Method and plant for hydraulic treatment of two flows

FIELD: process engineering.

SUBSTANCE: proposed process comprises compression of boost hydrogen in first compressor to get first flow of compressed boost hydrogen. First flow of compressed boost hydrogen is compressed in second compressor to get second flow of compressed boost hydrogen. Said second flow of compressed boost hydrogen is separated as second flow of compressed boost hydrogen for hydraulic treatment. First flow of hydrocarbons is processed over first flow for hydraulic processing including second flow of compressed boost hydrogen and first hydraulic processing catalyst to get first effluent flow of hydroprocessing products. Second flow of hydrocarbons is processed over second flow for hydraulic processing including first flow of compressed boost hydrogen and first hydraulic processing catalyst to get second effluent flow of hydroprocessing products. Said second effluent flow of hydroprocessing products is separated to get vaporous second effluent flow of hydroprocessing products. Said vaporous second flow is added to said boost hydrogen flow upstream of said first compressor.

EFFECT: perfected feed of hydrogen to separate process units.

9 cl, 2 dwg

 

This application claims the priority of patent applications U.S. 13/076647, 13/076658, 13/076670 and 13/076680, the date of submission of all these applications is March 31, 2011

The technical field to which the invention relates.

The invention relates to hydrobromide two hydrocarbon streams at different pressures.

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 obtain hydrocarbons with lower molecular weight. 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.

Usually upstream from the installation 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, such as diesel fuel.

The village is olcu 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 direction of diesel fuel in the damage output of gasoline. Mild hydrocracking can be carried out with less stringent regime, 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 legalized rules and regulations commodity diesel fuel must meet all lower limits on contaminants, 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 of less than 10 wppm (weight parts per million).

The Association of the units of hydrobromide in a single complex can meet such a situation, in which one the mouth of the transportation operates at a higher pressure than the other. For example, the setting for the hydrocracking runs at a higher pressure than the setting for Hydrotreating. Hydrogen must be submitted at different pressures. Excess hydrogen is recycled through the compressor for recirculation of gas, designed specifically for each installation of hydrobromide.

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 increasingly stringent requirements to the product. There is also a need for improved methods of supplying hydrogen to the individual process units at different pressures.

Disclosure of inventions

In one 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 in the first compressor receiving the first stream of compressed make-up hydrogen. The first portion of the first compressed make-up hydrogen is compressed in the second compressor to obtain a second stream of compressed make-up hydrogen. The second part of the first compressed make-up hydrogen select the second stream of hydrogen for hydrobromide. The flow of hydrocarbons is subjected to hydrocracking in the presence of the second compressed make-up hydrogen and a hydrocracking catalyst to obtain the exit stream of the products of hydrocracking. The flow of diesel fuel is subjected to Hydrotreating in the presence of the second stream of hydrogen for hydrobromide and Hydrotreating catalyst to obtain a second effluent product stream of hydrobromide. Finally, at least part of the said first exhaust product hydrobromide subjected to fractionation to obtain a flow of diesel fuel.

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 in the first compressor receiving the first stream of compressed make-up hydrogen. The first portion of the first compressed make-up hydrogen is compressed in the second compressor to obtain a second stream of compressed make-up hydrogen. The second part of the first compressed make-up hydrogen is taken as the second stream of hydrogen for hydrobromide. The flow of diesel fuel is subjected to Hydrotreating in the presence of the second stream of hydrogen for hydrobromide and Hydrotreating catalyst to obtain a second effluent product stream of hydrobromide. P is the current hydrocarbon is subjected to hydrocracking in the presence of the first stream of hydrogen for hydrobromide, containing the second compressed make-up hydrogen, and the catalyst for hydrocracking of obtaining the exit stream products. At least part of the said first exhaust products hydrobromide subjected to fractionation to obtain a flow of diesel fuel. The first output stream products hydrobromide share and receive vaporous first output stream products hydrobromide containing hydrogen. Vaporous first output stream products hydrobromide compress with getting the flow of recirculated hydrogen. Finally, the flow of recirculated hydrogen added to the first stream of hydrogen for hydrobromide.

In accordance with 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 in the first compressor receiving the first stream of compressed make-up hydrogen. The first portion of the first compressed make-up hydrogen is compressed in the second compressor to obtain a second stream of compressed make-up hydrogen. The flow of hydrocarbons is subjected to hydrocracking in the presence of the first stream of hydrogen for hydrobromide containing the second compressed make-up hydrogen, and the catalyst for hydrocracking with receipt of the first in the walking thread products hydrobromide. The second part of the first compressed make-up hydrogen is taken as the second stream of hydrogen for hydrobromide. The flow of diesel fuel is subjected to Hydrotreating in the presence of the second stream of hydrogen for hydrobromide and Hydrotreating catalyst to obtain a second effluent product stream of hydrobromide. At least part of the said first exhaust products hydrobromide subjected to fractionation to obtain a flow of diesel fuel. Finally, at least part of the second effluent product stream of hydrobromide subjected to fractionation to obtain diesel fuel with low sulfur content.

In one embodiment relating to a device, the invention includes a plant for production of diesel fuel containing piping make-up hydrogen, designed for carrying the flow of make-up hydrogen; the first compressor, which communicates with the pipe make-up hydrogen and is designed to compress the flow of make-up hydrogen to obtain a first compressed make-up hydrogen; separating device in communication with the first compressor, which serves to separate the first flow of compressed make-up hydrogen for the first part, transported through the first branch of the pipeline, and is that part containing the second stream of hydrogen for hydrobromide transported through the second branch pipe; and the second compressor is connected with the first branch pipeline to compress the first portion of the first compressed make-up hydrogen to obtain a second stream of compressed make-up hydrogen is transported through the second pipeline for compressed make-up hydrogen; hydrocracking reactor which is connected with the first branch pipe and designed for hydrocracking flow of hydrocarbons from receiving the flow of diesel fuel; the Hydrotreating reactor is communicated with the second branch of the pipeline and the hydrocracking reactor and is used for Hydrotreating the flow of diesel fuel.

In another embodiment relating to a device, the invention includes a plant for production of diesel fuel containing piping make-up hydrogen, designed for carrying the flow of make-up hydrogen; the first compressor, which communicates with the pipe make-up hydrogen and is designed to compress the flow of make-up hydrogen to obtain a first compressed make-up hydrogen; a second compressor which is connected to the first compressor for compressing a portion of the first compressed make-up hydrogen with obtaining W is the second compressed make-up hydrogen; the hydrocracking reactor which is connected with the second compressor, designed for hydrocracking flow of hydrocarbons from receiving the flow of diesel fuel; the Hydrotreating reactor is communicated with the first compressor and the hydrocracking reactor and is used for Hydrotreating the flow of diesel fuel.

In the following embodiment relating to a device, the invention includes a plant for production of diesel fuel containing piping make-up hydrogen, designed for carrying the flow of make-up hydrogen; the first compressor, which communicates with the pipe make-up hydrogen and is designed to compress the flow of make-up hydrogen to obtain a first compressed make-up hydrogen; hydrotreater unit which is connected with the first compressor, designed for hydrobromide flow of diesel fuel; a second compressor which is connected to the first compressor for compressing a portion of the first compressed make-up hydrogen to obtain a second stream of compressed make-up hydrogen; hydrocracking reactor which is connected with the second compressor, designed for hydrocracking flow of hydrocarbons to more low-boiling hydrocarbons; cold separator which is connected with the Hydrotreating reactor, designed to share the value of the second exhaust products hydrobromide obtaining second vaporous effluent product stream of hydrobromide, containing hydrogen is transported through the head pipe, and the second liquid exit stream products hydrobromide discharged through the bottom of the pipeline, while the second compressor is connected with the lead pipe.

In yet another embodiment relating to the method of the invention includes a method of hydrobromide two hydrocarbon streams including the stream compression make-up hydrogen in the first compressor receiving the first stream of compressed make-up hydrogen. The first portion of the first compressed make-up hydrogen is compressed in the second compressor to obtain a second stream of compressed make-up hydrogen. The second part of the first compressed make-up hydrogen is taken as the second stream of hydrogen for hydrobromide. The first stream of hydrocarbon is subjected to hydrobromide in the presence of the first stream of hydrogen for hydrobromide containing the second compressed make-up hydrogen, and the first catalyst hydrobromide with receipt of the first exhaust products hydrobromide. The second stream of hydrocarbons is subjected to hydrobromide in the presence of the second stream of hydrogen for hydrobrake containing the first compressed make-up hydrogen, and the second catalyst hydrobromide to obtain a second effluent product stream hydroebres the TCI. The specified second output stream products hydrobromide share and receive vaporous second output stream products hydrobromide. Finally, the vaporous second output stream products hydrobromide add to the flow of make-up hydrogen is higher during the flow from the second compressor.

In accordance with another embodiment relating to the method of the invention includes a method of hydrobromide two hydrocarbon streams including the stream compression make-up hydrogen in the first compressor receiving the first stream of compressed make-up hydrogen. The first portion of the first compressed make-up hydrogen is compressed in the second compressor to obtain a second stream of compressed make-up hydrogen. The second part of the first compressed make-up hydrogen is taken as the second stream of hydrogen for hydrobromide. The first stream of hydrocarbon is subjected to hydrobromide in the presence of the first stream of hydrogen for hydrobromide containing the second compressed make-up hydrogen and a hydrocracking catalyst to obtain a first effluent product stream of hydrobromide. The second stream of hydrocarbons is subjected to Hydrotreating in the presence of the second stream of hydrogen for hydrobromide and Hydrotreating catalyst to obtain a second exit stream etc the products of hydrobromide. The specified second output stream products hydrobromide share to obtain vaporous second exit stream products hydrobromide. Finally, the vaporous second output stream products hydrobromide add to the first part of the first compressed make-up hydrogen.

In accordance with another embodiment relating to the method of the invention includes a method of hydrobromide two hydrocarbon streams, including compressed make-up hydrogen flow in the first compressor receiving the first stream of compressed make-up hydrogen. The first portion of the first compressed make-up hydrogen is compressed in the second compressor to obtain a second stream of compressed make-up hydrogen. The second part of the first compressed make-up hydrogen is subjected to compression as the second stream of hydrogen for hydrobromide. The first stream of hydrocarbon is subjected to hydrocracking in the presence of the first stream of hydrogen for hydrobromide containing the second compressed make-up hydrogen and a hydrocracking catalyst to obtain a first effluent product stream of hydrobromide. The second stream of hydrocarbons is subjected to Hydrotreating in the presence of the second stream of hydrogen for hydrobromide and Hydrotreating catalyst to obtain a second exit stream about is aktov of hydrobromide. The specified second output stream products hydrobromide share to obtain vaporous second exit stream products hydrobromide. Received vaporous second output stream products hydrobromide add to the flow of make-up hydrogen upstream from the first compressor.

In yet another embodiment relating to a device, the invention includes a setting for hydrobromide two hydrocarbon streams containing the pipeline make-up hydrogen, designed for carrying the flow of make-up hydrogen; the first compressor, which communicates with the pipe make-up hydrogen and is designed to compress the flow of make-up hydrogen to obtain a first compressed make-up hydrogen; separating device in communication with the first compressor, which serves to separate the first flow of compressed make-up hydrogen for the first part, transported through the first branch pipe and the second part containing the second stream of hydrogen for hydrobromide transported through the second branch pipe; the second compressor is connected with the first branch pipe serving to compress the first portion of the first compressed make-up hydrogen to obtain a second stream of compressed make-up hydrogen, tra is sportowego through the second pipeline for compressed make-up hydrogen; the first reactor hydrobromide which is connected with the first branch pipe and intended to hydrobromide first stream of hydrocarbons; a second reactor hydrobromide which communicates with the second branch of the pipeline and is used to hydrobromide second stream of hydrocarbons; a separator which is connected with the second reactor hydrobromide and intended for separating the second effluent product stream of hydrobromide obtaining second vaporous effluent product stream of hydrobromide containing hydrogen is transported in the main pipe, while the second compressor is connected with the lead pipe.

In another embodiment relating to a device, the invention further includes a setting for hydrobromide two hydrocarbon streams containing the pipeline make-up hydrogen, designed for carrying the flow of make-up hydrogen; the first compressor, which communicates with the pipe make-up hydrogen and is designed to compress the flow of make-up hydrogen to obtain a first compressed make-up hydrogen; separating device in communication with the first compressor and is designed for the separation of the first compressed make-up hydrogen for the first part, transported first from ellenie pipeline and the second part containing the second stream of hydrogen for hydrobromide transported through the second branch pipe; a second compressor, which is connected with the first branch pipe and serves to compress the first portion of the first compressed make-up hydrogen to obtain a second stream of compressed make-up hydrogen is transported through the second pipeline for compressed make-up hydrogen; hydrocracking reactor which is connected with the first branch pipe and serving to conduct hydrocracking the first stream of hydrocarbons to more low-boiling hydrocarbons; hydrotreater unit which is connected with the second branch of the pipeline and used for carrying out Hydrotreating a second stream of hydrocarbons; the separator, reported by hydrotreater unit and intended for separating the second effluent product stream of hydrobromide obtaining second vaporous effluent product stream of hydrobromide containing hydrogen is transported in the head pipe; a second compressor connected with the main pipe at the connection point on the first branch of the pipeline.

According to another embodiment relating to a device, the invention includes a setting for hydrobromide two hydrocarbon streams, the soda is containing the pipeline make-up hydrogen, designed for carrying the flow of make-up hydrogen; the first compressor, which communicates with the pipe make-up hydrogen and is designed to compress the flow of make-up hydrogen to obtain a first compressed make-up hydrogen; separating device in communication with the first compressor and serves to separate the first flow of compressed make-up hydrogen for the first part, transported through the first branch pipe and the second part containing the second stream of hydrogen for hydrobromide transported through the second branch pipe; a second compressor, connected with the first branch pipe and intended to compress the first portion of the first compressed make-up hydrogen to obtain a second stream of compressed make-up hydrogen is transported through the second pipeline for compressed make-up hydrogen; hydrocracking reactor which is connected with the first branch pipe and serving to conduct hydrocracking the first stream of hydrocarbons to more low-boiling hydrocarbons; hydrotreater unit which communicates with the second branch of the pipeline and is used for Hydrotreating a second stream of hydrocarbons; a separator which is connected with the Hydrotreating reactor and is designed to split the I second exit stream products hydrobromide obtaining second vaporous effluent product stream of hydrobromide, containing hydrogen is transported in the head pipe; while the first compressor is connected with the lead pipe in the place of its connection with the pipeline to the make-up hydrogen.

Brief description of drawings

Fig.1 is a simplified process flow diagram for an embodiment of the present invention.

Fig.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 these components is provided by the material flow.

The term "message downstream" means that the operation of the installation, at least a portion of the material passing to the object of interaction, may, at the message below on the stream to pass from the subject of the interaction, which is reported to the specified object.

The term "message upstream" means that the operation of the installation, at least a portion of the material passing from the subject of the interaction, may, at the above message flow to pass to the object of interaction, which reported the specified entity.

The term "column" means a distillation column or columns that are designed to separate one or more components with different volatility. If not Ogawa is prohibited otherwise, each column above includes a capacitor which is used for condensing and returning part of the exhaust from the top (head) flow back into the upper part of the column, and in the lower part of the column heater for evaporation and direction of the exhaust from the bottom (bottom) 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 head vapors at the outlet for the vapor column. Waste temperature is a target temperature of the bottom liquid. The piping to the top (head) of the thread and pipelines for the lower (bottom) flow refers to the network of pipelines running from the column below in the direction of flow from the return phlegmy or return flow boiling in a column.

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 (the mass.%), 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 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

Stage installation for hydrobromide often operate at different pressures, and each of the two installations hydrobromide contains its own dedicated compressor recycle gas. If one of the settings for hydrobromide is a typical installation for Hydrotreating, it contains the compressor recycle gas, which removes gas from the cold separator is located downstream from the hydrotreater unit, and returns rich in hydrogen gas at the reactor inlet is of hydrobromide. Usually for both installations hydrobromide required supply flow makeup gas.

Compressor recycle gas in a single unit for hydrobromide can be eliminated by taking gas from the compression of feed gas used in the first installation of hydrobromide, which can be the setting for hydrocracking. The flow of feed gas can be discharged from the first compression stage and return upstream or downstream from the first foot compression. The second stage of compression, which is downstream from the first stage of compression may increase the pressure of the feed gas to a higher pressure required for the first installation for hydrobromide. Only a part of the make-up hydrogen is directed to the second unit for hydrobromide, which can be the Hydrotreating unit.

Reactors for carrying out mild hydrocracking operate at a low rigidity of the regime and, therefore, provide a low degree of conversion. Diesel fuel produced in the mild hydrocracking, is of insufficient quality to meet the existing technical requirements for fuel, in particular in relation to the sulphur content. In this regard, the diesel fuel produced by a soft cracking, can be processed in the installation is for Hydrotreating with the to be added to the finished 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.

In Fig.1 presents an apparatus and method 8 for the production of diesel fuel, which include a compressor section 10, the first installation 12 for hydrobromide, the second system 14 for hydrobromide and section 16 of the fractionation. First of hydrocarbon raw materials 38 may be filed in the first installation 12 for hydrobromide and converted into low-boiling hydrocarbons, such as diesel fuel. The exiting product stream from the unit 12 hydrobromide may be subjected to fractionation on a plot of 16 fractionation and product fractionation may be sent to the second system 14 for hydrobromide. The first installation 12 for hydrobromide runs at a higher pressure than the second unit 14 for hydrobromide.

The flow of make-up hydrogen through line 20 to the make-up hydrogen is fed to the first compressor 22 to increase the pressure of the flow of make-up hydrogen and receiving the first compressed stream of make-up hydrogen in the pipe 24. The flow of make-up hydrogen in the pipe 20 may first be combined with maroobra the th second output flow of the product, transported by pipeline 98, at the point 25 of the connection of these pipes with obtaining the combined stream in the pipe 26 above in the course of the flow from the first compressor 22. The combined stream in the pipe 26 can then be subjected to compression in the first compressor 22 to receive the first stream of compressed make-up hydrogen in the pipe 24 to the compressed make-up hydrogen. The first compressor may be a number of series-connected compressors.

The separation device 27 mounted on the pipe 24 to the compressed make-up hydrogen, allows you to get the first part of the compressed make-up hydrogen, which enters the first branch 28 of the pipeline, and the second part of the compressed make-up hydrogen entering into the second branch 30 of the pipeline. The second part of the compressed make-up hydrogen passing through the second branch 30 of the pipeline is directed to the second installation 14 hydrobromide.

The first part of the compressed make-up hydrogen passing through the first branch 28 of the pipeline may be subjected to additional compression in the second compressor 32, which may be a number of series-connected compressors, getting into the pipe 34 of the second compressed make-up flow. The second compressed make-up stream in drobopro the de 34 may be combined with a stream of recycle hydrogen, transported by pipeline 56, to produce in the pipe 36 of the first stream of hydrogen for hydrobromide. The first installation 12 for hydrobromide runs at a higher pressure than the second unit 14 for hydrobromide.

The first stream of hydrogen for hydrobromide transported by pipeline 36, which are selected from the second compressed make-up hydrogen may be combined with the first stream of hydrocarbon material passing through the pipe 38, to receive the first stream of raw materials for hydrobromide transported through the pipeline 40.

The flow of hydrocarbons is introduced into the pipe 38, for example, through an intermediate surge tank. According to one aspect of the described method and device, 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, neasfaltirovanyj solvent, oil, pyrolysis oil, high boiling synthetic oils, cycle oils, petroleum raw material gidrometeorologicheskii, the distillate of the catalytic cracking and the like. This hydrocarbon can contain from 0.1 to 4 wt.% of sulfur.

Suitable hydrocarbon feedstock is a GED 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 GED usually has a boiling point in the range of from 315°C (600°F) up to 565°C(1050°F).

The first reactor 42 hydrobromide can lower thread to communicate with one or more of the compressors 22 and 32 installed on the pipeline 20 make-up hydrogen from the first pipe line 38 for hydrocarbons and with the first branch 28 of the pipeline. The first flow of raw materials for hydrobromide can exchange heat with the first output stream products hydrobromide passing through the pipe 44 and is further heated in the firing heater before entering the first reactor 42 hydrobromide for holding hydrobromide first stream of hydrocarbons. The first reactor 42 hydrobromide may contain one or more containers, multiple layers of catalyst in each tank and various combinations of catalyst Hydrotreating and hydrocracking catalyst in one or more containers.

Hydrobromide, rewodina in the first reactor 42 hydrobromide, can be hydrolocking. According to one aspect, the first of hydrobromide may be installing 12 for hydrocracking, and in this case, the first stream of hydrogen for hydrobromide is a stream of hydrogen for hydrocracking in the pipe 36, the first reactor 42 hydrobromide is a hydrocracking reactor, below which flow communicates with the first branch 28 of the pipeline and the flow of raw material in the pipe 40 is a flow of feedstock to hydrocracking.

Hydrocracking refers to the process in which hydrocarbons craterous in the presence of hydrogen to hydrocarbons with lower molecular weight. In some aspects, the hydrocracking reaction provides a General conversion of hydrocarbons, at least 20 volume. % and typically more than 60 volume. % obtaining products boiling at temperatures below the boiling point of the fractions of diesel fuel. The reactor 42 hydrocracking can work with partial conversion, making up more than 50 volume. %, or deep conversion, component, at least 90 volume. % of raw materials on the basis of full conversion. To obtain the maximum amount of diesel fuel effective deep conversion. The first capacity or layer in the reactor 42 hydrocracking may contain a catalyst for Hydrotreating carried out with the purpose of demet is lisali, desulfurization or diazotoluene raw materials hydrocracking.

The reactor 42 hydrocracking can work in the mild hydrocracking. In the mild hydrocracking is selective conversion of raw materials into heavy products, such as diesel fuel and kerosene, with a low yield of lighter hydrocarbons, such as naphtha and gas. Pressure also choose moderate to limit the hydrogenation distillation product to a level optimal for treatment below in the course of the stream. The conditions are mild hydrocracking, will ensure total conversion of hydrocarbons from 20 to 60 volume. %, preferably from 20 to 50 volume. % obtaining products boiling at temperatures below the boiling point of the fractions 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 on the Hydrotreating catalyst may be a significant part of the overall conversion. If the first reactor 42 hydrobromide is designed for mild hydrocracking, it is assumed that the reactor 42 mild hydrocracking can be fully loaded catalyst for Hydrotreating or fully hydrocracking catalyst or a certain number of layers of catalysis is ora 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 subsequent layers of catalyst for hydrocracking are absent.

The first reactor 42 hydrobromide shown in Fig.1, contains in a single reaction vessel four layers of catalyst. If needed for mild hydrocracking, it is 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 the hydrocracking catalyst when carrying out mild hydrocracking.

According to one aspect, for example, if the product of the conversion of the preferred balance of middle distillate and gasoline can be made mild hydrocracking in the first reactor 42 hydrobromide using hydrocracking catalyst, which uses amorphous aluminosilicate framework or framework with a low content of zeolite is combined with one or more metal hydrogenating component is patients of Group VIII or Group VIB (the Periodic table). According to another aspect, if the middle distillate product conversion is largely preferred over gasoline in the first reactor 42 hydrobromide may be implemented partially or deep conversion using a catalyst which contains, in General, any basis of the crystalline zeolite catalyst for cracking, which precipitated hydrogenating metal component of Group VIII. For more hydrogenating components may be selected from Group VIB for Association with zeolite core.

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 exchange cations such as sodium, magnesium, calcium, rare earth metals, etc., These are the basics, in addition, characterized by the presence 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, t is s, X, Y and L of crystalline zeolites, for example, 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. An illustrative example of zeolite preferred group is synthetic molecular sieve type Y.

Naturally occurring zeolites are usually found in the sodium form, in the form of an 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 splitting of ammonium ions associated with the zeolite, leaving in their place hydrogen ions and/or ion-exchange sites, which would actually be dictionary subsequent removal of water. Hydrogen or dictionarie" type Y zeolites of this nature are described in more detail in the patent document US 3130006.

Mixed polyvalent metal-hydrogen zeolites can be prepared by first ion exchange with ammonium salt, and then partially reverse the exchange rate is Mr. 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 are at least 10 percent, and preferably at least 20 percent deficit 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 combination with them may also be used by other promoters, including the metals of Group VIB, for example, 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.%.

Preferred ability, the BPO implementation of the 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 of the catalyst is 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°F) 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, diluents or binders such as alumina, silica gel, aluminosilicate Coeli, activated clay, etc., in the ratios are in the range of 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, which can also be used with the person in accordance with the present invention, which implies, for example, the use of aluminophosphate molecular sieves, crystalline chromosomique and other crystalline silicates. Crystalline chromaticity more fully described in the patent document US 4363718.

In accordance with one approach of the hydrocracking conditions 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 psig) to 20.7 MPa (3000 psig), a clock volumetric 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 conditions may include a temperature of 315°C (600°F) to 441°C (825°F), the excess pressure in the range from 5.5 to 13.8 MPa (from 800 to 2000 psig), or more preferably 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).

Hydrobromide carried out in the first reactor 42 hydrobromide can be a hydrotreatment. Hydrotreating is a process in which a gas containing hydrogen, contacter is no with hydrocarbons in the presence of suitable catalysts, are active, mainly for removal from the source of hydrocarbons heteroatoms, such as sulfur, nitrogen and metals. When carrying out Hydrotreating hydrocarbons with double and triple bonds can be saturated. Aromatic compounds can also be saturated. Some Hydrotreating processes are designed specifically for the saturation of aromatic compounds.

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, at least one Group VI metal, preferably molybdenum and tungsten, on the material of the carrier with a large surface area, preferably of aluminum oxide. Other suitable Hydrotreating catalysts include zeolite catalysts, and the catalysts of noble metals, for which a noble metal selected from palladium and platinum. Within the scope of the present invention in the second reactor 42 hydrobromide can be used more than one type of Hydrotreating catalyst in the same capacity. The metal of Group VIII is generally in a quantity of from 2 to 20 the ACC.%, preferably in the range from 4 to 12 wt.%. The Group VI metal is typically in an amount of from 1 to 25 wt.%, preferably from 2 to 25 wt.%.

Preferred Hydrotreating conditions can 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), pressure in the range of from 3.4 MPa (500 psig), preferably from 4.1 MPa (600 psig) to 6.2 MPa (900 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/m3 oil (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, using a Hydrotreating catalyst or a combination of Hydrotreating catalysts.

Hydrobromide carried out in the first reactor 42 hydrobromide can be a hydroisomerization. The process of hydroisomerization may also include a catalytic dewaxing. Hydroisomerization puts a process in which in one aspect, at least 10 percent, in another aspect, at least 50 percent and, according to another aspect, from 10 to 90 percent n-paraffins source of hydrocarbons the env is Troitsa to isoparaffins effectively with obtaining the exit stream of products at least one of the values of cloud temperature 0°C (32°F) or less, the temperature fluidity loss 0°C (32°F) or less and/or the temperature of the cold clogged filter 0°C (32°F) or less.

Usually the process conditions of hydroisomerization include a temperature of from 260°C (500°F) up to 371°C (700°F), the pressure of 1.38 MPa (200 psig) to of 8.27 MPa (1200 psig), hourly space velocity of the fresh hydrocarbonaceous feedstock from 0.1 to 10 h-1the circulation rate of hydrogen from 168 to 1011 normal m3/m3oil (from 1000 to 6000 standard cubic feet per barrel). However, there are also other conditions of the process of hydroisomerization, depending on the quality of raw materials and other factors.

Suitable catalysts hydroisomerization are any known conventional catalysts hydroisomerization. For example, suitable catalysts may include zeolite components, components hydrogenation/dehydrogenization, and/or acidic components. In some forms, the catalyst may include at least one metal of Group VIII, such as a noble metal (i.e., platinum or palladium). Other forms of the catalyst may also include Aluminiy phosphate and/or zeolite aluminosilicate. Examples of suitable catalysts are described in patent documents US 5976351; US 4960504; US 4788378; US 4683214; US 4501926 and US 4419220. However, there may be used the Ana other isomerization catalysts depending on the feedstock composition, the operating parameters of the process, the desired performance and other factors.

The first output stream products hydrobromide exits the first reactor 42 hydrobromide pipeline 44. If the first reactor 42 hydrobromide is a hydrocracking reactor, the first output stream products vibroblade in the pipe 44 is an output stream of the products of hydrocracking. The first output stream products vibroblade passing through the pipe 44, exchanges heat with the first raw material for hydrobromide transported through the pipeline 40, and in one embodiment may be cooled before entering the first cold separator 46. The first cold separator 46 downstream communicates with the first reactor 42 hydrobromide. The first cold separator can operate in temperatures from 46° to 63°C (115° to 145°F) and at a pressure slightly below the pressure in the first reactor 42 hydrobromide, given the differential pressure to maintain the flow of hydrogen and light gases contained in the main flow, and liquid under normal conditions, the hydrocarbons in the bottom stream. The first cold separator 46 provides a receiving vaporous first exit stream for hydrobromide containing hydrogen, in the head pipe 48 and the first liquid output stream for hydrobromide in the bottom t is webpromote 50. The first cold separator also has a sump for collecting water phase withdrawn through pipe 52.

Vaporous first output stream for hydrobromide, which can be gaseous output stream to the hydrocracking transported by pipeline 48, may be subjected to compression in the compressor 54 recirculating gas stream was received recirculating hydrogen in the pipe 56. The compressor 54 recirculating gas may lower flow communication with the first reactor 42 hydrobromide, which may be a hydrocracking reactor. The compressor 54 recirculating gas may be compressed vaporous first output stream containing hydrogen, designed for hydrobromide coming through the pipe 48, receiving a stream of recycle hydrogen, and transporting compressed stream through line 56. The second stream of compressed make-up hydrogen is transported through the pipe 34, is combined with recycle hydrogen is supplied through a pipe 56, which is a compressed vaporous first output stream products for hydrobromide, for providing the first stream of hydrogen for hydrobromide supplied through the pipe 36. The reactor 42 hydrocracking reported below according to the flow pipe 56 for recirculating hydrogen across the pipes 36 and 40.

As noted above, in one embodiment, the flow re-circulating hydrogen in the pipe 56 may be combined with the second stream of compressed make-up hydrogen is transported through the pipeline 34, downstream from the compressor 54 recirculating gas. However, if the pressure of the recirculating flow of hydrogen in the pipe 56 is too high to add to it the flow of make-up hydrogen without adding additional compressors upstream from the pipe 34 to the second compressed make-up hydrogen, the second compressed make-up hydrogen may be added to the vapor exiting flow of the products of hydrocracking in the pipeline 48 above in the course of the stream from the compressor 54 recirculating gas. This can improve the performance of the compressor 54 recirculating gas due to more noise gas.

At least a portion of the first exhaust products hydrobromide, exhaust pipeline 44, may be fractionated in section 16, below which flow communicates with the first reactor 42 hydrobromide to produce a second stream of hydrocarbons transported by pipeline 86. According to one aspect of the first liquid output stream products vibroblade, which may be a liquid outlet bookproduct hydrocracking, transported by pipeline 50 may be subjected to fractionation on a plot of 16 fractionation. According to another aspect of section 16 of the fractionation may contain cool evaporative drum 58. Liquid first output stream of the products of hydrocracking, transported by pipeline 50 may be quickly evaporated in the cold evaporator drum 58, which can operate at the same temperature as the cold separator 46, but at a lower pressure, in the range from 1.4 to 3.1 MPa MPa (200-450 psig) to produce the first liquid exit stream products hydrobromide easy flow of liquid in the bottom of the pipe 62 and the flow of light fractions discharged through the head pipe 64. Water flow through the pipe 52 from the cold sump of the separator can be directed through the cold evaporator drum 58. Water flow remaining after rapid evaporation is extracted from the cold sump of the evaporative drum 58 through pipe 66. The easy flow of the liquid in the bottom pipe 62 may be further fractionated 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 the liquid in the bottom pipe 62 can be heated and sent to the Stripping column 70. The stream of light liquid is ti, which is a first liquid output stream products hydrobromide, 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 discharged by the head 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 in the range from 690 to 1034 kPa (100 to 150 psig). The bottom stream hydrobromide passing through the pipe 76, can be heated in the firing heater and directed 80 column fractionation. Part of the bottom stream hydrobromide passing through the pipeline 76 may be subjected to boiling and returned to the Stripping column 70 instead of using steam for steaming.

Column 80 fractionation can also carry out the Stripping of the bottom stream after hydrocracking using the steam entering through the pipe 82, to receive the head of a stream of naphtha is withdrawn through pipe 84, the flow of diesel fuel is discharged through line 86 as a side fraction, and exhaust on drobopro the remote control 88 of the flow of crude oil, which may be appropriate for further processing, for example, in the catalytic cracking process in the fluidized bed. For the downstream flow of naphtha is withdrawn through pipe 84 may be necessary to conduct additional processing before mixing in 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 an integrated installation for Hydrotreating. It is expected that additional lateral fraction may be selected to provide a separate stream of light diesel fuel or kerosene selected above selection of flow of heavy diesel fuel, designated by a pipe 86. A portion of the naphtha stream discharged by 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 donnag the product of the hydrocracking may be subjected to boiling and returned to the column 80 fractionation instead of using for steam water vapor.

In the flow of diesel fuel, designated by a pipe 86 can be reduced sulfur content, but it does not satisfy the technical requirement of low sulfur diesel fuel (LSD), which is less than 50 wppm sulfur, demand ULSD (ultra low sulfur in diesel fuel), which corresponds to a sulfur content of less than 10 wppm, or other standards. Therefore, the fuel can be further thrown the final processing in the second installation 14 hydrobromide, which can be the installation of 14 Hydrotreating. Accordingly, the flow of diesel fuel in the pipe 86 may be a second stream of hydrocarbons. The second stream of hydrocarbons may have a lower average boiling point than the first flow of hydrocarbons.

The second stream of hydrocarbons transported by pipeline 86, may be combined with the second stream of hydrogen for hydrobromide containing the second portion of the first compressed make-up hydrogen entering from the first branch 30 of the pipeline to receive the second stream 90 of raw materials for hydrobromide. The second stream of hydrocarbons transported by pipeline 86 can also be mixed together with supplied raw materials, which are not shown. The second thread 90 of raw materials for hydrobromide can exchange heat with at is that the output stream hydrobromide, transported by pipeline 94, may then be heated in the firing heater and sent to the second reactor 92 hydrobromide.

Accordingly, the second reactor 92 hydrobromide downstream communicates with the section 16 fractionation, separation device 27 and the first reactor 42 hydrobromide. In the second reactor 92 hydrobromide second stream of hydrocarbons, which can represent the flow of diesel fuel is hydrobromide in the presence of the second stream of hydrogen for hydrobromide and the second catalyst hydrobromide to obtain a second exit stream 94 products hydrobromide.

The second reactor 92 hydrobromide may contain more than one container and the many layers of catalyst. The second reactor 92 hydrobromide shown in Fig.1, contains two layers of catalyst in one reaction vessel. The second reactor 92 hydrobromide can work as a reactor for hydrocracking, Hydrotreating reactor or reactor hydroisomerization loaded with the appropriate catalyst, as described above in regard to the first reactor 42 hydrobromide. The second reactor 92 hydrobromide lower thread can be communicated with the second branch 30 of the pipeline and the first reactor 42 hydrobromide, which may be a hydrocracking reactor.

Hydrobromide carried out in the second reactor 92 hydrobromide may be Hydrotreating. According to one aspect of the second unit for hydrobromide can be an installation 14 Hydrotreating, and in this case, the second stream of hydrogen for hydrobromide can be a stream of hydrogen for Hydrotreating passing through the conduit 30. The second reactor 92 for hydrobromide is a hydrotreater unit which communicates downstream with the second branch 30 of the pipeline, and the commodity flow in the pipe 90 is a flow of feedstock to Hydrotreating.

In the reactor 92 for Hydrotreating hydrocarbons with heteroatoms can be optionally demetilirovanny, obesity and diazotrophy by hydrobromide as described above with respect to installation 12 for hydrobromide. The reactor 92 Hydrotreating can also contain Hydrotreating catalyst, which is suitable for the saturation of aromatic compounds, hydrodewaxing and hydroisomerization.

If the first reactor 42 hydrobromide works as mild hydrocracking reactor, said first reactor 42 hydrobromide can convert from 20 to 60 volume. % raw, boiling at a temperature above the boiling range of diesel fuel to produce a boiling point below the border instrumentation is of fractions of diesel fuel. The second reactor 92 hydrobromide can have a very low conversion rate and can be used mainly for desulfurization, if it is combined with the reactor 42 mild hydrocracking, in order to ensure the technical characteristics of the fuel, for example, meet the requirements of diesel fuel with ultra-low sulfur diesel (ULSD).

The second output stream products hydrobromide transported through line 94 to exchange heat with the second flow hydroblasting raw materials passing through the pipe 90. The second output stream products hydrobromide transported through the pipeline 94, can be divided in the second cold separator 96 to obtain vaporous second exit stream products hydrobromide containing hydrogen, in the head pipe 98 and the second liquid flow products hydrobromide in the bottom of the pipeline 100.

The second cold separator 96 can operate in temperatures from 46° to 63°C (115° to 145°F) and a pressure slightly below the pressure in the second reactor 92 hydrobromide, taking into account the differential pressure to maintain the hydrogen and light gases in the main stream and normally liquid hydrocarbons in the bottom stream. The water stream can be removed from the sump of the second cold separator 96 through line 102.

PA is obrazny second output stream products hydrobromide, containing hydrogen passing through the head pipe 98 may be directed to recirculated and added to the flow of make-up hydrogen passing through the pipe 20 upstream of the second compressor. In the embodiment with the "recirculation" shown in Fig.1, vaporous second output stream products hydrobromide containing hydrogen transported by pipeline 98, add in point 25 of the connection piping to the flow of make-up hydrogen is transported through the pipeline 20, upstream from the first compressor 22. Make-up gas in the pipe 20 and the recirculation gas in the pipe 98 are combined and sent to the pipeline 26, then mixed and sent to the compression, as described above. Accordingly, the first compressor 22 and the second compressor 32 downstream communicated with the head pipe 98.

Liquid second output stream products hydrobromide passing through the pipeline 100 may be fractionated in the column 104 fractionation, which can be a Stripping column. Thus, before its submission to the Stripping column 104 second liquid exit stream products hydrobromide transported by pipeline 100 may be heated. The specified second liquid exit stream products hydrobromide can be Oparin in the Stripping column 104 using odango pair, supplied from the pipeline 110, to receive the stream of naphtha and light fractions discharged through the head pipe 112. The product stream can be withdrawn through the bottom pipe 114. In one embodiment, the product stream is a stream of diesel fuel that contains sulfur in a quantity of less than 50 wppm, qualifying as LSD, and preferably less than 10 wppm, qualifying as ULSD. It is assumed that a Stripping column 104 can operate as a column fractionation using boiler (reboiler) instead of using steam for steaming.

Due to the recirculation of hydrogen from the second installation 14 hydrobromide back to the discharge side of the first compressor 22 second set hydrobromide can work without a compressor for recirculation of gas. Recirculating the hydrogen from the second system 14 for hydrobromide subjected to additional compression and is used in the first installation 12 for hydrobromide.

In Fig.2 shows the embodiment of "recycling" device and method 8', in which the recirculation of the vapor of the second exhaust products hydrobromide pipeline 98' second compressor 24' and used the hot separator upstream from the first cold separator. Many of the elements shown in Fig.2, have the same design, is then shown in Fig.1, and denoted by the same reference numbers positions. The elements of Fig.2, which correspond to elements in Fig.1, but are designed differently denoted by the same numbers position as in Fig.1, but is indicated by the symbol in the form of a dash ('). The embodiment in Fig.2 differs from that shown in Fig.1 scheme of the compressor section 10' and the first installation of 12' hydrobromide.

Compressor section 10' stream of make-up hydrogen in the pipe 20' to the make-up hydrogen is sent to the first compressor 22 to increase the pressure of the flow of make-up hydrogen and receiving the first flow of compressed make-up hydrogen in the pipe 24'. The first compressor 22 may be in the form of a number of sequentially installed compressors.

The separation device 27' mounted on a pipe 24' for the first compressed make-up hydrogen, provides the selection part of the compressed make-up hydrogen in the first branch 28' of the pipeline and the selection of the second part of the compressed make-up hydrogen in the second branch 30' of the pipeline. The second part of the compressed make-up hydrogen in the second branch 30' of the pipeline is directed to the second system 14 for hydrobromide. The connection 25' between the second branch 28' of the pipe and head pipe 98', conveying vaporous second output product is in hydrobromide, provides communication between the specified head pipe 98' and the first branch 28' of the pipeline. Valve, a second pressure that is installed on the first branch 28' of the pipeline, can equalize the pressure between the first compressed make-up hydrogen and vaporous second outgoing stream products hydrobromide to ensure supply and mixing of these two streams in the pipe 26'.

The mixture of the second part of the flow of compressed make-up hydrogen in the first branch 28' of the pipe and the vapor of the second exhaust products hydrobromide in the pipe 26' may be further compressed in the second compressor 32, which may be in the form of a number of sequentially installed compressors to produce in the pipe 34 of the second compressed make-up flow. Accordingly, the second compressor 32 downstream communicates with the main pipe 98', which directs the flow to bypass the first compressor 22.

The second stream of compressed make-up hydrogen passing through the pipe 34 may be combined with the recirculating flow of hydrogen passing through the pipe 56, to produce in the pipe 36 of the first stream of hydrogen for hydrobromide. The first stream of hydrogen for hydrobromide passing through the pipe 36, taken from the who stream of compressed make-up hydrogen, can be combined with the first stream of hydrocarbons to be transported through the pipe 38, for receiving the first stream of hydrocarbon feedstock to hydrobromide passing through the pipeline 40. The remainder of the embodiment of Fig.2 operates as in Fig.1, except as set forth below.

The second difference of the embodiment illustrated in Fig.2, shown in Fig.1, is to perform the first installation of 12' hydrobromide. The first installation of 12' hydrobromide may contain hot separator 120, which is downstream connected with the first reactor 42 hydrobromide through pipe 44' and provides a vaporous stream of hydrocarbons in the head pipe 122, and obtaining a liquid stream of hydrocarbons in bottom pipe 124. Hot separator 120 operates at a temperature of 177° to 343°C (350° to 650°F) and preferably at a temperature of 232° to 288°C (450° to 550°F). Hot separator can operate at a pressure slightly lower than in the reactor 42 hydrocracking, given the need for a differential pressure between them. Vaporous stream of hydrocarbons withdrawn through line 122 may be cooled before entering the first cold separator 46. Accordingly, the vaporous first output stream products hydrobromide can be divided in the first holo is a word separator 46 to receive the vaporous effluent stream of the products of hydrocracking, containing hydrogen transported by pipeline 48, and liquid exit stream of the products of hydrocracking in the pipeline 52. These flows are treated then as described above regarding the embodiment shown in Fig.1. In this regard, the first cold separator 46 downstream communicates with the main pipe 122 of the hot separator 120.

The liquid flow of hydrocarbons in bottom pipe 124 may be subjected to fractionation on a plot of 16' fractionation. According to one aspect of the liquid flow of the hydrocarbons passing through the pipeline 124, may be subjected to rapid evaporation in a hot pan drum 130, resulting in the receive stream of light fractions in the head pipe 132 and the flow of heavy liquid fractions in bottom pipe 134. Hot evaporative drum 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 in bottom pipe 134 may be subjected to a further fractionation on a plot of 16' fractionation. In accordance with one aspect of the liquid flow heavy fractions transported by pipeline 134 may be introduced to the Stripping column 70 at a lower level than the place of supply of liquid flow light f the shares, passing through the pipeline 62.

The remainder of the embodiment of the invention illustrated in Fig.2, may be the same as described in Fig.1, with pre-marked with the exception of the compressor section 10'. The embodiment of hot separator 120, just revealed in Fig.2, can also be used in the embodiment of Fig.1.

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 elaboration and research, using the above description of the invention, may use the present invention in its most complete. 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 proportions and percentages by weight, unless otherwise indicated. The pressure provided at the outlet of the columns and, in particular, the output steam flow from the columns having a number of output the s.

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

1. How hydrobromide two hydrocarbon streams, including
stream compression make-up hydrogen in the first compressor receiving the first stream of compressed make-up hydrogen;
compressing the first portion of the first compressed make-up hydrogen in the second compressor to obtain a second stream of compressed make-up hydrogen;
the selection of the second part of the first compressed make-up hydrogen as the second stream of hydrogen for hydrobromide;
hydrobromide first stream of hydrocarbons in the presence of the first stream of hydrogen for hydrobromide containing the second compressed make-up hydrogen, and the first catalyst hydrobromide with receipt of the first exhaust products hydrobromide;
hydrobromide second stream of hydrocarbons in the presence of the second stream of hydrogen for hydrobromide containing the first compressed make-up hydrogen, and the second catalyst hydrobromide to obtain a second exit stream about is aktov of hydrobromide;
split second specified output stream products hydrobromide obtaining second vaporous effluent product stream of hydrobromide; and
add the specified second vaporous effluent product stream of hydrobromide to the specified stream make-up hydrogen is higher in the course of the stream from the specified first compressor.

2. The method according to p. 1, wherein said first thread to hydrobromide subjected to hydrocracking in the presence of a hydrocracking catalyst, and the specified second thread for hydrobromide subjected to Hydrotreating in the presence of the Hydrotreating catalyst.

3. The method according to p. 1, further comprising fractionating at least a portion of the first exhaust products hydrobromide with receipt of the second stream of hydrocarbons, which represents the flow of diesel fuel.

4. The method according to p. 1, further comprising separating the first effluent product stream of hydrobromide on vaporous first output stream products hydrobromide containing hydrogen and liquid first output stream products hydrobromide; compression specified gaseous first effluent product stream of hydrobromide with getting re-circulating stream of hydrogen; adding the second compressed make-up hydrogen to the decree of the resultant vaporous first outgoing stream products hydrobromide or recirculating stream of hydrogen with receipt of the first stream of hydrogen for hydrobromide.

5. The method according to p. 1, further comprising separating the second effluent product stream of hydrobromide obtaining the second liquid exit stream products hydrobromide and subsequent fractionation of the specified second liquid exit stream products hydrobromide to obtain diesel fuel with low sulfur content.

6. Installation for hydrobromide two hydrocarbon streams containing:
the pipeline make-up hydrogen, designed for carrying the flow of make-up hydrogen;
the first compressor, which is communicated with the specified pipeline make-up hydrogen and is designed to compress the specified stream make-up hydrogen to obtain a first compressed make-up hydrogen;
a dividing device that communicates with a first compressor and serves to separate the specified first compressed make-up hydrogen for the first part, transported by the first branch pipe and a second part carried by the second branch of the pipeline;
the second compressor is connected with a first branch pipe and intended to compress the specified first part of the first compressed make-up hydrogen to obtain a second stream of compressed make-up of bodoro is in the second pipeline for compressed make-up hydrogen;
the first reactor hydrobromide which is connected with a first branch of the pipeline, designed to hydrobromide first stream of hydrocarbons;
the second reactor hydrobromide which is connected with the specified second branch of the pipeline, designed to hydrobromide second stream of hydrocarbons;
the separator which is connected with the specified second reactor hydrobromide designed for separating the second effluent product stream of hydrobromide obtaining second vaporous effluent product stream of hydrobromide containing hydrogen passing through the head pipe;
moreover, the specified second compressor is communicated with the specified head pipe; and said first compressor is communicated with the specified head pipe at the point of connection on the specified pipeline make-up hydrogen.

7. Installation according to p. 6, further containing a cold separator which is connected with the specified second reactor for hydrobromide designed for separating the second effluent product stream of hydrobromide on vaporous second output stream products hydrobromide containing hydrogen is transported through the head pipe, and the second liquid exit stream products hydrobromide, in bottom lines when it specified the Torah compressor is communicated with the specified head pipe at the point of connection on the specified second branch of the pipeline.

8. Installation according to p. 6, in which said first reactor hydrobromide is a hydrocracking reactor, and the specified second reactor hydrobromide is a hydrotreater unit.

9. Installation according to p. 6, further containing a column fractionation, which is reported with a specified bottom piping and is designed for fractionation of the specified second liquid exit stream products hydrobromide and obtain fractions of diesel fuel.



 

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Fuel compositions // 2443762

FIELD: machine building.

SUBSTANCE: method for reducing the adverse effect of detergent additive on cold flow of fuel composition containing distillate fuel, detergent additive and additive improving the cold flow, which involves introduction to the above composition of additional additive chosen from: (a) acids and their mixtures; and (b) additives improving the lubricating capacity. Also, there proposed is the method for improvement of cold flow of fuel composition, method improving the detergent additive concentration in fuel composition, method for obtaining fuel composition, method for reducing the amount of additive improving the cold flow and operating method of the fuel consumption system.

EFFECT: improvement of service performance of cold flow of fuel composition containing distillate fuel, detergent additive and additive improving the cold flow.

26 cl, 7 ex, 10 tbl

FIELD: organic chemistry.
SUBSTANCE: invention refers to using a flocculating and sequestering agent with the organic solution as an agent to facilitate such purification. A method of purifying an organic solution, comprising contacting a flocculating and sequestering agent with the organic solution, which organic solution comprises fatty acid alkyl esters, wherein the water content of the organic solution is equal or less than 5% by weight, when the pH in the organic solution is 9 to 12, wherein the flocculating and sequestering agent is chosen from polyaluminium coagulants. There is provided a process for purification of an organic solution of fatty acid alkyl esters suitable for use as biodiesel, comprising: adding a flocculating and sequestering agent chosen from polyaluminium coagulants to the organic solution so as to facilitate the purification when the pH in the organic solution is 9 to 12 and removing a portion from the organic solution, which portion comprises the flocculating and sequestering agent, and impurities, wherein the water content of the organic solution is equal or less than 5% by weight.

EFFECT: process will enable less energy input and becomes less time-consuming and less costly, as compared to the known processes using water to purify the organic solution.

10 cl, 3 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: method involves preparation of plant oil with heating to 80°C, alkaline ethanolysis using potassium hydroxide in ethanol with molar concentration of 2 mol/dm3 to obtain an ether-glycerine mixture which is separated to form two fractions - glycerine and a mixture of ethers. The mixture of ethers (biodiesel fuel) undergoes filtration, sorption purification and dehydration. The obtained biodiesel fuel is stored. Preparation of the plant oil is carried out such that before heating, the plant oil is mixed with 1% aqueous solution of an Ecofriend enzyme-probiotic preparation and the obtained mixture is held for 24 hours at temperature 23-27°C. After holding for 24 hours, the mixture of plant oil and this preparation is heated to said heating temperature. The products are taken in the following ratio, pts.wt: plant oil 5; 1% aqueous solution of Ecofriend enzyme-probiotic preparation 5; potassium hydroxide in ethanol 5.

EFFECT: method increases the amount of the obtained biodiesel fuel.

2 tbl, 3 ex

Gas-oil composition // 2429281

FIELD: chemistry.

SUBSTANCE: gas-oil composition includes a gas-oil composition and additives added in the following steps 1 and 2 and containing a synthetic base FT in amount of 60 vol. % or more with respect to total amount of the gas-oil composition, with weight content of sulphur equal to or less than 5 parts per million, content of aromatic compounds equal to less than 10 vol. %, content of oxygen equal to or less than 100 parts per million, final temperature of 360°C or lower, insoluble residue after oxidation resistance test equal to less than 0.5 mg/100 ml, wear spot diameter HFRR (WS1.4) equal to less than 400 mcm and specific ratio of content of normal paraffins and their overall content, (step 1) a lubricity additive containing a fatty acid and/or fatty acid ester is mixed in amount of 20 mg/l or higher and 300 mg/l or less in units of the active component with the gas-oil composition through flow mixing, forced mixing or settling the mixture for a suitable period of time; and (step 2) an additive which enhances fluidity at low temperature, which contains a copolymer of ethylene vinyl acetate and/or a compound having surface activity, is mixed in amount of 20 mg/l or more and 1000 mg/l or less in units of the active component, with the gas-oil composition through flow mixing, forced mixing or settling the mixture for a suitable period of time.

EFFECT: gas-oil composition having low-temperature properties and having low fuel consumption characteristics, is suitable for use during winter.

5 cl, 6 ex, 8 tbl, 1 dwg

FIELD: oil and gas production.

SUBSTANCE: invention refers to composition of gas-oil for utilisation in diesel engine with degree of geometric compression 16 or less equipped with supercharger and EGR containing synthetic base oil FT and content of sulphur 5 mln p. by weight or less, content of oxygen 100 mln p. or less, modulus of volume deformation 1250 MPa or more and 1450 MPa or less, colour by Saybolt +22 or more, lubricating capacity 400 mcm or less, initial boiling point 140°C or more and end boiling point 380°C or less in parametres of distillation and following properties (1)-(3) of fraction of each interval, where (1) cetane number of fraction in interval lower, than 200°C amounts to 40 or more and less, than 60; (2) cetane number of fraction in interval 200°C or more and less, than 280°C amounts to 60 or more and less, than 80; and (3) cetane number of fraction in interval from 280°C or more amounts to 50 or more.

EFFECT: production of fuel of high quality facilitating excellent operation properties, and environment safe which can be utilised at combustion with compression inflammation of homogenous medium.

7 cl, 12 ex, 12 tbl, 1 dwg

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

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: 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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