UA65356A - Apparatus for ammonia production - Google Patents

Abstract

Apparatus for ammonia production includes connected in sequence by a pipeline system compartments for sulfur purification, reforming, vapor formation, conversion of carbon oxide, mono-ethanolamine purification, methanization, compression with steam turbine and technological air compressor for reforming, air condensers for the worked-out steam of the turbine and the turbo-compressor cooling unit, section of synthesis with two evaporators for cooling the recirculation gas at the site of secondary condensation, one of those is included to the circuit of operation of two absorption-cooling units of the generator-rectifier with refluxer, condenser of the air cooling with receiver, overheater, absorber with a receiver, pump for feeding condensed solution, solution heat exchanger. The unit is equipped with two-cavity steam generator. Additionally there are installed air condensers. .

Description

The invention relates to refrigerating equipment, as well as to plants for the production of ammonia.

A known plant for the production of ammonia, which contains serially connected departments of desulfurization, reforming, steam generation, carbon monoxide conversion, monoethanolamine (MEA) purification, methanation, compression with a steam turbine and a process air compressor for reforming, air condensers of the spent turbine steam, connected in series by a pipeline system. a condensate collector with a pump for returning it to the steam generation department, a synthesis department with two evaporators for cooling the circulating gas in the secondary condensation section to a temperature (-5"С), one of which is included in the operation scheme of the water-ammonia absorption refrigeration unit (AHU) with a boiling temperature refrigerant (-10"С), and the second - to the working scheme of the ammonia-refrigerating plant for liquefaction of ammonia (see Kuznetsov L.D., Dmytrenko L.D., Rabina P.D., Sokolinsky Yu.A.

Ammonia synthesis. - Moscow: Chemistry, 1982. - b. 11-16, 0. 155).

The disadvantage of this installation is the increased consumption of electricity to drive the fans of the air condensers for cooling the spent steam of the turbine drive of the process air compressor. At the same time, the low potential heat of the spent steam with a pressure of 0.04MPa, a temperature of up to 90"C and a consumption of up to 54.5t/h, which is about ZOGcal/h, is irreversibly lost.

A known unit with a condensing column, a circulation line with a mixture of gas with ammonia vapors, absorption refrigerating units, a turbocompressor refrigerating unit, equipped with air cooling condensers and evaporators with liquid refrigerant supply lines and refrigerant vapor discharge lines | see AS USSR Mo 1002756 IPC R25815/04, publ. Bull. Me9 dated 07.03.83.

The disadvantage of this unit is the impossibility of turning off the turbo-compressor refrigerating unit in the spring-summer period, when the temperature of the atmospheric air is high, which leads to an increase in the cost of electricity for the production of cold.

The closest in terms of technical essence and achievable effect is an ammonia production facility, which consists of sequentially connected departments of sulfur removal, reforming, steam generation, carbon monoxide conversion, MEA purification, methanation, compression with a steam turbine and a process air compressor for reforming connected by a pipeline system, air condensers of spent turbine steam, a condensate collector and a pump for returning it to the steam generation department, the synthesis department with two evaporators for cooling the circulating gas in the secondary condensation section to a temperature (-5"C), one of which is included in the operation scheme of the ammonia turbocompressor refrigeration plant ( ATK) with a design refrigerating capacity of 4.2Gcal/h with an air condenser for condensing the refrigerant compressed by the ATK compressor, and the second - to the scheme of operation of two AHUs with a design refrigerating capacity of 5.4Gcal/h, containing a rectifier generator with a dephlegmator, an air cooling condenser from the resa verom, a subcooler, an absorber with a receiver, a pump for supplying a strong solution and a solution heat exchanger (see Permanent technological regulations of the ammonia workshop 1-B., Mo. 114. - Severodonetsk: PO "Azot", 1985. - 722 p.|.

Disadvantages of this installation include: high energy costs for obtaining cold with the help of ATK, the consumption of electricity to drive the compressor is 4,000 kWh; increased electricity consumption for cooling the spent turbine steam of the process air compressor in the air condensers, in which three fans are used, consuming 972 kWh of electricity; a decrease in the cooling capacity of the AHU in operating conditions at elevated ambient air temperatures, which is associated with the use of air condensers and cooling of the absorber with water coming from cooling towers. At the same time, an increase in the atmospheric air temperature (especially in the summer) above 25"C leads to an increase in condensation pressure, absorption, a decrease in the cooling capacity of the AHU, and, therefore, an increase in the temperature of the circulating gas cooling above the design temperature by an average of 5"C. As you know, see Babichenko A.K., Efimov V.T. The influence of temperatures of secondary condensation on the economic indicators of work! high-capacity ammonia synthesis units. //

Questions of chemistry and chemistry. technologies. - 1986. - Ex. 80. - P. 113-117), this leads to an increase in the consumption coefficients for natural gas and desalinated water, respectively (for a temperature of 1"C) by 3.85 nm3/t.Mnh and 36.8 kg/t.Mnh. For spring- in the summer period (5 months) with a unit productivity of 1,360 tons/day, overconsumption of natural gas is about 800,000 cubic meters, and water consumption is about 8,000 tons. In addition, the work of the ATK leaves much to be desired. It often breaks down, which requires the availability of a backup ATC for the normal operation of the unit as a whole. And this is connected with an increase in the time of repair work, both during the period of operation and during the period of annual shutdown repair of the unit.

The objective of the present invention is to increase the cooling capacity of absorption refrigeration units and reduce energy consumption at the secondary condensation section of ammonia production.

To solve the problem in a well-known plant for the production of ammonia, which contains successively connected departments of desulfurization, reforming, steam generation, carbon monoxide conversion, monoethanolamine purification, methanation, compression with a steam turbine and a process air compressor for reforming, air condensers of spent steam connected by a pipeline system a turbine, a condensate collector and a pump for returning it to the vaporization department, the synthesis department with two evaporators for cooling the circulating gas in the secondary condensation section, one of which is included in the scheme of operation of two water-ammonia absorption and refrigeration units, each of which contains a generator-rectifier and a dephlegmator, a condenser air cooling with a receiver, a subcooler, an absorber with a receiver, a pump for supplying a strong solution and a solution heat exchanger, according to the invention, the installation is additionally equipped with an ammonia double-chamber steam generator, one of the inputs of which is connected to a pipeline in exhaust steam outlet of the process air compressor turbine for reforming, and one of its outlets for condensed water vapor is connected to the inlet of the condensate supply to the air condenser for subcooling it in this condenser, the second outlet of the double-cavity steam generator along the flow of high-pressure working ammonia vapor is connected pipelines with steam ejectors for compression of evaporated ammonia vapors from the first and second evaporators, ammonia vapors from the dephlegmators of two AHUs, pressing ejector of working ammonia vapors of the AHUs of the second evaporator and entering the ATK air condenser and an additionally installed air condenser, the condensate formed from which is collected in to the condensate collector, from where one of the flows enters as a refrigerant to the first evaporator, mixing partially with the flow of liquid ammonia from the condensers

AHU, and the second stream is supplied by a liquid ammonia pump to the second inlet of the double-cavity steam generator to obtain the working ejection steam. The drawing shows a diagram of an ammonia production plant.

The installation includes the desulphurization department 1, reforming 2, steam generation 3, carbon monoxide conversion 4, monoethanolamine purification 5, methanation 6, compression 7, which contains a steam turbine 8 for driving a process air compressor 9, an air condenser 10 with a water condensate collector 11 and a pump 12 returning it to the vaporization department 3, the ammonia synthesis department 13 with two evaporators 14 and 15 for cooling the circulating gas in the secondary condensation section, the first of which is connected by the injection flow to the ejector 16, air cooling condensers 17 and 18, collector 19 of ammonia condensate, pump 20 and the double-cavity steam generator 21, the inlet of which is connected through the condensate cavity to the pipeline 22 of the spent steam from the steam turbine 8, and the output is to the pipeline 23 for the exit of water condensate for cooling in the air condenser 10, and the second output of the double-cavity steam generator 21 is to the supply pipeline 24 of high-pressure ammonia vapors in steam th ejector 16. The second evaporator 15 is connected to two absorption-refrigeration units 25, containing a generator-rectifier with a dephlegmator 26, a steam ejector 27, an air condenser with a receiver 28, a subcooler 29, a steam ejector 30 of the first stage of vapor compression from the evaporator 15 and direct partly into the absorber 31, and partly into the steam pressure ejector 32 of the second compression stage, the pump 33 for supplying the solid solution from the absorber 31 to the solution heat exchanger 34.

Evaporator 14 through the evaporation cavity is connected at the inlet to the pipeline 35 for the exit of liquid ammonia from the collector 19 of ammonia condensate, and at the output - to the pipeline 36 for the supply of ammonia vapors to the steam ejector 16, the output of which is through condensers 17 and 18 of air cooling, collector 19 of ammonia condensate and pump 20 is connected to the second inlet of the double-cavity steam generator 21, pipeline 38 for partial supply of compressed ammonia vapors in ejectors 27 and 32 to air condensers 17 and 18, pipeline 39 for partial supply of liquid ammonia from subcoolers 29 of two AHUs 25 and pipeline 40 for partial return of ammonia vapors from the first of the evaporator 14 through the subcooler 29 to compression in the ejectors 30 to the absorption pressure.

According to the scheme, the installation process is carried out as follows. Natural gas, for example, with an amount of 35,600 nm3/h at a pressure of 4.4 MPa is mixed with a nitrogen-hydrogen mixture (ABS) with an amount of bbOOnm3/h until the hydrogen content in the mixture is 10.79506. and is fed to the desulfurization department 1. In the desulfurization department 1, in a catalytic reactor on a cobalt-molybdenum catalyst at a temperature of 3907C, sulfur compounds contained in natural gas are hydrogenated to hydrogen sulfide, and then hydrogen sulfide is absorbed on an oxide-zinc absorber until its content is not more than 0.5mg/cm3. The purified gas mixture is mixed with steam, the consumption of which is 132 thousand nm3/h, and enters the reforming unit 2 of the first stage, where the conversion of natural gas with steam obtained in department of steam formation, to a residual methane content in the gas of 119506. After that, the gas enters the second stage of conversion, where at a temperature of 1200 "C, steam-air conversion of methane takes place to a residual methane content of 0395606. The steam consumption for steam-air conversion is 5000O0nmZ/h and is provided by the steam 3. Process air consumption in the amount of 50,400 nmZ/h is provided by compressor 9. The composition of the converted gas after separation of reforming 2 (in terms of dry gas, 9506.) is as follows: СНа-0.3; CO"-13;

NG-57; Meo-22.4; Ag-0.3. Gas consumption after reforming is 185,000 cubic meters per hour (in terms of dry gas).

After the conversion of methane, the gas goes to department 4 for the conversion of carbon monoxide. The conversion takes place in two stages at a temperature of 380"C in the first stage, and at 220"C and a pressure of ZMPa in the second. The composition of the gas after the conversion of carbon monoxide (in terms of dry gas, 9506.) is as follows: СН4А-0.3; bO2-17.3; No-61.6; M2-20; Ag-0.3;

CO-0.5. Consumption of wet gas after conversion of carbon monoxide is 292 thousand nmZ/h (in terms of dry gas - 207 thousand nmZ/h).

The obtained converted gas goes further for purification from carbon dioxide to the monoethanolamine purification department 5, where at a temperature of 40"C and a pressure of 2.8 MPa, carbon dioxide is absorbed by an aqueous solution of MEA to a COg content in the gas of 0.19506. The composition of the gas after purification from COg ( in terms of dry gas, 9006.) the following: СНа-0.4; СО2-0.1; Но-74.5; М2-24.1; Аг-0.3; СО-0.6. Degree of purification of gas from СО2-99,695.

Consumption of purified gas after absorption - 171.3 thousand nmZ/h.

Cleaned from CO: the gas enters the catalytic purification of oxygen-containing compounds to the methanation section b, where at a temperature of 350 "C and a pressure of 2.6 MPa, the oxygen-containing compounds are reduced to methane. After section 6, the nitrogen-hydrogen mixture (ABS) has the following composition (in 9506. ) СНа-1.1; Н2-74; Мо-24.6; Аг-0.3; бОЖСоО" - traces. This АВС with a pressure of 2.5MPa and a temperature of 43"С enters the compression department 7, where it is compressed by a four-stage compressor to pressure of 32 MPa. The compressor is driven by a steam turbine. At the same time, the steam with a pressure of 10 MPa goes straight from the steam generation department 3. The selection steam with a pressure of 4 MPa and a flow rate of 54.5 t/h enters the steam turbine 8 to drive the compressor 9 of the process air. Spent steam after turbine 8 with a pressure of 0.04MPa and a temperature of 80-907C (depending on the season) is divided into two streams.

The first flow in the amount of up to 4.5 t/h enters the air condenser 10, and the second flow through the pipeline 22 in the amount of about 50 t/h goes to the double-vacuum steam generator 21, where it condenses due to the transfer of heat to the liquid ammonia that evaporates at the same time, which enters from the collector 19. The formed water condensate of the second flow from the double-chamber steam generator 21 through the pipeline 23 goes to the condensers 10 for subcooling. From the condenser 10, the first and second streams, which have a temperature of 65"C, are collected in the water condensate collector 11, from where the water pump 12 is used for demineralization of water from oxygen-containing compounds to the steam generation department 3.

After the compression section 7, the high-pressure ABC in the amount of 168,000 nm3/h enters the ammonia synthesis section 13. In the ammonia synthesis column, at a pressure of no more than 32MPa and a temperature of 420-530"C, an exothermic reaction of ammonia formation from ABC occurs on an iron catalyst. Ammonia concentration in the gas after the column is not less than 129506. The separation of ammonia from the gas mixture is carried out by two-stage condensation due to its cooling. Cooling in the first stage is carried out by air condensers (not shown in the drawing), and in the second stage - in two vaporizers of liquid ammonia 14 and 15. Liquid ammonia in the amount of 22t/h enters the second evaporator 15 through the subcooler 29 from the receivers of the condenser 28 of two AHUs 25, and into the first evaporator in the amount of 14t/h - from the collector 19 of ammonia condensate (8t/h) and through the pipeline 39 from the receivers of the condenser 28 of two AHU 25 (bt/h). Evaporated ammonia at a pressure of 0.36MPa and a temperature (-57С) in the evaporator 14 is divided into two flows One flow through the pipeline 36 in the amount of 8t/h working flow of ammonia steam with a flow rate of at least 40t/h, with a pressure of at least ZMPa and a temperature of 65"С, obtained in the double-cavity steam generator 21, is compressed by the ejector 16 to a pressure of at least 1.58MPa, and the second stream with the number of bt/h through the pipeline 40 goes through the subcoolers 29 of two AHUs 25 to compression in the ejector 30 of two

AHU 25, preliminarily mixing with vaporized ammonia from the second evaporator 15. At the same time, the working stream of high-pressure ammonia steam obtained through the pipeline 37 with the same parameters and a total amount of 6b7t/h enters the ejectors 27, 30, and 32 of two AHUs 25. At the same time, in ejector 27 working stream with a consumption of 25t/h compresses refrigerant vapors from the rectifier generator with a dephlegmator 26 from a pressure of 1.2MPa to a condensation pressure of at least 1.58MPa. In the ejector 30 of the first stage, the compression of the flow of refrigerant vapors from the evaporator 15, which first passes through the subcooler 29 with a temperature of -23-537C and a pressure of 0.2MPa, is carried out by a working flow in the amount of 26t/h. After the ejector 30, a flow with a temperature of 30"C and with a pressure of no more than 0.6 MPa, it is divided in half. Part of the flow of ammonia vapors in the amount of 28 t/h goes to the absorbers with the receiver 31, where the vapors are absorbed by a weak water-ammonia solution with a concentration of up to 0.3 kg/kg, which comes from the cube of the generator-rectifier with the dephlegmator 26 and solution heat exchanger 34. The strong solution formed in the absorber 31 with a concentration of at least 0.42 kg/kg is fed by the pump 33 through the solution heat exchanger 34 for separation into the rectifier generator with a dephlegmator 26. The second part of the flow of ammonia vapors in the amount of 26t/h from the ejector 30 enters the pressing ejector 32 to a pressure of at least 1.58 mMPa with a high-pressure working flow in the amount of 15 tons/hour, at the outlet of which the temperature is 45"С, and the consumption is 4 1 ton/hour The total flow from the ejectors 32, 27 through the pipeline 38 in the amount of up to 6b7t/h is compatible with the flow from the ejector 16 in the amount of 48t/h through the pipeline 38 to the air condensers 17 and 18. Condensed ammonia is collected in the collector 19, from where the larger (107t/h) part of it, at a temperature of no more than 45"C, is fed to the two-chamber steam generator 21 by ammonia pumps 20, which provide a flow rate of up to 115 tons/hour.

Thus, the installation of a double-cavity steam generator for the production of high-pressure working ammonia vapors for the ejection process, ejectors included in the flow of ammonia vapor injection between the dephlegmator and the condenser of two AHUs, between the subcoolers and absorbers of the AHUs, pressing the ejector of the working ammonia vapor from the second evaporator, the ejector compression of ammonia vapors from the first evaporator, air condensers (together with existing ATC condensers) for condensing ammonia vapors, an ammonia condensate collector and a pump for supplying liquid ammonia to a two-cavity steam generator allows for the creation of a steam-ejector refrigeration system, which ensures an increase in the efficiency of the ammonia production plant due to exclusion from the circuit of an ammonia turbocompressor driven by an electric motor with a capacity of 4,000 kWh of electricity, an increase in the cooling capacity of two AHUs, a decrease in the boiling temperature of ammonia in the evaporators, as well as the cooling temperature of the circulating gas per secondary condensation units.

At the same time, the use of a double-chamber steam generator according to this scheme ensures the utilization of low potential heat of the spent water vapor of the process air compressor turbine in the amount of about

ZoGcal/h, which was irreversibly lost in air cooling condensers, and working steam is obtained with a pressure of at least ZMPa in the amount of (54.5.103-550/250)-120t/h (where 250kcal/kg is the specific heat of vaporization of ammonia at a temperature of 657C and of pressure ZMPa; 550 kcal/kg - specific heat of condensation of spent water steam of the turbine), which is necessary for the ejection process. Installation of ejectors in the scheme of two

The AHU between the dephlegmator and the condenser allows to stabilize and reduce the pressure in the generator-rectifier with the dephlegmator to the level of 1.2 MPa, and the condensation pressure - to the level of at least 1.58 MPa, which will ensure a decrease in the concentration of the weak solution in the cube of the generator-rectifier to a value of no more than 0 ,Zkg/kg. Installing an ejector between the subcoolers and absorbers of two AHUs allows you to stabilize and lower the ammonia pressure in the evaporator to 0.2 MPa, and in the absorber to a level of no more than 0.6 MPa, which will ensure a decrease and stabilization of the boiling temperature of ammonia in the evaporator at the level (-15" C), and in the absorbers of AHU due to the increase in pressure - an increase in the concentration of the solid solution to a level of at least 0.42 kg/kg. This will lead to an increase in the solution degassing zone to the value of (0.42-0.3)-:0.12 kg/ kg, due to which the multiplicity of solution circulation will decrease to the value 1-(0.993-0.3)/(0.42-0.3)-5.8, where 0.993Зkg/kg is the concentration of ammonia vapors at the outlet of the dephlegmator at 1 -557C and P-1.2 MPa (according to experimental data).

Reducing the circulation rate, as is known (I.S. Badlkes, R.L. Danilov, Absorption Refrigeration Machines." - M.: Pishchepromizdat, 1966. - P. 89, P. 291 | will allow to increase the consumption of liquid ammonia to the value of p-ai - 82.5/5.8-14t/h, where Sg-Merg t110m3/h.750 kg/m3-82.5t/h - consumption of strong solution.

This will make it possible to increase the cooling capacity of the installation by almost 1.5 times to 8 Gcal/h at a much lower boiling temperature of ammonia in the evaporator (no more than -157C), which is especially important in the summer, when the heat load of the circulating gas on the evaporator is particularly large. At the same time, the condensation pressure in the AHU stabilizes to a value of at least 1.58 MPa, and seasonal and daily changes in the temperature of the air cooling the AHU condensers and the water cooling the absorbers will practically not have a significant impact on the stability of the operation due to the constancy of the pressures AHU. Increasing the refrigerating capacity of AHUs, which are included in the operation of the second evaporator, will ensure a decrease in the required refrigerating capacity of the first evaporator, which used to be part of the ATK, to the value of 2 Gcal/h. The required amount of working ammonia vapors, according to calculations made in accordance with the well-known algorithm (Sokolov E.Ya., Singer N.M. Struynye apparatii!. - M.: Znergia, 1970. - p. 86 - 94), will be for injection of steam from the dephlegmators to the condensers of two AHUs no more than 25t/h, for the injection of steam from the first evaporator up to 40t/h, from the second evaporator included in the operation scheme of the AHU, no more than 42t/h, the production of which is provided by a double-vacuum steam generator. At the same time, in order to obtain this amount of working steam (107t/h), 50t/h of spent water vapor of the process air compressor turbines will be needed. In addition, the peculiarity of this installation is that in the summer the flow of spent water vapor, which is used to obtain high-pressure ammonia vapor in the double-cavity steam generator, has a higher temperature - at the level of 90"C, and in the winter the temperature is 82" WITH. This provides the possibility of obtaining steam with a higher pressure in the summer, and therefore a higher injection coefficient, which makes it possible to increase the refrigerating capacity in the steam ejector cycle, and in the cycle

AHU - a lower temperature in the evaporator, the general temperature of cooling the circulating gas, regardless of the time of year and day - at a level of no more than (-57C).

Therefore, due to the use of a flow of spent water vapor in a two-vacuum steam generator, a self-regulating system of the required increase in cooling capacity in the summer is provided. Also, the thermal load on the fans of the air condensers of the spent turbine pair is reduced, which will allow two electric motors of the fans to be disconnected from the three currently operating and consuming 324 kWh of electricity each. Finally, the withdrawal from the ATK scheme will allow to reduce the costs of repair work and shorten the period of annual overhaul, which means to increase the annual productivity of the synthesis unit.

Thus, with the implementation of the proposed installation, the ammonia turbo-compressor refrigeration unit, which consumes 4000 kW-h of electricity, is completely removed from operation, and the refrigerating efficiency of absorption-refrigerating units is increased by 1.5 times, and the secondary condensation temperature is stabilized at a level of no more than (-57С) regardless of the time of year and day.

The economic efficiency of the application of such a scheme, in comparison with the prototype, is ensured by the reduction of electricity consumption due to the removal of the ATK ammonia synthesis unit from the scheme and the reduction of the secondary condensation temperature in the summer period by an average of 5"C. At the same time, the reduction in electricity consumption from the use of the proposed installation will be:

MEM -AM2-Ma-Ma-Mv, where M1-4000kWh - electricity consumption for the ATK drive according to the old version;

Ma-972kWh - electricity consumption for the drive of air cooling fans of the spent turbine pair of the process air compressor according to the old version;

Maz-2000kWh - electricity consumption to drive fans of air condensers for condensing ammonia vapors in a steam-ejector refrigeration system according to a new version;

Ma-324kWh - electricity consumption to drive the fans of the air condensers of the spent steam turbines of the process air compressor according to the new version;

M5-16OkKWh - electricity consumption for the drive of the liquid ammonia pump according to the new version. m-4000-972-2000-324-160-2488kWh.

At the cost of electricity 156 hryvnias. for 1 thousand kWh and the average annual operation of the unit 8000 hours, the economic effect due to the reduction of electricity consumption will be about 3.105 million hryvnias.

Lowering the temperature of secondary condensation in the summer period (5 months) will allow to reduce the consumption of natural gas by 800 thousand cubic meters, desalinated water - by 8000 tons. At the cost of natural gas 190 hryvnias. for 1 thousand m and desalinated water UAH. for 1 ton, the economic effect will be about 150,000 hryvnias. At the same time, the total economic effect for one unit will amount to almost 3.3 million hryvnias. 1 TDAVTNKS KONADNNET 00 ek hnkyarRePE I 11. E 1 s Yak i tA AV 3 nya 5 E K nya ek mo urny g in shik

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Claims (1)

A plant for ammonia production, containing serially connected departments of desulfurization, reforming, steam generation, carbon monoxide conversion, monoethanolamine purification, methanation, compression with a steam turbine and a process air compressor for reforming, air condensers of spent turbine steam and a turbocompressor refrigeration unit connected by a pipeline system, synthesis department with two evaporators for cooling the circulating gas in the secondary condensation section, one of which is included in the scheme of operation of two absorption-refrigeration units consisting of a generator-rectifier with a dephlegmator, an air-cooling condenser with a receiver, a subcooler, an absorber with a receiver, and a strong solution supply pump , a heat exchanger of solutions, which is distinguished by the fact that it is additionally equipped with a double-cavity steam generator, one of the inlets of which is connected to the exhaust steam outlet pipeline of the turbine of the process air compressor for reforming, and one of the outlets its for condensed water vapor is connected to the inlet of the condensate supply to the air condenser for subcooling it in this condenser, along the flow of high-pressure working ammonia vapor is connected by pipelines to steam ejectors for compression of evaporated ammonia vapors from the first and second evaporators, ammonia vapors from dephlegmators of two absorption-refrigerating units, by the pressure ejector of ammonia working vapors of the absorption-refrigerating units of the second evaporator, entering the air condensers of the ammonia turbo-compressor refrigerating unit, and additionally installed air condensers connected to the collector of liquid ammonia, after which the distribution into two streams is carried out , from where one of the flows due to mixing partially with the flow of liquid ammonia from the condensers of absorption-refrigeration units is connected to the first evaporator, and the second flow is connected to the pump of liquid ammonia, the output of which is connected to the second input of the double-cavity steam generator for obtaining working of ejection pairs.