on the basis of full conversion. To obtain the maximum amount of diesel fuel effective deep conversion. The first camera or the layer in the reactor may contain a catalyst for Hydrotreating carried out with the aim of demetallization, desulfurization or diazotoluene raw materials hydrocracking.

The reactor 36 hydrocracking can work in the mild hydrocracking. The conditions are mild hydrocracking, will ensure total conversion of hydrocarbons from 20 to 60 vol.%, preferably from 20 to 50 vol.% obtaining products boiling at temperatures below the boiling point of the fractions of diesel fuel. When implementing mild hydrocracking products yield conversion is shifted towards the production of diesel fuel. When the reactor mode for mild hydrocracking Hydrotreating catalyst plays exactly the same or a greater role in the conversion than the catalyst hydrocracking. Conversion, passing across the Hydrotreating catalyst may be a significant part of the overall conversion. If the reactor 36 hydrocracking is designed for mild hydrocracking, it is assumed that the reactor 36 mild hydrocracking can be downloaded completely Hydrotreating catalyst or a catalyst GI is rocking, or a certain number of layers of catalyst for Hydrotreating and hydrocracking catalyst. In the latter case, the layers of the hydrocracking catalyst can generally follow the layers of the Hydrotreating catalyst. Most often three layers of the Hydrotreating catalyst may be preceded by one or two layers of catalyst for hydrocracking, or previous layers of catalyst for hydrocracking are absent.

The reactor 36 hydrocracking, shown in figure 1, contains in one reaction chamber four layers of catalyst. If it is desirable conduct for mild hydrocracking, in this case, provided that the first three catalyst layer contains a catalyst for Hydrotreating, and the last catalyst bed contains a catalyst for hydrocracking. If you would prefer partial or deep hydrocracking may be used for the additional layers of catalyst for hydrocracking in relation to the number of layers of catalyst when carrying out mild hydrocracking.

In conditions of mild hydrocracking feedstock selectively turns with heavy products, such as diesel fuel and kerosene at low yield of light hydrocarbons such as naphtha or gas. Pressure also choose moderate to limit the hydrogenation of the cubic product to the optimum level when processing, neither the e in the direction of flow.

According to one aspect, for example, if the product of the conversion of the balance of the middle distillate and gasoline, can be made soft in the first hydrocracking reactor 36 hydrocracking using a hydrocracking catalyst, based binder or on the basis of low-level zeolite combined with one or more hydrogenating metal component of group VIII or group VIB (Periodic system). According to another aspect, if the middle distillate product conversion is largely preferred in the production of gasoline, in the first reactor 36 hydrocracking can be carried out partial or deep conversion using a catalyst which contains, as a rule, the basis of the crystalline zeolite catalyst for cracking, which precipitated metal hydrogenating component from group VIII. For more hydrogenating components may be selected from group VIB to merge with the zeolite framework.

Zeolite framework of the cracking catalyst in the prior art is sometimes referred to as molecular sieves, and they are typically formed from silicon oxide, aluminum oxide and one or more capable of exchanging cations, such as sodium, magnesium, calcium, rare earth metals, etc. These principles, moreover, are characterized by the presence of the Institute of economy and management in the crystal structure of pores of relatively uniform diameter size in the range from 4 to 14 angstroms (10 -10m). It is preferable to use zeolites having a relatively high molar ratio of the silicon oxide/aluminum oxide, in the range from 3 to 12. Suitable natural zeolites are, for example, mordenite, stilbite, heulandite, ferrierite, dachiardite, chabazite, erionite and pajazit. Suitable synthetic zeolites include, for example, types B, X, Y, and L crystalline zeolites such as synthetic pajazit and mordenite. It is preferable to use zeolite crystals which have a pore diameter in the range from 8 to 12 angstroms (10-10m), with the molar ratio of the silicon oxide/aluminum oxide is from 4 to 6. One example of the zeolite preferred group is synthetic molecular sieve type Y.

Naturally occurring zeolites are usually found in the sodium form, in the form of alkaline earth metal and in a mixed form. Synthetic zeolites are almost always prepared initially in the sodium form. In any case, to use as the basis of the cracking catalyst preferably, most or all of monovalent metals - sources of zeolites have been replaced by ions of polyvalent metal and/or ammonium salt followed by heating to decomposition of ammonium ions associated with the zeolite, leaving in their place hydrogen ions and/or ion-exchange sites, which are essentially the Eski would be dictionary subsequent removal of water. Hydrogen or dictionarie" type Y zeolites of this nature are described in more detail in the patent document U.S. 3130006.

Mixed polyvalent metal - hydrogen zeolites can be prepared by ion exchange, first with ammonium salt, and then partially reverse exchange with the salt of polyvalent metal and then calcining. In some cases, as in the case of synthetic mordenite, hydrogen form can be prepared by direct treatment with an acid zeolites with alkali metal. According to one aspect of the preferred bases for cracking catalyst are those that at least 10 percent, and preferably at least 20 percent are deficient in the cation of the metal, based on the initial capacity of ion exchange. According to another aspect of the desired and stable class of zeolites is one in which at least 20 percent of the ion exchange capacity saturated with hydrogen ions.

The active metals used in the preferred hydrocracking catalysts of the present invention, as hydrogenating components are metals of group VIII, i.e. iron, cobalt, Nickel, ruthenium, rhodium, palladium, osmium, iridium and platinum. In addition to these metals in connection with them may also be used other promoter who, including the metals of group VIB, such as molybdenum and tungsten. The amount of hydrogenating metal in the catalyst may vary within wide limits. In the General case can be used any number in the range from 0.05 to 30 wt.%. In the case of noble metals, it is generally preferable to use from 0.05 to 2 wt.%.

The method of attaching a hydrogenating metal is contacting the zeolite material of the substrate with an aqueous solution of a suitable compound of the desired metal in which the metal is present in cationic form. After addition of the selected hydrogenating metal or metals, the resulting powder catalyst was filtered, dried, tabletirujut with added lubricants, binders or similar substances, if necessary, and calicivirus in air at a temperature of, for example, in the range from 371°C to 649°C (700° to 1200°R) to activate the catalyst and decompose ammonium ions. Alternatively, you might tabletroute zeolite component with the subsequent addition of the hydrogenating component and activation by calcination.

The above catalysts can be used in undiluted form, or powdered zeolite catalyst can be mixed and tabletroute together with other relatively less active catalysts, razbam is the teli or binders, such as alumina, silica gel, aluminosilicate Coeli, activated clay and the like in proportions in the range from 5 to 90 wt.%. These diluents can be used as such, or may contain a small proportion of added hydrogenating metal such as the metal of group VIB and/or group VIII. The hydrocracking catalysts promoted with additional metal may also be used in the method according to the present invention, which includes, for example, the use of aluminophosphate molecular sieves, crystalline chromosomique and other crystalline silicates. Crystalline chromaticity described in more detail in the patent document U.S. 4363718.

In accordance with one method of calculating the modal parameters of the hydrocracking may include a temperature of from 290°C (550°F) up to 468°C. (875°F), preferably from 343°C (650°F) up to 435°C (815°F), the excess pressure in the range from 3.5 MPa (500 psi) to 20.7 MPa (3000 lb/square inch (psig)), hour bulk liquid velocity (LHSV) of 1.0 to less than 2.5 h-1and the circulation rate of hydrogen from 421 to 2527 normal m3/m3oil (from 2500 to 15,000 standard cubic feet per barrel). If it is desirable conduct for mild hydrocracking, the operational parameters may include temperature of 315°C (600°F) to 441°C (825°F)overpressure online is rule from 5.5 to 13.8 MPa (from 800 to 2000 psig) or more typically from 6, 9 to 11.0 MPa (1000 to 1600 psig), clock volumetric liquid velocity (LHSV) of 0.5 to 2 h-1and preferably from 0.7 to 1.5 h-1and the circulation rate of hydrogen from 421 to 1685 normal m3/m3oil (from 2500 to 10,000 standard cubic feet per barrel).

The resulting product stream from the hydrocracking out of the reactor 36 hydrocracking through line 38. The output stream of the products of hydrocracking, transported by pipeline 38, exchanges heat with the raw material for hydrocracking supplied through the pipe 34, and in one embodiment it can be cooled before entering the cold separator 40. Cold separator 40 downstream communicates with the reactor 36 hydrocracking. Cold separator can operate at a temperature in the range from 46° to 63°C (115° to 145°F) and a pressure slightly below the pressure in the reactor 36 hydrocracking, given the differential pressure to maintain the flow of hydrogen and light gases contained in the top product of the column, and liquid hydrocarbons (under normal conditions) in the residuals of separation. Cold separator 40 provides receiving vaporous first exit stream to the hydrocracking containing hydrogen, in the pipe 42 of the upper cold vapor separator and liquid output stream to the hydrocracking in the pipe 44 for the remainder of separation. Cold separate who also has a sump for collecting water phase, exhaust pipeline 46. Vapor output stream of the products of hydrocracking transported through the pipe 42 to the upper vapor, may be subjected to washing by using a solution to remove ammonia and hydrogen sulfide as it is usually carried out before recycling the specified vapor exhaust of the products of hydrocracking containing hydrogen, the compressor 50 recirculating gas.

At least part of the exit stream 38 of the products of hydrocracking can be separated into fractions on a plot of 16 fractionation, below which flow communicates with the reactor 36 hydrocracking to produce flow of diesel fuel to be transported by the pipe 86. According to one aspect of the liquid output stream 44 of the products of hydrocracking may be subjected to fractionation on a plot of 16 fractionation. According to another aspect of section 16 of the fractionation may contain cold evaporative capacity of 48. Liquid exit stream 44 of the products of hydrocracking can be quickly evaporated in the cold evaporative capacity 48, which can operate at the same temperature as the cold separator 40, but at a lower pressure, in the range from 1.4 to 3.1 MPa MPa (200-450 psig)to obtain from a liquid flow of the products of hydrocracking of the easy flow of the liquid, ottimo the through line 62 to residues and flow light fraction withdrawn through line 64 to the upper vapor. Water flow through the pipe 46 from the cold sump of the separator can also be directed into the cold evaporative capacity of 48. The water stream obtained after rapid evaporation is extracted from the sump cold evaporative capacity 48 pipeline 66. The easy flow of the liquid withdrawn through line 62 to residues can be further divided into fractions on a plot of 16 fractionation.

Section 16 of the fractionation may contain a Stripping column 70 and 80 column fractionation. The easy flow of liquids transported by pipeline 62 for residues, can be heated and sent to the Stripping column 70. The easy flow of the liquid, which is a liquid exit stream of the products of hydrocracking, may be subjected to Stripping with water vapor coming through the pipe 72, receiving stream light fraction comprising hydrogen, hydrogen sulfide, water vapor and other gases withdrawn from the top of the column through pipe 74. Part of the flow of light fractions can be condensed and returned as phlegmy in the Stripping column 70. A Stripping column 70 can operate at temperatures VAT residue in the range from 232° to 288°C (450° to 550°F) and pressure gases removed from the top of the column, which range from 690 to 1034 kPa (100 to 150 psig). Stream VAT residue hydrocracking passing through the pipe 76, can be heated in the firing heater and directed 80 column fractionation.

Column 80 fractionation can also carry out the steaming VAT hydrocracking residue with steam entering through line 82, receiving a stream of naphtha is withdrawn from the top of the column through the pipe 84, the flow of diesel fuel is discharged through line 86 as a side fraction, and flow of crude oil withdrawn through pipe 88, which may be appropriate for further processing, for example, in the catalytic cracking process in the fluidized bed. For naphtha stream withdrawn from the top of the column through pipe 84 may be necessary to conduct additional processing before adding to the Park blends of gasoline. Typically, to increase the octane number of gasoline is necessary for carrying out catalytic reforming. For catalytic reforming is often necessary to carry out the allotted on top of the column nafta was besseren in the hydrotreatment of naphtha. According to one aspect subjected to hydrocracking naphtha can be besseren in the reactor 92 Hydrotreating, part of a Hydrotreating unit. It is assumed that additional lateral coat the Oia can be selected to provide a separate stream of light diesel fuel or kerosene, select above selection of flow of heavy diesel fuel discharged by the pipe 86. Part of the flow of naphtha is withdrawn from the top of the column through pipe 84 may be condensed and returned as phlegmy in column 80 fractionation. Column 80 fractionation can operate at temperatures VAT residue in the range from 288° to 385°C (550° to 725°F), preferably from 315° to 357°C (600° to 675°F) and at a pressure equal to or close to atmospheric. Part of the cubic product of hydrocracking may be subjected to boiling and returned to the column 80 fractionation instead of using for steam and water vapor.

In the flow of diesel fuel, designated by a pipe 86, the sulfur content is reduced, but it may not meet the technical requirement for diesel fuel with low sulfur (LSD), which is less than 50 mass/million sulfur, or demand for diesel fuel with ultra-low sulfur (ULSD), which corresponds to a sulfur content of less than 10 mass/mln, or other standards. In this regard, the fuel can be further thrown the final processing installation 14 Hydrotreating.

The flow of diesel fuel transported through the pipe 86 may be combined with the second the m stream of hydrogen for Hydrotreating, taken from the compressed hydrogen stream passing through the pipe 52 of the compressed hydrogen in the separation device 54 and transported through the second branch 56 of the pipeline for hydrogen, and as a result of this Association receive a flow of 90 raw material for Hydrotreating. In addition, the flow of diesel fuel to be transported in the pipe 86 may be mixed together with supplied raw materials (not shown). Stream 90 raw material for Hydrotreating can exchange heat with the outgoing product stream Hydrotreating transported by pipeline 94, is then heated in a fire heater and fed to the reactor 92 Hydrotreating. Accordingly, the Hydrotreating reactor downstream communicates with the section 16 fractionation, pipe 52 compressed hydrogen and the reactor 36 hydrocracking. In the hydrocracking reactor 92 the flow of diesel fuel is subjected to Hydrotreating in the presence of a stream of hydrogen for Hydrotreating and Hydrotreating catalyst, resulting in a receive output stream 94 products Hydrotreating. According to another aspect of the whole stream of hydrogen for Hydrotreating comes from pipe 52 compressed hydrogen through the second branch 56 of the pipeline for hydrogen.

The reactor 92 Hydrotreating may contain more than one camera and a number of layers of catalyst. The reactor 92 Hydra is clean, shown in figure 1, contains two layers of catalyst in the same reactor chamber. In the specified reactor Hydrotreating hydrocarbons with heteroatoms can be optionally demetilirovanny, obesity and diazotrophy. The hydrotreatment reactor can also contain Hydrotreating catalyst, which is suitable for the saturation of aromatic compounds, hydrodewaxing and hydroisomerization.

If the reactor 36 hydrocracking works as mild hydrocracking reactor, this reactor 36 hydrocracking can convert from 20 to 60 vol.% raw materials boiling at a temperature above the boiling range of diesel fuel, and to produce boiling in the boiling range of diesel fuel. Accordingly, the reactor 92 Hydrotreating can have a very low conversion rate and can be used mainly for desulfurization, if it is combined with the reactor 36 mild hydrocracking, in order to meet the requirements of fuel with ultra low sulfur diesel (ULSD).

Hydrotreating is a process in which a gas containing hydrogen, in contact with a hydrocarbon in the presence of suitable catalysts, which are active mainly to remove from the source of hydrocarbons heteroatoms, such as sulfur, nitrogen and metals. When carrying out Hydrotreating Ugledar the water with double and triple bonds can be saturated. Aromatic compounds can also be satisfied. Some Hydrotreating processes are designed specifically for the saturation of aromatic compounds. After Hydrotreating can also be achieved by reducing the cloud point of a petroleum product. The hydrocracking catalysts, suitable for use in the present invention are any known conventional Hydrotreating catalysts, including catalysts formed from at least one metal of group VIII, preferably iron, cobalt and Nickel, more preferably cobalt and/or Nickel and at least one group VI metal, preferably molybdenum and tungsten, the surface of the material media with high surface area, preferably of aluminum oxide. Other suitable Hydrotreating catalysts include zeolite catalysts, and the catalysts of noble metals selected from palladium and platinum. Within the scope of the present invention in the same reactor 92 hydrobromide can be used more than one type of Hydrotreating catalyst. The metal of group VIII is usually in the catalyst in an amount of from 2 to 20 wt.%, preferably in the range from 4 to 12 wt.%. The group VI metal will typically be present in an amount of from 1 to 25 wt.%, preferably from 2 to 25 wt.%.

Before occhialini mode parameters Hydrotreating may include a temperature of from 290°C (550°F) to 455°C (850°F), acceptable from 316°C (600°F) to 427°C (800°F) and preferably from 343°C (650°F) up to 399°C (750°F), the excess pressure in the range from 4.1 MPa (600 psig), preferably from about 6.2 MPa (900 psig) to 13.1 MPa (1900 psig), hourly space velocity of the fresh hydrocarbonaceous feedstock from 0.5 to 4 h-1preferably from 1.5 to 3.5 h-1the circulation rate of hydrogen from 168 to 1011 normal m3/m3oil (from 1000 to 6000 standard cubic feet per barrel), preferably 168 to 674 normal m3/m3oil (1000 to 4000 standard cubic feet per barrel), for raw materials containing diesel fuel, with a Hydrotreating catalyst or a combination of Hydrotreating catalysts. Installation 14 Hydrotreating combined with the installation of 12 hydrocracking, so they both operate at the same pressure, whereas the normal differential pressure.

The exiting product stream Hydrotreating transported through line 94 to exchange heat with the flow of feedstock to Hydrotreating, passing through the pipeline 90. The specified output stream products hydrobromide transported through the pipeline 94, can be divided in a warm separator 96 to receive the vaporous effluent product stream of hydrobromide containing hydrogen, in the pipe 98 vapors withdrawn from the top separator, and W is Drago flow products hydrobromide, exhaust through the pipe 100 for the remainder of the division. Vapor exiting product stream Hydrotreating containing hydrogen may be mixed with the output flow of the products of hydrocracking passing through the pipe 38, for example, before it is cooled and sent to a cold separator 40. Warm separator 96 can operate at a temperature in the range of from 149° to 260°C (300° to 500°F). The pressure in the warm separator 96 is slightly lower pressure in the reactor 92 Hydrotreating, taking into account the existing pressure differential. Warm separator can work with getting at least 90 wt.% diesel fuel and preferably at least 93 wt.% diesel fuel in the liquid flow transported through the pipeline 100. All other hydrocarbons and gases will rise up into the vapor leaving the product stream Hydrotreating the pipe 98, which is combined with the flow of the products of hydrocracking transported through the pipe 38, and can be processed in a cold separator 40 after pre-heating. When this cold separator 40 and, thus, the compressor 50 recirculating gas are reported below according to the flow pipe 98 to the upper vapor withdrawn from the warm separator. Accordingly, the contours of the recirculating gas section 12 hydrocracking and section 14 hydraotes the key have a common compressor 50 recirculating gas. In addition, at least part of the exhaust products Hydrotreating passing through the pipe 94, which is in the thread for the top gases removed then from the hot separator through the pipe 98 to the upper vapor containing hydrogen and hydrocarbons lighter than diesel fuel, is mixed with at least part of the exit stream of the products of hydrocracking transported through the pipe 38 to the products of hydrocracking.

Liquid exit stream products hydrobromide passing through the pipeline 100 may be subjected to fractionation in the Stripping column 102 Hydrotreating. In accordance with one aspect of the fractionation of the liquid exit stream Hydrotreating in the pipeline 100 may include rapid evaporation in warm evaporation vessel 104, which can operate at the same temperature as the warm separator 96, but at a lower pressure, in the range from 1.4 to 3.1 MPa MPa (200-450 psig). Thread the upper vapor discharged from the top to warm the evaporator capacity by pipeline 106 may be combined with liquid output flow of the products of hydrocracking transported through the pipe 44 to the fluid flow discharged from the bottom of the cold separator, and the combined stream can be routed to further fractionation. Accordingly, at the ore part of the exit stream products hydrobromide, containing hydrogen transported by pipeline 94, which then thread the upper vapor discharged from the top to warm the evaporator capacity on the pipeline 106, is mixed with at least part of the exit stream of the products of hydrocracking, transported by pipeline 38, which is in a liquid product stream from the hydrocracking transported through the pipe 44 to the fluid flow discharged from the bottom of the cold separator.

Liquid flux residue withdrawn from the bottom warm evaporative capacity on the pipeline 108 may be heated and sent to the Stripping column 102. Specified flux residue allotted bottom warm evaporative capacity, may be subjected to Stripping in the Stripping column 102 with the help of steam coming from the pipe 110, resulting in the receive stream of naphtha and light fractions in the pipeline 112 for top exhaust gases. The flow of naphtha and light fractions transported by pipeline 112 for top exhaust gases may be directed to the site 16 fractionation and, in particular, introduced in the Stripping column 70 at a level above the entry point of the easy flow of the liquid in the pipe 62.

The product stream containing diesel fuel, is discharged through pipe 114 for VAT residue, thus obtained diesel fuel contains less than 50 Masson sulfur and qualifies as LSD, preferably contains less than 10 mass per million of sulfur and qualifies as ULSD. It is assumed that a Stripping column 102 can operate as a fractionation column, with the boiler instead of using steam for steaming.

When working the warm separator 96 with elevated temperature to separate the largest part of the hydrocarbons lighter than diesel fuel, a Stripping column 102 Hydrotreating unit can function easier, because it does not assume the office of naphtha from lighter components and because diesel fuel is separated very small amount of naphtha. In addition, the warm separator 96 has a common cold separator 40 from the reactor 36 hydrocracking, and warmth, useful for fractionation in the Stripping column 102 remains in the outgoing product flow Hydrotreating.

Figure 2 presents an embodiment of the method and installation of 8', which uses hot separator 120 for pre-separation of the exit stream of the products of hydrocracking passing through the pipe 38'. Many of the elements shown in figure 2, have the same design, as shown in figure 1, and denoted by the same reference numbers positions. The elements in figure 2, which correspond to the elements in figure 1, but are designed differently denoted by the same numbers position, that is to 1, but is indicated by the symbol in the form of a dash (').

Hot separator 120 to install 12' hydrocracking downstream communicates with the reactor 36 hydrocracking and provides a vaporous stream of hydrocarbons withdrawn through line 122 to the upper vapor and liquid flow of hydrocarbons withdrawn through line 124 for heavy residues. Hot separator 120 operates at a temperature in the range from 177° to 343°C (350° to 650°F) and preferably from 232° to 288°C (450° to 550°F). Hot separator can operate at a pressure which is only slightly smaller than in the reactor 36 hydrocracking, taking into account the existing pressure differential between them. Vaporous stream of hydrocarbons in the pipeline 122 may be combined with the vapor output stream products hydrobromide in the pipe 98'passing from area 14' Hydrotreating, mixed and transported with him through the pipeline 126. Mixed flow through the pipe 126 may be cooled before entering the cold separator 40. Accordingly, the vaporous product stream from the hydrocracking can be divided together with the vapor output stream products hydrobromide in a cold separator 40 with getting vapor exhaust of the products of hydrocracking, containing hydrogen in the pipe 42 and the liquid exit stream is of Reducto hydrocracking in the pipeline 44, which is treated as described above in relation to the process diagram in figure 1. In this regard, the cold separator 40 is communicated downstream from the pipe 122 to the upper vapor passing from the hot separator 120 and the pipe 98' for the upper vapor passing from the warm separator 96.

The liquid flow of hydrocarbons discharged by pipeline 124 for residues, can be fractionated on the section 16' fractionation. In one aspect, the liquid flow of hydrocarbons withdrawn through line 124, may be subjected to rapid evaporation in hot evaporative capacity 130 to receive the stream of light fractions in the pipe 132 to the upper vapor and liquid flow heavy fractions in the pipe 134 for residues. Hot evaporative capacity 130 can operate at the same temperature as the hot separator 120, but at a lower pressure, in the range from 1.4 to 3.1 MPa MPa (200 to 450 psig). The liquid flow of heavy fractions transported through line 134 to residues may be subjected to a further fractionation on a plot of 16' fractionation. According to one aspect of the liquid flow heavy fractions, exhaust pipeline 134 may be introduced to the Stripping column 70 to a point located at a lower level than the feed point of the liquid stream of light fractions through line 62.

The remainder of the embodiment of the invention illustrated in figure 2, may be the same as described in figure 1, with the above exceptions.

Here is described the preferred embodiment of the present invention, including the best ways known to the inventors for carrying out the invention. It should be understood that the illustrated embodiments are only examples, and they should not be construed as limiting the scope of invention.

It is believed that the specialist in the art without further investigation, using the above description of the invention, may use the present invention in its entirety. The preceding preferred specific embodiment it should be understood, therefore, only as illustrative and not limiting in any way the remainder of the description.

In the above specification, all temperatures are given in degrees Celsius and all of the shares and interest of the mass, unless otherwise noted. The pressure provided at the outlet of the columns (separators), in particular at the outlet steam flow from columns (separators), having a number of outputs.

From the above description, the specialist in the art can easily set the essential features of the present invention without going beyond the scope and essence of the image is to be placed can make various changes and modifications of the invention, in order to adapt it to different conditions and applications.

1. Method for the production of diesel fuel from a stream of hydrocarbons, including
stream compression make-up hydrogen compressor to receive the compressed stream make-up hydrogen;
the selection of the flow of hydrogen from the specified compressed stream of make-up hydrogen;
conducting hydrocracking flow of hydrocarbons in the presence of a stream of hydrogen for hydrocracking, and hydrocracking catalyst to obtain the exit stream of the products of hydrocracking;
the separation of the upcoming products of hydrocracking to vapor output stream of the products of hydrocracking containing hydrogen, and a liquid exit stream of the products of hydrocracking;
compressing the vaporous effluent stream of the products of hydrocracking of obtaining a compressed stream of hydrogen;
the selection of a stream of hydrogen for the Hydrotreating of the specified compressed stream of hydrogen;
fractionation of the liquid exit stream of the products of hydrocracking to receive the stream of diesel fuel; and
carrying out Hydrotreating flow of diesel fuel in the presence of a stream of hydrogen for Hydrotreating and Hydrotreating catalyst to obtain the exit stream of the product Hydrotreating.

2. The method according to claim 1, further comprising separating the exit stream of products t vaporous o is handled ow Hydrotreating and liquid exit stream products Hydrotreating and mixing the vaporous effluent product stream Hydrotreating, containing hydrogen, with the output flow of the products of hydrocracking.

3. The method according to claim 1, in which the selection of the specified stream of hydrogen for hydrocracking of compressed make-up hydrogen flow includes:
compression of the specified make-up hydrogen flow in the compressor recycle gas to produce a compressed stream of hydrogen; and
the selection of a stream of hydrogen for the hydrocracking of a compressed stream of hydrogen.

4. The method according to claim 1, further comprising separating the exit stream of the products of hydrocracking in a vaporous stream of hydrocarbons and a liquid stream of hydrocarbons and further separation of the vaporous stream of hydrocarbons with getting vapor exhaust of the products of hydrocracking containing hydrogen, and a liquid exit stream of the products of hydrocracking.

5. The method according to claim 1, further comprising fractionating the liquid exit stream products Hydrotreating containing at least 90 wt.% diesel fuel, for receiving the flow of diesel fuel with low sulfur content.

6. Installation for production of diesel fuel that contains
the hydrocracking reactor, which communicates with one or more compressors that are installed on the pipeline make-up hydrogen, and the pipeline for hydrocarbon raw materials, intended for hydrocracking the and flow of hydrocarbons from obtaining hydrocarbons with lower boiling temperature;
compressor recycle gas which is connected with the specified hydrocracking reactor and is designed to compress the vapor exhaust of the products of hydrocracking containing hydrogen, to obtain a compressed hydrogen stream in the compressed hydrogen; and
the hydrotreater unit which communicates with the compressed hydrogen and a hydrocracking reactor and is suitable for Hydrotreating flow of diesel fuel to obtain diesel fuel with low sulfur content.

7. Installation according to claim 6, in which the compressor is re-circulated gas is communicated with the specified pipeline make-up hydrogen.

8. Installation according to claim 6, further containing a plot of fractionation which is connected with the hydrocracking reactor and used for fractionation of flow of the products of hydrocracking to receive the stream of diesel fuel, with a Hydrotreating reactor in communication with plot fractionation.

9. Installation according to claim 6, additionally containing warm separator that communicates with the Hydrotreating reactor and serves to separate the exit stream products Hydrotreating to vapor exiting product stream Hydrotreating containing hydrogen discharged via pipeline to the upper vapor and liquid exit stream products Hydrotreating allocated in the pipeline is an ode to residues when this compressor for recirculating gas is communicated with the specified pipe to top of vapor.

10. Installation according to claim 9, further containing a column fractionation, which communicates with the pipeline for the remainder of the warm separator and is intended for fractionation of liquid exit stream products Hydrotreating with getting the flow of diesel fuel with low sulfur content.



 

Same patents:

FIELD: chemistry.

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EFFECT: high output of the lubricating oil of high quality.

14 cl, 5 tbl, 21 ex

FIELD: oil and gas industry.

SUBSTANCE: invention refers to a hydrocracking method of hydrocarbon raw material containing 200 ppm - wt 2% of asphaltenes and/or more than 10 ppm wt of metals. The method involves hydrodemetallisation at least in two reaction zones of periodic action, which contain a hydrodemetallisation catalyst and possibly hydrodenitration; then, hydraulic cleaning to reduce content of organic nitrogen with further hydrocracking in a fixed bed and by a distillation stage.

EFFECT: invention provides a possibility of direct treatment of raw material types containing the amounts considerably exceeding known specifications; those raw material types can be treated individually or in a mixture, thus maintaining durability of a traditional cycle.

18 cl, 4 ex, 1 dwg

FIELD: chemistry.

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EFFECT: improved characteristics of products, higher conversion.

16 cl, 5 dwg, 4 tbl, 1 ex

FIELD: oil and gas industry.

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10 cl, 1 dwg, 3 tbl, 1 ex

FIELD: oil and gas industry.

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14 cl, 3 dwg

FIELD: power engineering.

SUBSTANCE: invention relates to a method for production of a high-octane component of engine fuel, including hydraulic treatment of a straight-run benzene fraction, separation of liquid products of hydraulic treatment into light and heavy fractions, isomerisation of light fraction and reforming of heavy fraction in presence of a platinum-containing catalyst with direction of excessive reforming hydrogen for isomerisation. Isomerisation is carried out in presence of a sulfate-zirconium catalyst and hydrogen, the produced isomerisate is stabilised with subsequent release of light and heavy fractions from the isomerisate by rectification, the mixture of which represents a product of isomerisate and also fractions containing n-hexane and methyl pentanes, which is recirculated in raw materials of isomerisation, the reformate released in process of heavy fraction reforming is exposed to rectification with release of a reformate fraction boiling up to 60-70°C, sent for mixing with the isomerisate prior to its stabilisation and fraction of 60-70°C-KK, mixed with the isomerisate product to product the target product.

EFFECT: reduced costs for isomerisation process together with preservation of the target product quality.

2 cl, 1 tbl, 6 ex

FIELD: oil and gas production.

SUBSTANCE: invention refers to procedure and installation for processing heavy oil raw stock wherein at least 80 wt % of compounds have temperature over 340°C. The procedure consists in the following stages: (a) hydraulic conversion in a reactor with a boiling layer of catalyst operating on a rising flow of liquid and gas at temperature 300- 500°C with conversion 10-98 wt % of a fraction having boiling temperature above 540°C; (b) division of exit flow after stage (a) into gas containing hydrogen and H2S, a fraction including benzene and, not necessarily, a fraction heavier, than the benzene fraction and the fraction of naphtha; c) hydrofining by contacting at least one catalyst and at least one fraction including benzene produced at stage (b); d) division of exit flow after stage (c) into gas containing hydrogen and at least one benzene fraction with contents of sulphur below 50 p/mln, preferably less, than 20 p/mln and more preferably less, than 10 p/mln. Stage of hydro-conversion (a) is performed at pressure P1 and stage of hydrofining (c) is performed at stage P2; difference ΔP=P1-P2 amounts to at least 3 MPa. Hydrogen is supplied at stage of hydro-conversion (a) and hydrofining (c) by means of one system of hydrogen compression with n steps.

EFFECT: reduced expenditures at maintaining rational duration of cycle of catalytic hydrofining, reduced content of sulphur.

37 cl, 2 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for hydrogenation processing of vacuum distillate, involving mild hydrocracking of vacuum distillate at high temperature and pressure in the presence of a hydrocracking catalyst, followed by extraction of diesel distillate, where the diesel distillate extracted after the mild hydrocracking is split into two streams, one of which, in amount of 10-30 wt %, is taken for mixing with the initial vacuum distillate, and the other, in amount of 90-70 wt %, is taken for further hydrofining to obtain the desired diesel fuel.

EFFECT: reducing content of sulphur in the obtained diesel fuel to less than 50 ppm according to the Euro-4 standard and less than 10 ppm according to the Euro-5 standard.

4 cl, 5 ex

FIELD: power industry.

SUBSTANCE: paraffin hydrocracking method is described, in which the reactor with fixed layer is provided with catalytic reaction zone in which the first catalytic layer contains the first amorphous solid acid, the second catalytic layer contains zeolite and the third catalytic layer contains the second amorphous solid acid, which are located in such an order; paraffin has to flow in direction from the first catalytic layer to the third catalytic layer in zone of catalytic reaction in presence of hydrogen.

EFFECT: high output of average distillate and basic component of lubrication oil and obtaining gasoil fraction having excellent low-temperature fluidity.

6 cl, 1 tbl, 5 ex, 1 dwg

FIELD: oil and gas production.

SUBSTANCE: procedure consists in following stages: (a) there is performed hydrocarbon raw stock hydraulic processing by means of gas enriched with hydrogen for production of hydraulically treated output flow containing mixture of fluid and vapour; mixture of fluid and vapour is separated into liquid phase and vapour phase; (b) liquid phase is separated to controlled liquid part and excessive liquid part; (c) vapour phase is connected with excessive liquid part for production of vapour-liquid part; (d) there is extracted fraction containing raw stock for FCC from controlled liquid part and simultaneously there is performed hydro-cracking of vapour-liquid part for production of diesel-containing fraction or there is performed hydro-cracking of controlled liquid part for production of diesel containing fraction and simultaneously there is extracted fraction containing raw stock for FCC from vapour-liquid part. The invention also refers to the device for implementation of the procedure of hydraulic cracking with partial conversion.

EFFECT: production of diesel fuel with ultra-low content of sulphur and substantially better combustibility.

9 cl, 3 ex, 4 tbl, 4 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention is related to hydrocracking processes, under conditions of which large proportion of heavy hydrocarbon stock e.g. Vacuum Gas Oil (VGO) turns to hydrocarbons with lower molecular mass and lower boiling temperature. The invention relates to the method of production of base oil, involving: a) hydrocracking of heavy hydrocarbon stock with hydrocracking catalyst containing the preset amount less than 15 wt % of beta-zeolite with flow coming out of a hydrocracking plant containing at least 40 wt % of hydrocarbons boiling at temperature of 382°C (720°F), and b) separation from flow coming out of a hydrocracking plant of unconverted oil with pour point not above 18°C (65°F) in form of high-boiling fraction containing base oil.

EFFECT: improvement of base oil quality.

11 cl, 1 dwg, 4 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: invention is related to a combined method of conversion of oil-derived hydrocarbon fractions into high-quality hydrocarbon mixtures as fuel, which includes catalytic cracking of hydrocarbon fraction in catalyst fluidised bed with catalyst containing ERS-10 zeolite, where the specified catalyst contains at least two components, where the specified components represent: (a) a component containing one or more catalytic cracking catalysts in fluidised, and (b) a component containing ERS-10 zeolite for obtaining Light Cycle Gas Oil (LCGO), hydrotreatment of light cycle gas oil, interaction of hydrotreated light cycle gas oil obtained at the previous stage of hydrotreatment in presence of hydrogen with catalytic system. The invention also touches the method of catalytic cracking and a stage of catalytic cracking in fluidised bed.

EFFECT: production of high-quality hydrocarbons, conversion increase.

21 cl, 3 tbl, 1 ex

FIELD: machine building.

SUBSTANCE: invention relates to the hydroconversion method for raw hydrocarbons in the mix with the circulating part of the hydroconversion vacuum residue by a high-aromatic modifier, dispersion of a catalyst precursor and hydrogen-containing gas which is supplied in the amount of maximum 800 nm3 per 1 m3 of raw material in terms of hydrogen and of minimum the value of chemical hydrogen demand. The above is carried out in a reactor with an internal circular baffle plate which adjoins the reactor top in a pressure tight way and forms axial and circular cavities, and with separation space at the top of the circular cavity. Hydroconversion gas is removed from the separation space, liquid hydroconversion product is removed from the top of the axial cavity, circulating reaction mass is removed from the bottom of the reactor's circular cavity, cooled and delivered for mixing with heated raw liquid-vapour mixture, the temperature of the liquid hydroconversion product is kept close to the upper limit of the hydroconversion temperature range, the temperature of the heated raw mixture and the temperature of the circulating reaction mass are kept close to the lower limit of the hydroconversion temperature range. Hydroconversion products are separated and rectified to isolate light fractions, heavy gas oil and vacuum residue, part of the latter is recirculated, and the balance part is recovered to produce regenerated catalyst precursor.

EFFECT: reduction of power inputs and metal consumption of equipment along with the provision for high yield of light fractions.

1 dwg, 1 ex

FIELD: engines and pumps.

SUBSTANCE: invention relates to production of fuel for jet engines from kerosene stock. Proposed method comprises hydrofining of kerosene stock with freezing point interval of 163-302°C (325-575°F) over hydrofining catalyst under conditions of hydrofining. This allows getting hydrofined kerosene stock. Besides, it includes dewaxing of, in fact, all hydrofined kerosene stock over catalyst including 1-D molecular sieve with ten rings under conditions of dewaxing to get water-dewaxed kerosene stock. Also, it includes fractionating of water-dewaxed kerosene stock to get fuel for jet engines.

EFFECT: higher yield, better properties.

10 cl, 1 dwg, 2 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: initial hydrocarbon raw material is initially separated and first part of initial raw material is introduced into first zone of dehydration reaction, which functions without oxidation re-heating, and obtained as a result output flow is introduced into second zone of dehydration reaction, which functions without oxidation re-heating. Obtained as a result output flow from second zone of dehydration reaction, together with second part of initial raw material is introduced into third zone of dehydration reaction, which functions with oxidation re-heating.

EFFECT: increased method productivity.

10 cl, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention is referred to method of production of high-octane petrol and includes fractionation of hydrotreated naphtha into light and heave fractions; light naphtha isomerisation and heavy naphtha reforming in presence of platinum-containing catalyst with delivery of excessive hydrogen from reforming to isomerisation. Isomerisation is carried out with sulfate-zirconia catalyst with subsequent separation of isomerisate into three fractions: low-boiling fraction, medium fraction containing n-hexane and methylpenthanes and high-boiling fraction; medium fraction is recirculated to isomerisation raw material. By rectification from reformate light and heavy reforming fractions are obtained; heavy fraction is mixed with low- and high-boiling fractions of isomerisate with production of the target product while light fraction of reforming boiling away up to 85-95°C is subjected to hydroisomerisation at 250-300°C in presence of platinum-containing catalyst and obtained hydroisomerisate is delivered to be mixed with isomerisate.

EFFECT: reduction of benzole and aromatic hydrocarbons content in compliance with requirements to modern types of petrol with preservation of integration for reforming and isomerisation processes.

2 cl, 1 tbl, 7 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method for hydrocracking a hydrocarbon stream involving the following operations: providing hydrocarbon starting material (12); feeding the hydrocarbon starting material (12) into a hydrofining zone (14) to obtain an output stream (30) of the hydrofining zone; feeding the output stream (30) of the hydrofining zone into a separation zone (16) in order to separate one or more streams of hydrocarbons with a lower boiling point (34, 58, 62, 66) from a stream of liquid hydrocarbons with a higher boiling point (68); inlet of at least a portion of the stream of liquid hydrocarbons with a higher boiling point as material (68) for hydrotreatment without using a considerable amount of hydrocarbons coming from the hydrotreatment zone with an essentially continuous liquid phase; adding hydrogen (70) to the material (68) for hydrotreatment in an amount which is sufficient to maintain essentially liquid-phase conditions; feeding the material (68), mixed with hydrogen, for hydrotreatment into the hydrocracking zone (24) with an essentially continuous liquid phase; and carrying out a reaction for hydrocracking the material (68) for hydrotreatment in the hydrocracking zone (24) with an essentially continuous liquid phase with a hyrocracking catalyst in hydrocracking conditions to obtain an output stream (72) of the hydrocracking zone having a lower boiling point compared to the stream (68) of liquid hydrocarbons with a higher boiling point. The invention also relates to another method for hydrocracking a hydrocarbon stream.

EFFECT: improved characteristics of products, higher conversion.

16 cl, 5 dwg, 4 tbl, 1 ex

FIELD: power engineering.

SUBSTANCE: method is described to produce hydrocarbon fractions, which may be used as diesel fuel or as components of diesel fuel, based on a mixture of biological origin, containing ethers of fatty acids, possibly, with a certain amount of free fatty acids, which includes the following stages: 1) hydrodesoxygenation of a mixture of organic origin; 2) hydroisomerisation of a mixture produced at the stage (1), after possible treatment for cleaning; besides, the specified stage of hydroisomerisation is carried out in presence of a catalytic system, which contains the following: a) a carrier of acid nature, including a fully amorphous micro-mesoporous silicon-aluminium oxide, having a mole ratio SiO2/Al2O3 in the range from 30 to 500, the surface area of more than 500 m2/g, volume of pores in the range from 0.3 to 1.3 ml/g, the average diameter of pores below 40 Ǻ, b) a metal component containing one or more metals of group VIII, possibly mixed with one or more metals of the group VIII.

EFFECT: production of a hydrocarbon fraction, which may be applied as diesel fuel or as a component of diesel fuel.

55 cl, 4 tbl, 3 dwg, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing jet fuel for supersonic aircraft via hydrogenation and subsequent hydrodewaxing of secondary petroleum material in the presence of a hydrogen-containing gas and catalysts, at high temperature and pressure in two hydrogenation reactors and in a hydrodewaxing reactor. The secondary material used is a mixture of gas oils from catalytic cracking and delayed coking in ratio from 90%-10% to 70%-30% and straight-run gas oil is further added in amount of not more than 30 wt % based on the total load of the material, wherein the straight-run gas oil is fed into the top part of the first or second hydrogenation reactor or in different fractions into the top part of the first and second hydrogenation reactors, wherein the hydrogenation reactors are loaded with nickel sulphide - tungsten catalyst, and the hydrodewaxing reactor is 70% loaded with a molybdenum catalyst on a zeolite support, and 30% by a nickel sulphide - tungsten catalyst.

EFFECT: wider range of raw material resources for producing scarce jet fuel for supersonic aircraft, improved technological effectiveness of the process owing to a simple temperature control scheme in the reaction zone and high output of the end jet fuel.

3 cl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method for synthesis of branched olefins, said method involving dehydrogenation of an isoparaffin composition containing 0.5% or less quaternary aliphatic carbon atoms on a suitable catalyst. Said isoparaffin composition is obtained via hydroisomerisation a paraffin composition and contains paraffin containing 7-18 carbon atoms. Said paraffins, at least some of their molecules, are branched, where content of branched paraffins in the isoparaffin composition is equal to at least 50% of the weight of the isoparaffin composition. The average number of branches per paraffin molecule is between 0.5 and 2.5 and the branches include methyl and optional ethyl branches. Said branched olefins contain 0.5% or less quaternary aliphatic carbon atoms. Said paraffin composition is obtained using Fischer-Tropsch method. The invention also relates to methods of producing a branched alkyl aromatic hydrocarbon and branched alkylaryl sulphonates including the method described above.

EFFECT: high versatility and cost effectiveness of the method.

7 cl, 19 ex

FIELD: by-product-coking industry.

SUBSTANCE: claimed method includes hydrofining of by-product-coke resin with subsequent hydrodealkylation. In hydrofining step hydrogen donators such as naphthalene, anthracene, and phenanthrene hydro- or alkyl-derivatives, containing in coal-far resin, are obtained. Dealkylation is carried out using the said hydrogen donators. Quantitative content of hydrogen donators is equal the same of benzene, naphthalene, alkyl-derivatives, and other hydrodealkylated compounds (15-30 wt.% as calculated to raw material). Hydrofining is carried out under hydrogen pressure of 2-5 MPa, at 280-4000C, feed space velocity of 0.5-2 h-1, in hydrogen/feed ratio of 500-1000 l/kg in flowing system.

EFFECT: finished product of improved quality.

4 cl, 2 tbl, 2 ex

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