RU2486943C1 - Method of neon-helium mix enrichment and unit to this end - Google Patents

Abstract

FIELD: process engineering.

SUBSTANCE: invention relates to production of inert gases. In compliance with this method, green neon-helium mix is directed to adsorber unit. Adsorbents are filled with sorbent that absorbs nitrogen selectively. Downstream of one of adsorbers, produced neon-helium mix is fed into collector and, further, is forced by diaphragm-type compressor into cylinders of filling stage. At the same time, second adsorber undergoes regeneration at decreased pressure. Residual gas composed of, mainly, nitrogen with admixtures of neon and helium, is released into atmosphere. In adsorber regeneration, portion or produced mix is forced through said adsorber via gaged nozzle from clean end. After saturation of first adsorber with nitrogen, flow of green neon-helium mix is switched to regenerated adsorber. Proposed unit comprises two adsorbers, receiver at initial mix flow, product collector at adsorbers outlets, filling stage with cylinders, flow meter, gates, switch valves, control actuators for switching the valves by special cycle pattern, and connection pipes.

EFFECT: efficient separation of nitrogen, enriched neon-helium mix with low nitrogen content.

11 cl, 2 dwg

Description

The invention relates to technological processes for producing inert gases and can be used to obtain an enriched neonogel mixture from a stream of crude neonogel mixture, including that taken from air separation plants (ASUs).

As you know, a crude neonogel mixture is obtained in the ASU by partially liquefying a gaseous stream taken from the upper part of the latter along the capacitors, in a special built-in device (concentrator or reflux condenser) and removing the mixture enriched in neon from the upper part of this device [Catalog "Cryogenic equipment" , Tsintihimneftemash, M., 1988].

The crude neon-helium mixture thus obtained contains up to 60% nitrogen, about 2% hydrogen, the rest is neon + helium in the air ratio (3 parts of neon per 1 part of helium). Therefore, the main task of the primary processing of the crude neonogel mixture is its enrichment in neon and helium by removing most of the nitrogen. In this case, hydrogen is either removed at this stage, or this operation is postponed to the stage of final processing of the neon-helium mixture before its separation into pure neon and helium. The second option is preferred for economic reasons, because usually carried out at a centralized enterprise, equipped with modern means of analytical control.

A known method of pre-cleaning the crude neonogel mixture from nitrogen, including the primary cooling of the crude neonogel mixture and the primary separation of part of nitrogen in the form of a liquid, while after the primary separation of nitrogen, the raw mixture is first compressed to 20-150 atm, then further cooled to 77.4-80 K, and the condensate formed is fed into the initially cooled initial gas mixture [RU 2211415, F25J 3/08, 08/27/2003].

The disadvantages of this method include increased energy costs associated with compressing the mixture to high pressure, as well as the need to select liquid nitrogen from the ASU to ensure cryogenic temperatures in the enrichment apparatus.

There is also known a method that includes two-stage refluxing with liquid nitrogen boiling at atmospheric pressure and under vacuum, throttling the enriched mixture using cold choke effect for final reflux, the reflux is purified from neon by evaporation, the neonogel mixture is separated by distillation before each reflux, the enriched mixture after throttling separated, and the gas phase is used as the final product [RU 2006763 C3, F25J 3/00, B01D 53/02, F25J / 08, 01/30/1994].

The disadvantages of this method also include increased energy costs associated with the selection of liquid nitrogen from the ASU to ensure cryogenic temperatures (about 78-80 K) in the mixture enrichment apparatus.

There is also a method of enrichment of a crude neonogel mixture, in which the reflux condenser is combined with an adsorber in one apparatus, which allows for almost complete purification of the mixture from nitrogen [G. Golovko Cryogenic inert gas production. - L .: Engineering, 1983, p. 314].

The disadvantages of this method include both the aforementioned increased energy costs due to the need to maintain cryogenic temperatures in the apparatus, and the excessive complexity in the manufacture of the apparatus type reflux condenser-adsorber high performance, which is why this technical solution was found to be ineffective in the case of binding the device to modern ASU of great productivity [Ibid., P. 315].

There is also known a method of enriching a neonogel mixture [US 5100446 A1, F25J 3/04, 03/31/1992], including 4 stages:

Stage 1 - the introduction of an air source mixture containing neon into the ASU unit and obtaining, using the low-temperature distillation method, a first neon-containing stream having a nitrogen concentration that exceeds its content in the air source mixture and the concentration of neon in it exceeds its content in air initial mixture;

Stage 2 - passing the first non-containing stream from the ASU through the neon column and receiving a second non-containing stream in it having a nitrogen concentration that is lower than its content in the first non-containing stream and having a neon concentration that exceeds its content in the first non-containing stream;

Stage 3 - passing a second non-containing stream through an adsorption layer, which preferably absorbs nitrogen, to obtain a production neon having a neon concentration that exceeds its content in the second non-containing stream; and

Stage 4 - desorption of the adsorption layer at a pressure below the pressure at which the previous adsorption stage is carried out in it, and the direction of the waste gas resulting from the desorption to the ASU unit. In addition, between step 2 and step 3, a sub-step for removing hydrogen from the mixture is introduced by introducing oxygen into the stream, followed by its catalytic binding in the reactor and removing the burning product (water) on a separate sorbent layer.

The disadvantage of this technical solution regarding the method is the excessive complexity of the technological scheme at the stage of preliminary processing of the crude neonogel mixture, which produces only an intermediate product, intended in the future for final separation into pure products. This complication consists in introducing an additional distillation column for washing neon into the ASU technological scheme, which, in turn, leads to an increase in potential losses of neon with waste gas at the desorption stage in adsorbers, since the initial mixture at their inlet has an increased (almost 2 , 5 times), in comparison with the usual crude neonogel mixture, the content of neon. Therefore, to reduce these losses, it is necessary to direct this waste gas back to the ASU, and since the pressure of the waste gas at the desorption stage is very low (usually lower than atmospheric), a vacuum pump must be installed on the waste stream, the discharge pressure of which must also exceed the pressure in the column high pressure switchgear, which leads to significant additional capital and operating costs. In addition, the direct connection of rapidly switching adsorbers of the enrichment unit with the exit from the neon column inevitably leads to pressure fluctuations in the latter and instability in the operation of its upper part.

A serious drawback of this technical solution is the fact that it does not provide for the processing of crude neon-helium mixture from currently operating ASUs, which, for the most part, do not have an additional neon column.

The closest in technical essence is the method of enrichment of a gas containing adsorbable impurities [US 6315818, Al, F25J 3/04, 11/13/2001], in which the enrichment is carried out by short-cycle adsorption without heating (CCA) using several adsorbers, while the adsorbers are connected a single cyclogram and each adsorber goes through a cycle containing operational phases that are sequentially carried out in each of the adsorbers with a time offset of 1 / n of the duration of the cycle T, where n = 3, 4 ... the number of adsorbers wherein each complete technological cycle comprises the inlet of unrefined gas into the adsorber through the first end of the adsorber with the circulation of the above-enriched gas in the adsorber and the simultaneous removal of enriched gas through the other end of the adsorber, as well as the subsequent regeneration of the adsorber, the aforementioned phase of regeneration starting with a single-stage countercurrent pressure reduction by equalizing the pressure with another adsorber, which is at this time in the phase of increasing pressure. A distinctive feature of this method is the completion of the regeneration phase with a phase during which the residual (in the adsorber) gas partially joins the flow of the dirty mixture at the inlet of the installation, and the rest of it is a purge.

The disadvantages of the closest technical solutions in relation to the method are the relatively narrow scope of its application, due to the fact that it can be used to obtain a pure product under the conditions of one well-sorbing component (nitrogen) with a relatively low content in the initial mixture (3 ... 10 times lower than at the output of the ASU), a relatively complex scheme of the device implementing the method, in which 3 or more adsorption apparatuses are used, and providing an increased (up to 30 bar) mixture pressure at the inlet hell orbera.

This narrows the scope of the known method in solving other technical problems, in particular, if it is necessary to obtain only an intermediate product at the place of operation of the ASU, intended for subsequent final purification from hydrogen, deeper purification from nitrogen and separation into production neon and helium at a specialized enterprise.

The closest technical solution in relation to the method has a relatively high demand for energy consumption, since, as mentioned above, the method requires a sufficiently high pressure of the initial mixture at the inlet to the installation, which makes it necessary to introduce a high pressure compressor into its installations, and this is not only leads to increased energy costs, but also does not allow rational use of the available flow pressure of the crude neonogel mixture, removed from the ASU.

The required technical result regarding the method is to expand the scope and reduce the requirements for the amount of energy consumption during its implementation.

The required technical result is achieved by the fact that according to the method according to which the enrichment of the initial gas mixture, which is used as a raw neonogel mixture, taken from an air separation unit (ASU), for its purification from nitrogen, is carried out by short-cycle non-heating adsorption (CCA) using several adsorbers, while the adsorbers are connected by a single cyclogram and each adsorber goes through a complete cycle containing operational phases, which are successively carried out in each of the adsorbers with about a time shift of 1 / n from the duration of the cycle T, where n is the number of adsorbers, and the full cycle includes the inlet of the non-enriched gas into the adsorber through the inlet end of the adsorber with the circulation of the above-enriched gas through the adsorber from the inlet end to the outlet end and by simultaneous removal through the outlet end of the adsorber of the enriched gas, as well as the subsequent regeneration of the adsorber, two adsorbers are used, while the intake of raw gas into the adsorbers is carried out from an air separation unit at the technological pressure formed by it with additional equalization of pressure fluctuations, the enriched gas is discharged through the outlet end of the adsorber into cylinders with preliminary enrichment gas collection, and the subsequent adsorber regeneration is performed by dumping the residual gas into the atmosphere and supplying part of the enriched gas from the other adsorber through the outlet end at the same time, the gas mixture is additionally transferred from the spent adsorber to the regenerated adsorber.

In addition, the desired technical result is achieved in that the amount of enriched gas directed to the adsorber, which is at the stage of regeneration, from another adsorber, is from 5 to 20% of the enriched gas discharged from the adsorber.

In addition, the required technical result is achieved by the fact that the transfer of the gas mixture from the spent adsorber to the adsorber that has passed regeneration is carried out from both ends of the adsorbers, and the bypass operation from the output end begins earlier than the bypass operation from the input end.

In addition, the required technical result is achieved in that the concentration of neon + helium in the initial gas mixture is from 30 to 50%.

In addition, the desired technical result is achieved in that the cycle time is from 2 to 6 minutes.

Also known are devices for enriching a crude neonogel mixture.

One of the known devices consists of two stages of separation. The first stage contains a heat exchanger connected in series, a condenser and a liquid separator located in the nitrogen bath, and is connected by an inlet to an air separation unit and an outlet to a compressor inlet. The compressor is located on the product exit line. The heat exchanger is placed in a nitrogen bath. An additional separation stage includes a heat exchanger, a condenser, a liquid separator and a throttle located in a nitrogen bath and is connected by an input to the compressor output and an output to the product output line. The lower part of the liquid separator of the additional separation stage is connected through the throttle to the upper part of the liquid separator, and a small capacitor is installed between the throttle and the upper part of the liquid separator [RU 2211415, F25J 3/08, 08/27/2003].

The disadvantage of this device is the need to work at a cryogenic temperature level and the associated increased capital (caused primarily by the need for expensive thermal insulation) and operating costs.

Another device is also known, which includes a cube with a coil integrated in it, additional rectification sections, 3 reflux condensers, a throttle valve, a separator, a liquid nitrogen supply pipe with a control valve and a heat exchanger. At the same time, the device is structurally a separator, a heat exchanger and a vertical apparatus interconnected by pipelines, consisting of three reflux condensers with distillation sections between them and a cube with a coil built into it [RU 2006763 C1, F25J 3/04, F25J 3/02, F25J 3 / 08, 01/30/1994].

The disadvantage of this device is also the increased energy costs associated with the cryogenic level of temperatures at which it is operated.

It is also known a device for producing an enriched neonogel mixture from a crude mixture taken from the upper part of the ASU capacitors, containing at least one neon column integrated in the ASU unit with a lower evaporator and an upper condenser, from which the raw mixture, heater, and catalytic reactor are selected oxidation of hydrogen with a device for supplying oxygen to it, a cooler, a separator for separating the water formed as a result of catalysis, a block of adsorbers from several devices filled with a two-layer sorbent, The first part of the sorbent along the flow is activated carbon, and the second is zeolite (a two-layer sorbent is intended not only to remove most of the nitrogen from the initial mixture, but also to remove residues of the above moisture and oxygen, since the hydrogen bonding reaction proceeds with an excess of oxygen against stoichiometric equilibrium) and a vacuum pump to return the desorbate to the entrance to the ASU [US 5100446 A1, F25J 3/04, 03/31/1992].

The disadvantage of this technical solution is the relatively narrow functionality, since although it allows you to get the enriched neonogel mixture from the raw mixture taken from the ASU, it is not intended to process the mixture with a low neon content, which is usually removed from the currently operating ASU without additional neon columns.

In addition, the presence in the circuit of a vacuum pump of high power (since it is necessary to overcome the resistance of the high pressure switchgear of the ASG along the discharge line) significantly complicates the circuit of the device, and also reduces its efficiency and increases energy consumption.

In addition, the direct connection of rapidly switching adsorbers, the working cycle of which is from one to several minutes, directly to the exit from the ASU should lead to pressure fluctuations in the node for receiving the crude neon-helium mixture of the ASU and worsen its performance.

The closest in technical essence to the proposed device for producing an enriched mixture from a crude neon-helium mixture according to the method proposed above is a device for purifying a gas mixture using CCA adsorption, including 3 or more adsorbers switching according to a special cyclogram, a compressor for compressing the initial mixture to pressure of the order of 30 bar, the supply pipe of the initial mixture, the product pipeline, the pipeline for supplying the residual gas to the line of the initial mixture in front of the compressor on which the buffer is located Single vessel residual gas purge line with discharge into the atmosphere, and a system of switching valves by operating the control device. In addition, the device has a reservoir into which part of the product from the adsorbers is collected and which is designed to fill the adsorbers with it in the last regeneration phase [US 6315818 A1, F25J 3/04, 11/13/2001].

The disadvantages of the closest technical solutions include the relatively high energy costs caused by the need to use a compressor at the entrance to the installation, which reduces the efficiency of the device.

In addition, this technical solution has relatively narrow functional capabilities, since it does not directly enrich the crude neonogel mixture, which can be taken from the ASU, where it is formed at the outlet under pressure (5-6 bar), and the inclusion of an additional compressor results in indicated above, to increase energy costs.

In addition, the scheme is excessively complicated by the number of adsorption apparatus included in it (3-4 adsorbers), and the location of the tank on the product exit line is extremely unsuccessful, because with its help, only one problem is solved - filling the adsorber product in the last phase of preparation for the adsorption stage, and the problem of smoothing the pressure fluctuations in the production line is not solved, which is very important when a compressor is included in the circuit to compress the product into cylinders.

The required technical result is to expand the functionality by ensuring the feasibility of the enrichment process of the raw neonogel mixture from the ASU and increasing the efficiency.

The required technical result is achieved by the fact that in the installation for implementing the proposed method of enrichment of the neonogel mixture containing the first and second adsorbers with the sorbent placed in them, and working according to the CCA method, which are connected by a single cyclogram, and each adsorber goes through a cycle containing operational phases that sequentially carried out in each of the adsorbers with a time offset of 1/2 from the duration of the cycle T, while the full process cycle contains an inlet of unenriched gas into the adsor ep through the inlet end of the adsorber with the circulation of the aforementioned raw gas in the adsorber from the inlet end to the outlet end and simultaneously exhausting the enriched gas through the outlet end of the adsorber, as well as the subsequent regeneration of the adsorber and filling the adsorber with the initial mixture, a receiver, a collection of enriched neonogel mixture, and a compressor for compression are introduced enriched neon-helium mixture, filling ramp with cylinders, flow meter, first to eighth switching valves, command and actuating device for switching valves and control valves from first to third, the first of which is made in the form of a calibrated nozzle, and the filling ramp with cylinders through the second valve is connected by a pipeline to the compressor outlet for compressing the enriched neonogel mixture, the inlet of which is connected by a pipeline to the outlet of the enriched neonogel mixture collection, and the input of the collector through the eighth switching valve is connected by a pipeline to the outputs of the third and fourth switching valves, the inputs of which are connected by pipelines to the output the ends of the first and second adsorbers, respectively, while the output ends of the first and second adsorbers are connected by a pipeline through the first control valve, the receiver inlet is connected by a pipe through a flow meter and the second valve to the pipeline supplying the initial neonogel mixture to the unit, and the receiver output through the seventh valve switch is connected by a pipeline to the inputs of the first and second switching valves, the outputs of which are connected by pipelines to the input ends, respectively, of the first and second of adsorbers, the adsorbers are connected to the input ends of the pipelines to the outputs, respectively, fifth and sixth switching valves whose inputs are connected via a common conduit to a gas discharge line to the atmosphere.

In addition, the required technical result is achieved by the fact that NaX zeolite, or CaA zeolite, or activated carbon is used as a nitrogen-containing sorbent in adsorbers.

In addition, the required technical result is achieved by the fact that a high-pressure compressor of the membrane type is used as a compressor.

In addition, the required technical result is achieved by the fact that for the implementation of cycles containing the operational phases, the first and second adsorbers are switched alternately by a command-executive device, while when one of them is at the adsorption stage, the other undergoes regeneration.

In addition, the required technical result is achieved by the fact that the volumes of the receiver and the collection of the enriched neonogel mixture correspond to the flow rate of the initial neonogel mixture and the compressor productivity and make up from 5 to 15% of their hourly values.

In addition, the required technical result is achieved in that the flow cross section of the calibrated nozzle is calculated depending on the volume of the adsorbers and the pressure drop between them so that the amount of enriched neonogel mixture passing through it is 5-20% of the amount of enriched neonogel mixture sent to a collection of enriched neonogel mixture.

Figure 1 - Functional diagram of the installation for implementing the proposed method of enrichment of the neonogel mixture.

Figure 2 - The sequence of switching valves of the adsorber assembly.

Installation for implementing the proposed method of enrichment of the neonogel mixture contains first 1 and second 2 adsorbers operating on the CCA cycle, nitrogen-containing sorbent 1a, placed in adsorber 1, nitrogen-containing sorbent 2a, placed in adsorber 2, receiver 3 at the input of the initial mixture into the installation, product collector 4 at the outlet of the installation, a flow meter 7 for supplying the initial mixture to the receiver 3, a membrane compressor 5 for compressing the resulting product and delivering it to the cylinders of the filling ramp 6, forced switching valves from first to the 8th octal ... 15 and three control valves from the first to the third 16 ... 18, one of which (the first control valve 16) is a calibrated double-acting nozzle.

In the installation for implementing the proposed method, the filling ramp 6 through the third valve 18 is connected by a pipeline to the outlet of the membrane compressor 5, the input of which is connected by a pipe to the output of the product collector 4, and the input of the product collector 4 is connected by a pipe to the output of the eighth switching valve 15, the input of which is connected to the outputs the third and fourth switching valves 10, 11 located at the output end of the adsorber assembly. The input ends of the third and fourth switching valves 10, 11 are connected by pipelines to the output ends of the adsorbers, respectively, 1 and 2, while the output ends of the adsorbers 1 and 2 are also connected to each other through the first valve 16.

The output of the receiver 3 is connected by a pipeline through the seventh switching valve 14 with the inputs of the first and second switching valves 8, 9, the outputs of which are connected to the inputs of the adsorbers, respectively, 1 and 2, and the input of the receiver 3 is connected by a pipeline through the flowmeter 7 and the second valve 17 with the feed input the initial mixture in the installation.

The outputs from the fifth and sixth switching valves 12, 13 located at the inlet end of the adsorber assembly are connected by a pipeline to the outlet of the waste (purge) gas into the atmosphere, and the inputs of these switching valves are connected to the inputs to the adsorbers, respectively, 1 and 2.

Switching the valves from the first to the eighth (pos. 8-15 in FIG. 1) is performed by force using a command-executive device (not shown in the diagram).

The proposed method for producing enriched neonogel mixture from the crude mixture is implemented in the proposed installation as follows.

The initial mixture from the ASU under a pressure of 5-6 ata through the valve 17 is fed into the receiver 3, from which it is sent for cleaning to one of the alternately working adsorbers (for example, to 1). Receiver 3 serves as a buffer tank for smoothing pressure drops when switching adsorbers. The flow rate of the feed mixture is controlled using a flow meter 7. On the nozzle 1a of the adsorber 1, selective absorption of nitrogen from the crude neonogel mixture occurs, and at the outlet of the adsorber, the nitrogen concentration in the product decreases from 50-60 vol.% To 3-5 vol.% . At the same time, the content of neon and helium in the product increases accordingly.

Having passed the adsorber, the production mixture is collected in a collection vessel 4, from where it is compressed using a membrane compressor 5 to a pressure of 200 bar and sent to the cylinders of the ramp 6.

Consider the cycle on the example of adsorber 1. After the adsorption stage (phase a in Figure 2) is completed, the sorbent regeneration stages are carried out in it: pressure equalization in the adsorbers with the discharge of gas into the neighboring adsorber, which is carried out both on a clean (output) and along the dirty (inlet) ends (phases b, c, d), reducing the pressure to the minimum with discharge of the desorbate (residual gas) into the atmosphere and supplying to the adsorber from the clean end of the purified product from the neighboring adsorber through nozzle 16 (phases e, f, g, h) alignment pressure in adsorbers with the reception of gas from a neighboring adsorber, which is carried out both at the clean (outlet) and dirty (inlet) ends (phases i, j, k), increasing the pressure to the maximum by supplying gas from both clean and from the dirty end (phases l, m, n), and the valve opening phase (m) from the clean end is 1 time interval ahead of the valve opening phase (n) from the dirty end. After that, the cycle repeats.

The adsorber 2 passes through the same phases only with a half-cycle shift of t half = Tc / 2.

The claimed method for producing enriched neonogel mixture can be implemented on the installation, schematically shown in figure 1, and containing two parallel-connected adsorbers 1 and 2, connected to a single technological scheme using control valves, calibrated nozzles, switching valves and pipelines, as well as including the receiver in the stream of the initial mixture 3, the collection of the production mixture 4, the compressor 5 and the filling ramp 6 with cylinders.

The installation has connections with an air separation device (ASU) to obtain from it the required amount of the initial crude neonogel mixture. The installation is equipped with the necessary instrumentation, including a flowmeter 7 and a command-executive device (not shown in the diagram) for switching valves 8-15 in accordance with a given sequence diagram.

As a result, it is possible to obtain an enriched neonogel mixture from a crude mixture taken from the ASU at ambient temperature without involving cryogenic liquids to cool the working apparatus. The supply of a part of the product to the adsorber, which is at the stage of regeneration, allows to increase the purity of the obtained product, and the inclusion of the receiver in the flow diagram of the installation of the source mixture from the ASU allows to reduce the pressure fluctuations associated with the switching of the adsorbers, which have a negative impact on the stability of the operation of the selection unit the original mixture from the ASU.

Thus, thanks to improvements in the known methods and devices, the required technical result is achieved, which regarding the method is to expand the scope and reduce the requirements for the amount of energy consumption during its implementation, and regarding the device - to expand the functionality by ensuring the feasibility of the enrichment process of the raw neonogel mixture from the ASU and increasing profitability.

Claims (11)

1. A method of enrichment of a neonogel mixture, according to which the enrichment of the initial gas mixture, which is used as a raw neonogel mixture, taken from an air separation unit (ASU), for its purification from nitrogen, is carried out by means of short-cycle non-heating adsorption (CCA) using several adsorbers, In this case, the adsorbers are connected by a single cyclogram and each adsorber goes through a complete cycle containing operational phases, which are successively carried out in each of the adsorbers with a time offset of and the value 1 / n of the duration of the cycle T, where n is the number of adsorbers, and the full cycle includes the intake of unrefined gas into the adsorber through the inlet end of the adsorber with the circulation of the above-enriched gas through the adsorber from the inlet end to the outlet end and simultaneous discharge through the outlet the end of the enriched gas adsorber, as well as the subsequent regeneration of the adsorber, characterized in that two adsorbers are used, while the admission of unenriched gas into the adsorbers is carried out from an air separation unit at The process pressure adjusted by it with additional equalization of pressure fluctuations, the enriched gas is discharged through the outlet end of the adsorber into cylinders with preliminary enrichment gas collection, and the subsequent adsorber regeneration is carried out by dumping the residual gas into the atmosphere and supplying part of the enriched gas from the other adsorber through the outlet end at the same time, the gas mixture is additionally transferred from the spent adsorber to the regenerated adsorber. 2. The method according to claim 1, characterized in that the amount of enriched gas sent to the adsorber located in the regeneration step from another adsorber is from 5 to 20% of the amount of enriched gas discharged from the adsorber. 3. The method according to claim 1, characterized in that the transfer of the gas mixture from the spent adsorber to the adsorber, which has passed regeneration, is carried out from both ends of the adsorbers, and the bypass operation from the output end begins earlier than the bypass operation from the input end. 4. The method according to claim 1, characterized in that the concentration of neon-helium in the initial gas mixture is from 30 to 50%. 5. The method according to claim 1, characterized in that the cycle time is from 2 to 6 minutes 6. Installation for implementing the method of enrichment of the neonogel mixture according to claim 1, containing the first and second adsorbers with an adsorbent placed in them, working by the CCA method, which are connected by a single cyclogram, and each adsorber goes through a cycle containing operational phases that are carried out sequentially in each of adsorbers with a time offset of 1/2 by the duration of the cycle T, the full technological cycle containing an inlet of non-enriched gas into the adsorber through the inlet end of the adsorber with the circulation of the aforementioned the enriched gas in the adsorber from the inlet end to the outlet end and simultaneously exhausting the enriched gas through the outlet end of the adsorber, as well as subsequent regeneration of the adsorber and filling the adsorber with the initial mixture, characterized in that a receiver, an enriched neon-gel mixture collector, and a compressor for compressing the enriched neon-gel mixture are introduced, filling ramp with cylinders, flow meter, first to eighth switching valves, command and control device for switching valves and control valves from the first the third, the first of which is made in the form of a calibrated nozzle, the filling ramp with cylinders through the second valve connected by a pipeline to the compressor outlet for compressing the enriched neonogel mixture, the inlet of which is connected by a pipe to the outlet of the enriched neonogel mixture, and the collector inlet through the eighth valve switch is connected by a pipeline to the outputs of the third and fourth switching valves, the inputs of which are connected by pipelines to the output ends of the first and second absorbers, while the output ends of the first and second adsorbers are connected by a pipeline through the first control valve, the receiver inlet is connected by a pipeline through a flowmeter and the second valve to the pipeline supplying the initial neon-helium mixture to the installation, and the receiver's output through the seventh switching valve is connected by a pipeline to the inputs of the first and second switching valves, the outputs of which are connected by pipelines to the input ends of the first and second adsorbers, respectively, the input ends of the adsorbers are connected They are connected by pipelines with exits of the fifth and sixth switching valves, respectively, whose inlets are connected through a common pipeline to the gas discharge line into the atmosphere. 7. Installation according to claim 6, characterized in that as a nitrogen-containing sorbent in the adsorbers, NaX zeolite, or CaA zeolite, or activated carbon is used. 8. Installation according to claim 6, characterized in that the membrane type high-pressure compressor is used as a compressor. 9. The installation according to claim 6, characterized in that for the implementation of cycles containing the operational phases, the first and second adsorbers are switched alternately by a command-and-control device, while when one of them is at the adsorption stage, the other undergoes regeneration. 10. The installation according to claim 6, characterized in that the volumes of the receiver and the collection of the enriched neonogel mixture correspond to the flow rate of the initial neonogel mixture and the compressor capacity and range from 5 to 15% of their hourly values. 11. The installation according to claim 6, characterized in that the flow cross section of the calibrated nozzle is calculated depending on the volume of the adsorbers and the pressure drop between them so that the amount of enriched neonogel mixture passing through it is 5-20% of the amount of enriched neonogel mixture, sent to the collection of enriched neonogel mixture.

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