Installation and method for isomerisation of hydrocarbon flow

FIELD: chemistry.

SUBSTANCE: invention refers to an installation for the isomerisation of a hydrocarbon flow rich in hydrocarbon C4 and/or at least one of hydrocarbons C5 and C6. The installation comprises: A) a container, which comprises a fluid containing a hydrogen-rich gas; B) a device for displacing the above fluid flow receiving the fluid containing the hydrogen-rich gas from the above container; C) at least one drier receiving the fluid containing the hydrogen-rich gas from the above device for displacing the fluid; the above at least one drier operates in the first mode to dry the fluid containing the hydrogen-rich gas and in the second mode in the regeneration environment performed by means of a regenerant; D) a reactor connected with at least one drier for receiving the fluid containing the hydrogen-rich gas; at least one drier is connected to the above container by at least supplying the fluid containing the hydrogen-rich gas, or the regenerant through a flow orifice at least for the flow regulation and/or decrease in the pressure of the regenerant supplied into the above container. The invention refers to a method.

EFFECT: using the present invention enables reducing the undesired effect following the regeneration of the gas drier preventing functional failures of downstream equipment.

9 cl, 4 dwg

 

The technical field to which the invention relates.

The present invention relates to an apparatus and method for isomerization of the flow of hydrocarbons.

The level of technology

Isomerization of light paraffins in many cases provide for increasing the octane number of gasoline. Typically, such methods isomerization is performed with a separate fractions of light hydrocarbons. As an example, the isomerization of butane or pentane and/or hexane (hereinafter may be called for short the isomerization of pentane-hexane) is conducted with the aim of improving the quality of gasoline in a separate device for isomerization. Typically, the isomerization of butane and pentane-hexane is carried out in a process of liquid/steam or steam phase in a fixed bed of catalyst. In the reactor can do the feedstock of light paraffins, mixed with gas containing significant amounts of hydrogen.

When isomerization of butane or pentane-hexane water is a harmful substance, which can reduce the service life of the catalyst in the reactor. Therefore, it is desirable to remove the water before rich hydrogen gas and/or paraffin feedstock will be available in the reactor. Therefore, usually as a source of raw materials, and the specified gas to remove the water is passed through a separate apparatus for the dehydration (drying).

In many cases, both the use of the dehydrator when placing them in series or parallel with the alternate operations of regeneration, regardless of whether the processed fluid medium gas, rich in hydrogen, or a hydrocarbon containing butane or pentane and butane. Accordingly, one dehumidifier can operate, while the other desiccant may be in the process of regeneration. At the final stage of regeneration of the desiccant may be a liquid regenerating agent, if the desiccant is a desiccant hydrocarbon or gaseous regenerating agent, if the dryer is a gas dryer. Depending on the hydrocarbon fraction, which is subjected to isomerization, regenerating agent may include, mainly, the isomerized product, such as isobutane or at least one product from isopentane and methylpentane or Dimethylbutane (which hereinafter may be called the isopentane-isohexane); or regenerating agent may include a mixture of one or more different compounds with branched-chain, compounds are of normal structure and cyclic compounds. In another example, as a rule, regenerating agent out of the dryer before the regenerated desiccant actuate, or as you enter the desiccant in action. Regenerating agent is normally sent to the reactor.

Regenerating agent, gaseous or liquid, may vyzyvaet the violations in the work published after his technological devices. In particular, gaseous regenerating agent can cause a drop in temperature of the reaction, as this regenerating agent replaces the hydrogen used in the reactor, and violates the molar ratio of hydrogen-hydrocarbon in the reactor. In addition, the liquid regenerating agent can cause a drop in temperature in the reactor during replacement of the reagent, namely raw materials containing paraffin hydrocarbons. In addition, normally gaseous regenerating agent has a greater molecular weight than the gas rich in hydrogen. As a result, the replacement of gas rich in hydrogen, can disrupt the regulation of gas flow, namely the flow rate of feed gas, and upset the regulation of the pressure in a distillation column, which is usually used after the reactor. Thus, there is a need to mitigate the above undesirable effects after regeneration of the desiccant gas in order to prevent disruption posted by downstream devices.

The invention

One example embodiment may be setup for isomerization stream of hydrocarbons rich in a C4 hydrocarbon and/or at least one of the hydrocarbons C5 and C6. The installation may include: a vessel containing a fluid medium containing at least one reagent; device is isto to move the fluid, receiving from a specified capacity specified fluid medium containing at least one reagent and at least one desiccant receiving the fluid containing at least one reagent from the specified device to move the fluid; and a reactor which is connected, at least one drier for receiving a fluid medium containing at least one reagent. In addition, the at least one desiccant can be reported with a specified capacity, at least by means of a flow of a fluid medium containing at least one reagent or regenerating agent through a narrowing device for the fluid. Specified narrowing device for a fluid medium can flow regulation and/or reducing the pressure regenerating agent acting in a specified capacity. The specified at least one desiccant, can operate in the first mode for drying a fluid medium containing at least one reagent, and in the second mode in the conditions of regeneration by using a regenerating agent.

Another example embodiment of the invention may be a method for regenerating at least one desiccant installation for isomerization stream of hydrocarbons rich in a C4 hydrocarbon and/or rich in at least one of the hydrocarbons C5 and C6. Indicated the p method may include: regeneration, at least one dryer by using a regenerating agent, with the specified at least one desiccant contains the used regenerating agent; and a recirculation of the used regenerating agent upstream from the specified at least one drier for mixing for a period of time sufficient to dilute the used regenerating agent fluid medium containing at least one subject-dehydration reagent, to minimize violations when conducting one or more transactions below along the flow path.

Another example embodiment of the invention may be a method for regenerating at least one zone of the drying installation for isomerization stream of hydrocarbons. The method may include recycling used regenerating agent, rich in C4 hydrocarbon and/or rich in at least one of the hydrocarbons C5 and C6, upstream of at least one drying zone for mixing for a period of time sufficient to dilute the used regenerating agent fluid medium containing at least one subject-dehydration reagent to minimize irregularities in the conduct of one or more process operations below along the flow path.

T is thus, disclosed here, the embodiment can minimize violations in the operations below in the direction of flow from a zone of drying fluid environment by recycling used regenerating agent in the direction upstream from the drying zone. Used regenerating agent can be passed through a narrowing device for the fluid in order to provide dilution used regenerating agent flowing fluid medium to be dehydrated.

Definition

Used in the present description, the term "stream" can mean a stream containing molecules of various hydrocarbons such as alkanes, alkenes, alkadienes and alkynes with normal unbranched chain, branched or cyclic structure, and optionally other substances such as gases, for example hydrogen, or impurities, for example, heavy metals, and compounds of sulfur or nitrogen. The specified stream may also contain aromatic or not aromatic hydrocarbons. In addition, the hydrocarbon molecules can be abbreviated designated as C1, C2, C3..., JV, where n is the number of carbon atoms in the hydrocarbon molecule. In addition, the term "hydrocarbon SP-SP+1", for example, hydrocarbons, C5-C6" can mean at least one of the hydrocarbons C5 and C6.

Used herein, the term "area" may refer to some areas and, containing one or more units and/or one or more subbands. Equipment may constitute one or more reactors or tanks, reactors, heaters, separators, heat exchangers, piping, pumps, compressors and regulators. In addition, equipment such as the reactor, dehumidifier, or capacity can also form one or more zones or subzones. It should be understood that each zone can contain a greater amount of equipment and/or containers than shown in the figures.

Used in this description, the term "narrowing device for fluid" generally means a device that, at least, directly or indirectly regulates the flow or reduces the pressure of the fluid. Usually narrowing device for the fluid reduces the flow of the fluid as compared with the absence of the orifice, for example in the pipeline, and may be due to the decrease of the cross section to regulate the flow of fluid, and not to interrupt the flow of fluid. An example of such orifice for the fluid can serve as a restrictive orifice or controller, such as controller with indication of the differential pressure regulator with pressure indicator, regulator with display of flow rate, flow indicator or indicator giving is to be placed, usually consistently acting jointly with one or more other devices, such as control valve or restrictive orifice. Examples of the implementation of contractions for the fluid may include a combination of two or more elements, such as restrictive orifice, flow indicator, regulator with display differential pressure regulating valve; or acting jointly regulator with flow indication and control valve. Narrowing device for a fluid medium may be installed on one or more pipelines to change the flow rate of fluid or pressure.

Used herein, the term "device for moving fluid" generally means a device for transporting a fluid medium. Such devices are pumps that are used, usually for liquids, and compressors, usually for gas.

Used herein, the term "rich" can generally mean the content in the stream, at least 50% and preferably 70% (molar content) compounds or groups of compounds in the stream.

Used herein, the term "mainly" can generally mean at least 90%, preferably 95%, and optimally 99% (molar content) compounds or groups of compounds in the stream.

Use is used here, the term "absorption" can refer to the ability to retain the material in the layer, containing the absorbent and/or adsorbent, due to chemical or physical interactions between matter such as water, and a layer, and includes, but is not limited to absorption and/or adsorption. Removal of substances from the adsorbent can be referred to here as "desorption".

Used herein, the term "used regenerating agent" can refer to a regenerating agent, which has already been used for drying or deformirovaniya, or which has been passed through one or more devices or pieces of equipment, such as a dehumidifier. Used regenerating agent may contain or may not contain desormiere substance, such as water, but it is possible that the used regenerating agent is in the apparatus, once placed inside the unit work item, for example a molecular sieve, was regenerated.

Used herein, the term "coupled" may mean that two elements are directly or indirectly articulated, bonded, connected, joined or formed together as a single unit by means of chemical or physical means using technological processes, such as stamping, casting or welding. In addition, two elements can be connected with the third element, such as a fastening element, such as a screw, spilk is, clip or rivet; or by using an adhesive or solder.

Brief description of drawings

Fig.1 is a schematic diagram of an example installation for the isomerization of fluid.

Fig.2A is a schematic diagram of a first example of the device for draining fluid.

Fig.2B is a schematic diagram of a second example of the device for draining fluid.

Fig.3 is a schematic diagram of the third example of the device for draining fluid.

Detailed description

In Fig.1 shows the installation of 100 for isomerization stream of hydrocarbons. In the installation 100 may receive fluid medium containing at least one reagent 110, passing through the pipeline 210 or pipeline 410. Normally fluid 110 can be a liquid stream of hydrocarbons in the pipeline 210 or rich in hydrogen gas in the pipeline 410. Liquid flow of hydrocarbons can be stream rich in C4 hydrocarbons, such as butane, if the installation 100 is setup for the isomerization of C4 hydrocarbons. Alternatively, the liquid flow of hydrocarbons can be rich in hydrocarbons, C5-C6, such as pentane-hexane, if the installation 100 is a unit for isomerization of hydrocarbons C5-C6. Typical installation of both types are disclosed, for example, in source: Nelson A. Cusher, UOP Butamer Process and UOP Penex Process of the Handbook of Petroleum Refining Processes, Third Edition, Robert A. Meyers Editor, 2004, page 9.7-9.27. However, in some examples of embodiment of the installation 100 can also be used for the simultaneous isomerization of flow of one or more of butane, one or more of pentane, and one or more hexanol. It should be noted that isomerization reactions include reactions in which the quality of raw materials used mainly normal paraffins and isomerization product - branched paraffins, and such reactions, in which as a feedstock predominantly use highly branched paraffins, and as a product of isomerization of normal paraffins. In other words, the liquid flow of hydrocarbons can be rich in isobutane or branched hydrocarbons C5-C6. Other isomerization reactions, with the participation of hydrocarbons, C4, or C5-C6, are also within the scope of the present invention.

To simplify the following disclosure of the invention, the term "liquid hydrocarbon" and "regenerating agent" may refer to a generalized terms, and you need to understand that they are applicable, for example, to install for the isomerization of C4 hydrocarbon or installation for the isomerization of hydrocarbons C5-C6. As an example, the flow of hydrocarbons rich in a C4 hydrocarbon, may be subjected to isomerization reactor for isomeri the emission of hydrocarbons C4, and the product containing isomerized hydrocarbons C4, can be used as a regenerating agent in the isomerization of C4 hydrocarbons. Similarly, the flow of hydrocarbons, rich in hydrocarbons, C5-C6, can be Samaritan in the reactor for isomerization of hydrocarbons, C5-C6, and a product containing samaritane hydrocarbons, C5-C6, can be used as a regenerating agent in the isomerization of hydrocarbons C5-C6.

Installation 100 may contain one or more containers 130, one or more devices 140 to move the fluid, one or more zones 150 drying, and one or more technological devices 160 that are located below in the direction of flow. One or more containers 130 may include a surge tank 230 or receiving tank 230 distillation column (hereinafter, such capacity may be collectively called surge capacity 230) serving to receive the flow of hydrocarbons, and the capacity of 430 suction (compressor), which provides for receiving gas, rich in hydrogen, for example, a recirculating flow of hydrogen gas.

One or more devices 140 to move the fluid may include a pump 240 for receiving the flow of hydrocarbons from ravnitelnaya 230, and the compressor 440 for receiving gas rich in hydrogen from the tank 430 suction. One or more zones 150 drying may include an area of 250 dehydration fluid, which makes the liquid flow of hydrocarbons pumped by pump 240, and an area of 450 gas drying, which takes gas from the compressor 440.

In General, a balance tank 230, the pump 240 and area 250 dehydration of the liquid part of the first device 200 for draining the fluid. Typically, the liquid flow of the hydrocarbon flows through the pipeline 210 and out through the pipe 310. In addition, the capacity of 430 suction, compressor 440 and area 450 of the drying gas are included in the second device 400 for draining the fluid. Typically, the gas flows through the pipeline 410 and exits through the pipe 510. Both devices 200 and 400 will be described in detail below.

One or more technological devices 160, placed downstream, can be separated with the formation of the reaction zone 170 and the fractionation zone 180, which can be technological operations provided below in the direction of flow. After exiting areas 250 and 450 drying a stream of hydrocarbon gas rich in hydrogen can be combined in the reaction zone 170. The reaction zone 170 may include a first reactor 172 and the second reactor 174 posted sequence is correctly with the first reactor 172. Although the figure shows only the first reactor 172 and the second reactor 174, it should be understood that the reaction zone 170 may also contain other equipment or other containers, as for example, one or more heaters, compressor recycle gas separation capacity and additional reactors. Alternatively, the reactor 172 and 174 may be included in one operation. The stream resulting from the reaction zone 170 may flow through the pipe 176 to the zone 180 fractionation.

Area 180 fractionation may contain distillation column 192, producing one or more of the separated products 182. Although in Fig.1 shows one distillation column 192, installation can be used two or more distillation columns arranged in series and/or parallel. One or more of the separated products 182 may include a first product comprising one or more gaseous products sent, for example, combustible gas by pipeline 184, and a second or isomerized product transported by pipeline 186. Some portion of the second product can be designated by a pipe 188 and used as a regenerating agent. Used regenerating agent can be returned back to isomerise the bath product flowing in the pipe 190, as will be describe below. The combined stream may be directed into the storage tank isomerizing product in a distillation column or other technological device.

In Fig.2 presents the first device 200 for draining the fluid. Specified, the first device 200 for draining the fluid medium can be used for dehydration of liquid flow of hydrocarbons, typically representing a stream of light normal paraffins. Usually, the first device 200 for draining the fluid medium contains a balance tank 230, the pump 240, at least one drier 254, one or more valves 260, convergent device 290 for the fluid and the heater 300.

Preferably, at least one drier 254 includes a first desiccant 256 fluid and the second desiccant 258 fluid. These dehumidifiers 256 and 258 can be located in an area of 250 dehydration fluid, as shown in Fig.1. In addition, each drier 256 and 258 may contain molecular sieve, which is the absorption of water, and appropriate internal zone or sub-zone drying. Typically, each drier 256 and 258 operates in the first mode to dry the flow of hydrocarbons passing through the drier, and in the second mode to regenerate the desiccant. As the government is about, these dehumidifiers 256 and 258 may be placed sequentially and regenerated alternately when operating in the drying mode other desiccant.

One or more valves 260 may include a valve 262, the valve 264, the valve 264' valve 266, the valve 268, the valve 270, the valve 270', the valve 272, the valve 274, the valve 276, the valve 278, valve 280, the valve 282 and valve 284. Various combinations of valve 260 can be opened and closed in order to direct the process flow for implementing the first and second modes of operation of the dryers.

In this example embodiment of the convergent device 290 for the fluid may include a display controller 292 flow interacting with a control valve 294, and can adjust the flow and reduce the pressure of the regenerating agent. The heater 300 may include a steam heater 304 and the superheater 308, intended for heating the regenerating agent in order to ensure the functioning of the desiccant in the second mode - the mode of regeneration of the desiccant. In particular, a steam heater 304 can be used for evaporation of the regenerating agent before you raise with superheater 308 temperature regenerating agent to a temperature sufficient to deformirovaniya water from the molecular sieve desiccant 256 or 258.

In the bottom example of the operation of the regeneration fluid stream of hydrocarbons can be transported by pipeline 210 in a balance tank 230. After that, the liquid flow of the hydrocarbons can flow into the pump 240 and then in the first drier 256 or second desiccant 258. Typically, the liquid flow of hydrocarbons is fed into one of the dryers, for example, passes through the valves 278 and 280 in the drier 258 to remove the water. Then dehydrated liquid flow of hydrocarbons may pass through the valves 272 and 268 and pipeline 310 in the reaction zone 170, shown in Fig.1. Typically, the liquid flow of hydrocarbons dehydrate in a dehydrator 258 with closed valves 266, 270, 270' and 276, while the valves 278, 280, 268 and 272 are opened.

All this time the other drier 256 gas may be in the regeneration mode. Typically, the regeneration is a multi-stage process that uses liquid regenerating agent coming from the pipe 188, shown in Fig.1, directed to the heater 300. In the process of regeneration regenerating agent may be gradually heated, first through a steam heater 304 and then use as a steam heater 304 and superheater 308, and the heating is carried out up until the specified regenerating agent will not be heated to a temperature sufficient to deformirovaniya water from the molecular sieve. Usually regenerating agent flows through the steam heater 304, superheater 308 and then by pipeline 288, about the odya through the valve 282, comes up drier 256. Regenerating agent may sequentially pass through the drier 256, the valve 284 and line 298, before it is cooled using, for example, cooling water heat exchanger. Then regenerating agent may be returned through pipe 190 to samaritana product, as shown in Fig.1.

Then regenerating agent is slowly cooled through first off superheater 308 and then steam heater 304, but at the same time, there is a continuous passage of the regenerating agent through the drier 256. Thus, the drier 256 and associated equipment can be gradually cooled to provide a slow temperature decrease. At the end of the regeneration process in the drier 256 is typically liquid regenerating agent.

In the case of liquid flow of hydrocarbons used regenerating agent can be directed from the dryer 256 up to the pipeline 286 through the open valves 262 and 264, as shown in Fig.2A. Alternatively, when using a liquid flow of hydrocarbons used regenerating agent can be directed from the dryer 256 down through the open valves 274 and 264 to the pipeline 286, as shown in Fig.2B. Used liquid regenerating agent can flow through the PE ulator 292 with consumption display, interacting with the control valve 294. Typically, the control valve 294 regulates the flow of liquid returned in a balance tank 230 or before it. When passing the used regenerating agent through the control valve 294 pressure fluid medium can be reduced so that it is passing in a balance tank 230. Typically, there is a large pressure difference used regenerating agent to control valve 294 and in a surge tank 230. The use of control valve 294 to reduce the pressure used regenerating agent can prevent "blow-in" surge capacity 230. It is often desirable not only to regulate the flow rate used regenerating agent, but also to reduce its pressure. Adjusting the return of the used regenerating agent in the balance tank, you can mix and dilute the used regenerating agent fluid medium flowing in a pipeline 210, to reduce the adverse effects of the regenerating agent held on downstream manufacturing operations and downstream equipment and/or capacity, for example, technological devices 160 that are included with the devices of the reaction zone 170 and zone 180 fractionation shown in Fig.1. Although it was the decree is but to use a controller with indication of the flow-regulating valve, it should be understood that can be used and other types of contractions for a fluid medium, such as a restrictive orifice or device of another type. In addition, during the flow of the used regenerating agent back to the balance tank 230 can be calculated period of time to achieve the desired dilution regenerating agent. The controller 292 flow can be adjusted to increase or decrease the flow of regenerating agent passing through the control valve 294. Usually, the presence of orifice 290 for a fluid medium, such as a control valve 294, can reduce the amount of liquid returned back to the balance tank 230, compared to the amount of liquid returned back in the absence of the orifice.

As mentioned above, the desiccant 258 may operate in the first mode, and the other drier 256 can operate in the second mode. You should take into account that in Fig.2A and 2B presents only a concept, and additional piping and/or valves can be used to ensure operation of the drier 256 in the first mode, the desiccant 258 in the second mode, and both dryers with serial connection. As an example, dehumidifiers 256 and 428 after regeneration can be returned is back in the sequential mode of operation, for example, so that the drier 256 functioned with a time lag relative to the desiccant 258.

In Fig.3 presents a second device 400 for draining the fluid. The specified second device 400 for draining the fluid medium can be used for drying a gas stream, for example, a gas stream rich in hydrogen. Usually the second device 400 for draining the fluid medium contains a capacity of 430 suction, compressor 440, at least one drier 454, one or more valves 460, convergent device 490 for the fluid and the heater 500. The second device 400 for draining the fluid may also contain other narrowing device 590 for the fluid, which can be used in the alternative embodiment described below.

Preferably, at least one drier 454 includes a first desiccant 456 gas and the second desiccant 458 gas. These dehumidifiers 456 and 458 can be part of the zone 450 gas drying, shown in Fig.1. In addition, each drier 456 and 458 may contain molecular sieve, which is the absorption of water, and includes an appropriate internal zone or sub-zone drying. In General, each drier 456 and 458 operates in the first mode for drying gas, rich in hydrogen, passing through the drier 456 or 458, and in the second mode, DL is the regeneration of the desiccant 456 or 458. Usually these dehumidifiers 456 and 458 are placed sequentially and regenerated alternately when operating in the drying mode other desiccant.

One or more valves 460 may include a valve 462, valve 464, valve 466, valve 468, valve 470, valve 472, valve 474, valve 476 valve 478, valve 480, valve 482, valve 484, valve valve 550 and 554 and the valve 562. Various combinations of valves 460 can be opened and closed in order to direct the process flow in the implementation of the first and second mode of operation of the dryers.

In this example embodiment of the narrowing device 490 for the fluid may contain restrictive opening 492 and indicator 494 consumption, and can reduce consumption and to reduce the pressure of the regenerating agent. The heater 500 may contain steam heater 504 and the superheater 508 to heat regenerating agent in the operation of the desiccant in the second mode - the mode of regeneration of the desiccant. In particular, a steam heater 504 can be used for evaporation of the regenerating agent before the superheater 508 will heat regenerating agent to a temperature sufficient to remove water from the molecular sieve desiccant 456 or 458.

In one example of operation of the regeneration gas, for example gas, rich in hydrogen, can postupat the pipeline 410 in the capacity of 430 suction. Then, this gas can consistently held to the compressor 440 and one of the dehydrators 456 and 458. As an example, the gas through the valve 478 and 480 may enter the dryer 458 for deformirovaniya water. After that, the dried gas through the valves 472 and 468 can be carried in the pipeline 510 for its Association with the liquid flow of hydrocarbons before entering the reaction zone 170, as shown in Fig.1. Typically, the gas stream is dried in the drier 458 with closed valves 466, 470, 474, and 476, while the valves 478, 480, 468 and 472 are open.

All this time the other drier 456 gas may be in the regeneration mode. Typically, the regeneration is a multi-stage process that uses liquid regenerating agent coming from the pipe 188, shown in Fig.1, directed to the heater 500. In the process of regeneration regenerating agent may be gradually heated, first through a steam heater 504 and then use as a steam heater 504 and superheater 508, and the heating continues as long as the regenerating agent will not be heated to a temperature sufficient to deformirovaniya water from the molecular sieve. Usually regenerating agent flows through the steam heater 504, superheater 508 and then by pipeline 488 passing through the valve 482 comes up drier 456. Regen is yuushi agent may sequentially pass through the drier 456, the valve 484 and pipeline 498, before it is cooled using, for example, cooling water heat exchanger. After that, regenerating agent may be returned to the pipeline 190 to samaritana product, as shown in Fig.1. Valves 462,474, 476 and 562 in this case closed.

Then regenerating agent may be slowly cooled through first off superheater 508, but at the same time, there is a continuous passage of the regenerating agent through the drier 456. Thus, the drier 456 and associated equipment can be cooled to provide a slow temperature decrease. At the end of the regeneration process in the drier 456 usually is regenerating agent in the form of a gas.

When using a gas rich in hydrogen, is used regenerating agent can be directed from the drier 456 to 486 pipeline through the open valves 462 and 464 and 550 with a closed valve 554. Gas used regenerating agent can flow through the regulator 494 with indication of flow rate and bounding the hole 492. Usually restrictive orifice 492 reduces consumption and, in addition, reduces the pressure of the regenerating agent circulating back into the tank 430 on the suction or the pressure of the regenerating agent to the vessel 430 suction. Due to the pressure drop used the CSOs regenerating agent when passing through the restrictive orifice 492 reduced pressure to the desired level can prevent "blow-in" capacity 430 suction. In addition, it is often desirable to reduce the flow of regenerating agent in order to provide dilution (reduction) in the specified capacity 430 suction. Mixing the used regenerating agent supplied with fluid medium in the pipeline 410 allows to dilute the regenerating agent and to reduce its adverse impact on the downstream operations and downstream equipment and/or capacity, for example, on technological devices 160, is placed in the reaction zone 170 and 180 fractionation shown in Fig.1. Although it was stated above the use of the indicator 494 consumption and restrictive holes 492, it should be understood that they can be used and other types of contractions for a fluid medium, such as controller with indication of the flow interacting with a control valve or one or more devices of a different type. In General, the presence of the orifice 490 for a fluid medium, such as a restrictive orifice 492, can reduce the amount of gas that is returned back into the tank 430 suction, compared to the amount of gas returned back in the absence of restrictive openings.

By choosing the geometric dimensions of the bounding holes duration of recycling can be adjusted dragostinova dilution used regenerating agent in the vessel 430 suction before passing the diluted regenerating agent, at least through one of the dehydrators 454 and then into the reaction zone 170, as shown in Fig.1. By reducing flow and pressure used regenerating agent returned back into the tank 430 suction used regenerating agent may be diluted with other gases acting in the capacity of 430 pipeline 410. The result can be minimized unwanted effect of regenerating agent held on downstream operations and downstream equipment and/or technological devices 160, shown in Fig.1.

An alternative embodiment can prevent condensation and absorption regenerating agent at a molecular sieve in order to expedite removal of the used regenerating agent of the regenerated desiccant by reducing the pressure of gas rich in hydrogen supplied to the drier 456. In this example embodiment of the drier 456 at the end of the regeneration process typically contains the used regenerating agent in the form of gas. In the case of gas, rich in hydrogen, this gas can pass through the open valve 476 when the closed valve 474. The specified rich in hydrogen gas can be carried in the pipeline 564 and through a narrowing device 590 for a fluid medium containing the indicator 594 consumption and restrictive hole 592 delasnerie gas pressure. After that the gas can pass through the open valve 562 in the drier 456. Regenerating agent can be forced out of the drier 456 through the open valves 462 and 464. Then the valve 554 can be opened, and the valve 550 may be closed, so that the regenerating agent can be directed to bypass the convergent device 490 for the fluid through the pipeline 558 and comes in line 486. Then regenerating agent can be given to the capacity of 430 suction or collector or her. Thus, convergent device 590 for the fluid may indirectly regulate the flow and reduce the pressure used regenerating agent, and to maintain the pressure in the drier 456 below the saturation pressure used regenerating agent.

As mentioned above, the desiccant 458 may operate in the first mode, and the other drier 456 may operate in the second mode. You should take into account that additional piping and/or valves can be used to ensure operation of the drier 456 in the first mode, the desiccant 458 in the second mode and for both dryers with serial connection. As an example, dehumidifiers 456 and 458 after regeneration can be returned back in the sequential mode of operation, for example, so that the drier 456 functioned with zapustiv the deposits in time with respect to the desiccant 458.

Believe that the person skilled in the art from the above description, without further elaboration may use the present invention in its entirety. Disclosed above preferred specific embodiment, therefore, should be interpreted only as illustrative and in no way limiting the rest of disclosure.

In the above specification, all temperatures are not translated in degrees Celsius and all proportions and percentages are expressed in Mols unless otherwise noted.

From the above description, the specialist in the art can easily set the essential features of the invention and, without going beyond the scope and nature of the invention to make various changes and modifications of the invention in order to adapt it to different contexts and use cases.

1. Installation for isomerization stream of hydrocarbons rich in a C4 hydrocarbon and/or at least one of the hydrocarbons C5 and C6, containing:
A) a vessel containing a fluid containing gas, rich in hydrogen;
B) a device for moving a fluid medium, the host of the listed capacity on the specified fluid environment containing a gas rich in hydrogen;
C) at least one drier, receiving the fluid containing the gas rich in hydrogen from the specified y is trojstva to move the fluid, when this is specified at least one dehumidifier operates in the first mode for drying the fluid containing gas, rich in hydrogen, and in the second mode in the conditions of regeneration by using a regenerating agent;
D) a reactor which is connected to at least one drier for receiving the fluid containing gas, rich in hydrogen, at least one drier is reported with a specified capacity, at least by means of a flow of fluid containing gas, rich in hydrogen, or regenerating agent through a narrowing device for a fluid medium, at least to regulate the flow and/or decreasing the pressure regenerating agent acting in a specified capacity.

2. Installation under item 1, additionally containing a fluid line connecting the at least one dehumidifier with a specified capacity, thus narrowing device for a fluid medium is placed on the specified line and includes a restrictive orifice or control valve.

3. Installation under item 2, in which a narrowing device for a fluid medium includes or restrictive orifice, regulator with display of flow, interacting with regulating valve, or control valve.

4. Installation under item 1, in which the reactor includes at least one re is ctor isomerization of C4 hydrocarbons, C5 or C5 hydrocarbons and C6.

5. Installation under item 1, in which the capacity is a balance tank or receiving tank.

6. Installation under item 1, additionally containing a fractionation zone comprising at least one distillation column, receiving stream flowing from the reactor, and producing one or more separated products; and providing at least part of one of the separated products in at least one desiccant as a regenerating agent.

7. Installation under item 1, in which at least one desiccant posted molecular sieve.

8. Method for regenerating at least one desiccant installation for isomerization stream of hydrocarbons rich in at least one hydrocarbon selected from the group consisting of at least one C4 hydrocarbon, at least one C5 hydrocarbon, at least one C6 hydrocarbon, or mixtures thereof, including:
A) regeneration of at least one desiccant with a regenerating agent, and at least one desiccant is used regenerating agent; and
B) recycling the used regenerating agent to at least one drier for mixing within a period of time sufficient for razbam the texts used regenerating agent fluid medium, containing at least one subject of the drying gas, rich in hydrogen, to minimize irregularities in the conduct of one or more process operations below along the flow path.

9. The method according to p. 8, in which the specified fluid contains liquid, rich in C4 hydrocarbons, liquid, rich in at least one of the combinations of hydrocarbons C5 and C6, or a gas rich in hydrogen.



 

Same patents:

FIELD: oil-and-gas industry.

SUBSTANCE: invention relates to isomerisation of hydrocarbon flow rich in C4 and/or at least one of C5 and C6. Proposed plant comprises: first and second dehydrator adapted for intake of fluid including at least one reagent. Note here that said first dehydrator can operate in one reagent-fluid drying first mode. Second dehydrator can operate in second mode for recovery with the help of regenerating agent. Reaction zone is communicated with first dehydrator to receive fluid containing at least one reagent and with second dehydrator to receive regenerating agent. Note also that regenerating agent flows through fluid restrictor for adjustment of regenerating fluid flow rate to reaction zone. First pipeline feeds fluid bearing fluid rich on C4 and/or one of C5 and C6 from first dehydrator into reaction zone. Second pipeline communicates second dehydrator with reaction zone. Note here that said fluid restrictor comprises orifice or control valve connected with at least first or second pipeline. Besides, this invention relates to dehydrator recovery.

EFFECT: invention decreases undesirable effect of the gas dehydrator recovery that helps to keep the devices work properly.

6 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of isomerisation of light gasoline fractions, which consists of the preparation of straight-run and secondary gasoline fractions for isomerisation, with the further separation of raw isopentane in the first rectification column - deisopentaniser, after that, its supply to isomerisation in an isomerisation reactor with further release of gases and reflux in the second rectification column - debutaniser, from the bottom of which a stable isomerisate is supplied successively for the separation into the third rectification column for the separate extraction of isopentane and pentane and to the fourth rectification column for the separate extraction of isohexanes and hexane, side runs of the third and fourth rectification columns, containing respectively, pentane and hexane are recirculated for isomerisation into the isomerisation reactor. As a raw material used are straight-run and secondary gasoline fractions 40÷75…85°C, preparation and supply to isomerisation of the straight-run gasoline fraction 40÷75…85°C is carried out separately from the gasoline fraction 40÷75…85°C of the secondary processes of oil refining, with the gasoline fraction 40÷75…85°C of the secondary processes being supplied into the second or third rectification column.

EFFECT: application of the claimed method makes it possible to increase resources of the isomerisation process raw material due to the involvement into the process of the gasoline fraction of the secondary processes, output of target isohexanes, octane number of the isomerisate and isopentane fraction mixture and resources of high-octane semiproducts for compounding commercial gasoline.

5 cl, 3 tbl, 3 dwg

FIELD: chemistry.

SUBSTANCE: device contains the first drier and the second drier, adapted for the reception of a gaseous flowing medium, containing, at least, one reagent. The first drier is made with a possibility of functioning in the first mode of drying the flowing medium, which contains, at last, one reagent, and the second drier is made with a possibility of functioning in the second mode, under conditions of carrying out regeneration by means of a regenerating agent. it also contains a reaction zone, connected by means of the first pipeline to the first drier for the reception of the gaseous flowing medium, which contains, at least, one reagent; and a system of replacement of a regenerating agent in the direction from top to bottom, adapted for the supply and regulation of consumption or reduction of pressure of a part of the said gaseous flowing medium into the second drier, removal of the replaced regenerating agent from the second drier and technological operations, which are performed downstream, to minimise disturbances in the implementation of the said operations.

EFFECT: application of the claimed invention makes it possible to minimise disturbances in carrying out operations downstream.

10 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of separating an isopentane-pentane-hexane fraction during an isomerisation process, consisting of a first fractionation column for preparing material, from which the ballast product contained in the material is separated with the distillate. The residue from the bottom of the fractionation column is taken for conversion of pentanes and hexanes into isomers in an isomerisation reactor. Isomerisation products are fed into a second fractionation column for debutanisation, from where butane is removed from the top of the column and the isomerisation product is removed from the bottom of the column, said product containing reaction isomers obtained during the reaction, which are fed for separation into a third fractionation column for depentanisation, from which isopentane, recycled pentane and a hexane fraction are successively removed from the top. The recycled pentane is returned into the isomerisation reactor. The method is characterised by that the starting material used is a 75-85°C fraction of straight-run gasoline, and the ballast product removed from the top of the first fractionation column is isopentane contained in the material; reaction isopentane is removed from the top of the third fractionation column for depentanisation as a distillate or with the first side cut. Excess butane is removed as the distillate. Pentane is removed with the second side cut of the depentanisation column and fed into the isomerisation reactor as a recycle stream. A mixture of isohexane and normal hexane is removed from the bottom of the depentanisation column and then fed as material into an additional fourth fractionation column for deisohexanisation, from which the isohexane fraction is removed with the distillate and recycled hexane is removed with the side cut and then fed for re-conversion into the isomerisation reactor, and higher-boiling components are removed with the residue.

EFFECT: use of the present method enables to cut the amount of energy spent in the isomerisation process on producing isoparaffins, widens the range of products and provides flexibility of the process and purity of the end products.

2 cl, 4 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing alkylbenzine via alkylation of isobutane with olefins in a catalytic reactor at high temperature and pressure, where isobutane is fed into the top section of the reactor then successively passed through all sections with a catalyst, and olefin-containing material is distributed into several streams, the number of which is equal to the number of catalyst sections and then simultaneously fed into the section containing catalyst in parallel streams in order to conduct an alkylation reaction. A hydrocarbon stream containing unreacted isobutane and reaction products is divided into two streams: a vapour stream obtained by evaporating isobutane, which is then condensed and taken for recycling, and a liquid stream which is the reaction product coming from the reaction system or partially taken for recycling. Temperature and pressure in each reactor section is kept so as to ensure an equilibrium vapour-liquid state of the mixed hydrocarbon stream passing through the reactor. The olefins used in the method are C2-C4 olefins. The number of sections ranges from 2 to 10. Before entering the section containing catalyst, the olefin-containing stream is mixed with isobutane in ratio of 1:(250÷1000), and 50-99.9 wt % vapour stream from the overall stream coming out of the last reactor section is taken for recycling.

EFFECT: method enables to increase the cycle length of the catalyst and reduce power consumption.

4 cl, 8 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: at the first step, raw material containing at least one fatty acid, having 8-26 carbon atoms, is esterified with at least one fatty alcohol having 8-26 carbon atoms to obtain esters, at the second step, the obtained esters are hydrogenated to fatty alcohols, at the third step, the obtained fatty alcohols are dehydrogenated to alpha-olefins, at the fourth step, the alpha-olefins are oligomerised to oligomers which are then hydrogenated at the fifth step. The invention also relates to polyolefin base oil or a base oil component obtained using the described method.

EFFECT: invention enables to obtain branched saturated hydrocarbons from renewable sources.

15 cl, 5 tbl, 4 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a mixture of isoalkanes as oil bodies for cosmetic or pharmaceutical agencies, whose 1H-NMR-spectrum in the region of a chemical shift δ of from 0.6 to 1.0 ppm relative tetramethylsilane, has a surface integral of from 25 to 70% of the total integral surface. The mixture, which has density from 0.7 to 0.82 g/cm3, contains not less than 70 wt % alkanes with 8-20 carbon atoms, and the fraction of side chains with alkyl groups which have 2 or more carbon atoms is less than 20% of the total number of branching sites and is free from squalane. The invention also relates to a method of preparing said mixture, as well as a cosmetic or pharmaceutical agent based on said mixture and a hair cosmetic agent also based on said mixture.

EFFECT: improved method.

24 cl, 2 tbl, 809 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of processing mixtures of aliphatic alcohols containing glycerin in amount of 27-86 wt % via a cross-condensation reaction at temperature 300-350°C, inert gas pressure 1-5 MPa, specific speed of feeding the mixture of aliphatic alcohols per catalyst 0.4-0.8 dm3/h dm3 cat, where the catalyst used is tungsten oxide, rhenium oxide, deposited on γ-aluminium oxide, with the following ratio of components, wt %: tungsten oxide 1.2-6.7, rhenium oxide 0.9-1.3, γ-aluminium oxide - the rest.

EFFECT: use of present method increases output of alkane hydrocarbons and lowers output of gaseous products.

4 cl, 5 tbl, 12 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to heterogeneous catalytic conversion of organic compounds, specifically to catalytic conversion of a mixture of aliphatic alcohols to a mixture of alkane-olefin hydrocarbons, particularly C5-C8 hydrocarbons. Described is catalyst for synthesis of alkane-olefin hydrocarbons based on γ-aluminium oxide, distinguished by that, the catalyst contains tungsten oxide and rhenium oxide with the following ratio of components, in wt %: tungsten oxide 1.2-6.7; rhenium oxide 0-1.3; γ-aluminium oxide - the rest. Described also is a method for synthesis of alkane-olefin hydrocarbons with an even or combined even and odd number of carbon atoms through cross-coupling reaction of ethanol or its mixture with aliphatic alcohols in the presence of the said catalyst.

EFFECT: described catalyst enables to increase output of C5-C8 olefin-alkane fractions to 45% and reduce output of gaseous C1-C2 products to 30-35% with 85-95% conversion of initial alcohols.

5 cl, 5 tbl, 3 dwg, 9 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of processing products of fermentation of plant biomass to alkane hydrocarbons of the C4-C10 fraction through cross-condensation in the presence of a Fe2O3-MgO/Al2O3 and a Pt/Al2O3 catalyst in ratio Fe:Mg:Pt=13:2:1, at temperature 320-370°C, argon pressure 1-5 MPa and specific feed rate of starting material onto the catalyst equal to 0.4-0.8 dm3/h·dm3 catalyst.

EFFECT: use of the method reduces gas formation and increases output of saturated hydrocarbons.

1 cl, 9 ex, 3 tbl

FIELD: oil-and-gas industry.

SUBSTANCE: invention relates to isomerisation of hydrocarbon flow rich in C4 and/or at least one of C5 and C6. Proposed plant comprises: first and second dehydrator adapted for intake of fluid including at least one reagent. Note here that said first dehydrator can operate in one reagent-fluid drying first mode. Second dehydrator can operate in second mode for recovery with the help of regenerating agent. Reaction zone is communicated with first dehydrator to receive fluid containing at least one reagent and with second dehydrator to receive regenerating agent. Note also that regenerating agent flows through fluid restrictor for adjustment of regenerating fluid flow rate to reaction zone. First pipeline feeds fluid bearing fluid rich on C4 and/or one of C5 and C6 from first dehydrator into reaction zone. Second pipeline communicates second dehydrator with reaction zone. Note here that said fluid restrictor comprises orifice or control valve connected with at least first or second pipeline. Besides, this invention relates to dehydrator recovery.

EFFECT: invention decreases undesirable effect of the gas dehydrator recovery that helps to keep the devices work properly.

6 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: device contains the first drier and the second drier, adapted for the reception of a gaseous flowing medium, containing, at least, one reagent. The first drier is made with a possibility of functioning in the first mode of drying the flowing medium, which contains, at last, one reagent, and the second drier is made with a possibility of functioning in the second mode, under conditions of carrying out regeneration by means of a regenerating agent. it also contains a reaction zone, connected by means of the first pipeline to the first drier for the reception of the gaseous flowing medium, which contains, at least, one reagent; and a system of replacement of a regenerating agent in the direction from top to bottom, adapted for the supply and regulation of consumption or reduction of pressure of a part of the said gaseous flowing medium into the second drier, removal of the replaced regenerating agent from the second drier and technological operations, which are performed downstream, to minimise disturbances in the implementation of the said operations.

EFFECT: application of the claimed invention makes it possible to minimise disturbances in carrying out operations downstream.

10 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of isomerising normal butane containing initial material, containing at least 50 wt % normal butane to an isomerate which contains isobutane, involving: (a) isomerisation of the initial material under isomerisation conditions, involving presence of isomerisation catalyst, until an output isomerisation stream is obtained, containing normal butane, but with less concentration than in the initial isomerisation material; (b) distillation of at least part of the output isomerisation stream until a low-boiling fraction is obtained, containing isobutane and light paraffins, where at least 80 wt % of the low-boiling fraction is isobutane, and a high-boiling fraction, containing normal butane and at least 10 wt % isobutane; (c) bringing at least part of the fraction containing normal butane from stage (b) into contact with medium at the retentate side of a permeation-selective membrane, with efficiency index of flow of C4 permeate equal to at least 0.01 and pressure difference between media on both sides of the membrane, which allows for obtaining a retentate fraction containing at least 80 wt % isobutane, and for obtaining a permeate fraction at the permeate side, after passage through the membrane, with high concentration of normal butane; and (d) tapping off retentate fraction from stage (c).

EFFECT: simplification of method.

10 cl, 2 dwg

FIELD: organic synthesis.

SUBSTANCE: invention pertains to obtaining branched alkanes with general formula CnH2n+2, where n = 4-10. CCI4 is gradually added to a mixture of hexane, triethylaluminium - Et3Al and a catalyst - PdCl2, in an argon atmosphere at atmospheric pressure and temperature of 10-60°C for a period of 0.5-2 hours. The molar ratio of hexane: Et3Al : CCl4 : PdCl2 is 75:10:20:0.1.

EFFECT: obtaining of a mixture of branched alkanes with high output.

1 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: method includes: A) bringing flow of raw material in reaction zone of isomerisation with catalyst of isomerisation under conditions of isomerisation, in order to obtain flow, which flows out of isomerisation zone, B) into zone of stabiliser and extraction of stabilised upper flow, which contains one or more C5- hydrocarbons, lower flow, which contains at least 85 wt % of one or more C6+ hydrocarbons, and side fraction, which contains at least 85 wt % of one or more C5+ hydrocarbons. Then C) passing at least part of side fraction in evaporating zone; and D) supply of lower flow of evaporating column, which contains at least 90 wt % of one or more C5+ hydrocarbons, into zone of separating C5 and passing of flow from zone of separation of hydrocarbons C5 in reaction zone of isomerisation.

EFFECT: method demands lower engineering provision for recirculation of C5 stream.

10 cl, 5 tbl, 1 dwg

FIELD: oil-and-gas industry.

SUBSTANCE: invention relates to isomerisation of hydrocarbon flow rich in C4 and/or at least one of C5 and C6. Proposed plant comprises: first and second dehydrator adapted for intake of fluid including at least one reagent. Note here that said first dehydrator can operate in one reagent-fluid drying first mode. Second dehydrator can operate in second mode for recovery with the help of regenerating agent. Reaction zone is communicated with first dehydrator to receive fluid containing at least one reagent and with second dehydrator to receive regenerating agent. Note also that regenerating agent flows through fluid restrictor for adjustment of regenerating fluid flow rate to reaction zone. First pipeline feeds fluid bearing fluid rich on C4 and/or one of C5 and C6 from first dehydrator into reaction zone. Second pipeline communicates second dehydrator with reaction zone. Note here that said fluid restrictor comprises orifice or control valve connected with at least first or second pipeline. Besides, this invention relates to dehydrator recovery.

EFFECT: invention decreases undesirable effect of the gas dehydrator recovery that helps to keep the devices work properly.

6 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of isomerisation of light gasoline fractions, which consists of the preparation of straight-run and secondary gasoline fractions for isomerisation, with the further separation of raw isopentane in the first rectification column - deisopentaniser, after that, its supply to isomerisation in an isomerisation reactor with further release of gases and reflux in the second rectification column - debutaniser, from the bottom of which a stable isomerisate is supplied successively for the separation into the third rectification column for the separate extraction of isopentane and pentane and to the fourth rectification column for the separate extraction of isohexanes and hexane, side runs of the third and fourth rectification columns, containing respectively, pentane and hexane are recirculated for isomerisation into the isomerisation reactor. As a raw material used are straight-run and secondary gasoline fractions 40÷75…85°C, preparation and supply to isomerisation of the straight-run gasoline fraction 40÷75…85°C is carried out separately from the gasoline fraction 40÷75…85°C of the secondary processes of oil refining, with the gasoline fraction 40÷75…85°C of the secondary processes being supplied into the second or third rectification column.

EFFECT: application of the claimed method makes it possible to increase resources of the isomerisation process raw material due to the involvement into the process of the gasoline fraction of the secondary processes, output of target isohexanes, octane number of the isomerisate and isopentane fraction mixture and resources of high-octane semiproducts for compounding commercial gasoline.

5 cl, 3 tbl, 3 dwg

FIELD: chemistry.

SUBSTANCE: device contains the first drier and the second drier, adapted for the reception of a gaseous flowing medium, containing, at least, one reagent. The first drier is made with a possibility of functioning in the first mode of drying the flowing medium, which contains, at last, one reagent, and the second drier is made with a possibility of functioning in the second mode, under conditions of carrying out regeneration by means of a regenerating agent. it also contains a reaction zone, connected by means of the first pipeline to the first drier for the reception of the gaseous flowing medium, which contains, at least, one reagent; and a system of replacement of a regenerating agent in the direction from top to bottom, adapted for the supply and regulation of consumption or reduction of pressure of a part of the said gaseous flowing medium into the second drier, removal of the replaced regenerating agent from the second drier and technological operations, which are performed downstream, to minimise disturbances in the implementation of the said operations.

EFFECT: application of the claimed invention makes it possible to minimise disturbances in carrying out operations downstream.

10 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to a family of aluminosilicate zeolites, a method of producing zeolites and a method of converting hydrocarbons. Described is a novel family of microporous crystalline aluminosilicate zeolites, having a space frame of at least tetrahedral AlO2 and SiO2 units, wherein the empirical composition of the zeolite in anhydrous state is expressed by the following formula: Mm+Rr+Al1xExSiyOz, where M is sodium or a combination of potassium and sodium cations capable of exchange, m is the molar ratio of M to (Al+E) and varies from 0.05 to 2, R denotes a single-charge propyl trimethylammonium cation, r is the molar ratio of R to (Al+E) and varies from 0.25 to 3.0, and E is an element selected from a group consisting of gallium, iron, boron and mixtures thereof, x is the molar fraction or H and varies from 0 to 1.0, y is the molar ratio of Si to (Al+E) and varies from more than 8 to 40, and z is the molar ratio of O to (Al+E) and has a value defined by the equation: z=(m+r+3+4y)/2.

EFFECT: said zeolites are characterised by a unique X-ray diffraction pattern and composition, and have catalytic activity for carrying out various hydrocarbon conversion processes.

10 cl, 5 tbl, 4 ex

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