UA20992U - Installation for ammonia production - Google Patents

Abstract

Installation for ammonia production relates to refrigeration engineering and provides decrease of electric power consumption in the process of circulation gas cooling, with increase of cold productivity and stabilization of temperature mode at section of secondary condensation.

Description

Description of the invention

The utility model applies to refrigeration equipment, as well as ammonia production plants.

A known facility for the production of ammonia, containing serially connected departments of sulfur purification, reforming, vaporization, carbon monoxide conversion, monoethanolamine (MEA) purification, methanation, compression with a steam turbine for driving a compressor of process air for reforming, a compressor for compression of fresh nitrogen -hydrogen mixture (ABS) and circulation compressor, air condensers of spent steam turbines, condensate collector with a pump for returning it to the steam formation department, 70 synthesis department with a condensation column, a remote heat exchanger, a synthesis column with a gas start-up heater, a water heater, air cooling devices with a separator for the primary condensation of ammonia and two low-temperature evaporators for cooling the circulation gas in the section of the secondary condensation of ammonia to a temperature of no more than 59C, one of which is included in the scheme of operation of the ammonia turbocompressor refrigeration unit (ATK) by project holo with an additional productivity of 4.2 Gcal/h with an air t condenser for condensing the refrigerant compressed by the ATC compressor, and the second - to the scheme of operation of two water-ammonia absorption refrigeration units (AHU) with a design cooling capacity of 5.4 Gcal/h (see

Permanent technological regulations of the ammonia workshop 1-B, Mo. 114. - Severodonetsk: PO "Azot", 1985. - 72265.;

Kuznetsov L.D., Dmytrenko L.D., Rabina P.D., Sokolinsky Yu A. Ammonia synthesis. - M.: Chemistry, 1982.-S.11-16,

P.155).

Disadvantages of this installation include: high energy costs for obtaining cold with the help of ATK, the consumption of electricity for the drive of which is 4000 kW h; increased electricity consumption for cooling the spent water vapor of the turbine of the process air compressor in the air condensers, in which three fans are used, consuming 972 kW h of electricity; the low potential rbv is not used. The heat of the spent water steam of the turbines with a pressure of 0.04MPa, a temperature of up to 902С and a consumption of 54.5t/h, which is about ZOGcal/h; insufficient reliability of the APC operation, which often fails, which requires the availability of a backup APC for the normal operation of the production as a whole, as a result of which the volume and time of repair work increases, both during the period of operation and during the annual shutdown repair of the ammonia synthesis unit. with

A well-known synthesis unit with a condensing column, a circulation line with a mixture of gas with ammonia vapors, absorption refrigeration units, a turbocompressor refrigeration unit, equipped with air cooling condensers and evaporators with liquid refrigerant supply lines and Ge withdrawal lines! refrigerant vapors (see AS USSR Mo1002756 IPC G25815/04, publ. bulletin Me9 dated 07.03.8311.

The disadvantage of this unit is the impossibility of turning off the turbo-compressor refrigeration unit in the island

35 is the spring-summer period, when the high temperature of the atmospheric air, which causes the temperature to rise to almost 402C during the cooling process of the circulating gas with the help of air condensers in the primary condensation section of the synthesis department. After the circulation compressor compresses the circulating gas, its temperature rises to 502C, which leads to an increase in the heat load with the circulating gas due to the temperature increase even up to 249 (1822 according to the project) on the low-temperature evaporators of the secondary condensation section, and therefore to an increase in the cost of electricity for the production of cold at the expense of the ATK. At the same time, the temperature of secondary condensation reaches the critical limit of 59C, which is unacceptable according to the technological regulations.

The closest in terms of technical essence and achievable effect is the ammonia production plant, which contains successively connected departments of desulfurization, reforming, steam generation, carbon monoxide conversion, monoethanolamine (MEA) purification, methanation, compression with a steam turbine and a process air compressor, connected by a pipeline system for reforming, air condensers of spent turbine steam and o turbocompressor refrigeration unit, synthesis department with two low-temperature evaporators for cooling circulating gas in the secondary condensation section, one of which is included in the scheme of operation of two ise) absorption-refrigeration units as part of a generator-rectifier with a dephlegmator , an air cooling condenser with a receiver, a subcooler, an absorber with a receiver, a pump for supplying a strong solution, a heat exchanger for solutions, a two-cavity steam generator, one of the inputs of which is connected to the exhaust pipe of the exhaust steam of the compressor turbine process air for reforming, and one of its exits 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, it is connected to 22 pipelines with steam ejectors for compression of evaporated vapors ammonia from the first and second low-temperature evaporators, ammonia vapors from the dephlegmator of two absorption-refrigeration units, the pressure ejector of working ammonia vapors of the absorption-refrigeration units of the second low-temperature evaporator, which enters the air condensers of the ammonia turbocompressor refrigeration unit, and additionally installed air condensers, with connected to the liquid ammonia collector, 60 after which it is divided into two streams, from where one of the streams, due to partial mixing with the stream of liquid ammonia from the condensers of absorption-refrigeration units, is connected to the first low-temperature evaporator, and the second stream connected to a liquid ammonia pump, the output of which is connected to the second input of a two-cavity steam generator for obtaining working steam for ejection | see Declaration patent of Ukraine Mo6b5356 A, IPC g25815/04, E25849/00, СО1С1/04, publ. Bull. Ministry of Health dated 15.03.2004). because the disadvantage of this installation is the increased consumption of electricity in the amount of about 2200 kW h for the drive of air cooling fans for condensation of almost 120 t/h. of working steam and refrigerant steam and an ammonia pump drive for supplying 107t/h. liquid ammonia.

The need to condense ammonia vapor requires the use of 10 condensers, each of which weighs 69.7 tons and consists of two air cooling devices of the type ABZ-14.6-16-B1-83T4 with an electric motor of the type

VASV-14-34-24 for driving a fan with UK-2M blades, which leads to an increase in the total metal capacity of the installation only due to capacitors up to 700t. Taking into account the significant distance of up to 100 m, which occurs in real conditions, the AHU from the steam generation department, the total metal capacity will exceed 1000 tons due to the laying of additional pipeline communications to the AHU ejectors. 70 In addition, the parallel operation of two AHUs on one evaporator is impractical, which complicates the process of controlling the operation of the AHUs and leads, under conditions of different resistance, in the steam lines of the steam supply to the generator-rectifier and the suction lines of the ammonia vapor between the evaporator and the absorber to a mismatch of pressures, respectively, in rectifier generators and absorbers. The amount of ammonia vapors sucked in the two installations will be different. The concentration of water-ammonia solutions, the multiplicity of circulation, and therefore the 7/5 cooling capacity will also be different. This phenomenon is observed in real operating conditions, as a result of which it is impossible to ensure the same maximum cooling capacity of each installation. Drainage of phlegm from one evaporator to two AHUs also leads to a difference in AHU operating modes.

The task of the useful model is to reduce the consumption of electricity in the process of cooling the circulating gas, increase the cooling capacity and stabilize the temperature regime in the secondary condensation section.

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, a compressor for compression of fresh nitrogen -hydrogen mixture, an air heat exchanger for cooling the nitrogen-hydrogen mixture and a circulation compressor, an air condenser of the spent water vapor of the gas turbine and a water condensate collector with a pump for returning it to the steam generation department, a steam ejector refrigeration system as part of a two-cavity steam generator, one of the inlets of which is connected to by the pipeline of the exhaust steam outlet of the process air compressor turbine for reforming, and one of its outlets for condensed steam is connected to the inlet of the condensate supply to the air condenser for subcooling it in this condenser, working steam to which comes from the second exit of the double-cavity steam generator, the air condenser of the turbo-compressor refrigeration unit, the ammonia condensate collector and the liquid ammonia supply pump to the second entrance of the double-cavity steam generator, the synthesis department b" with a condensation column, a remote heat exchanger, a synthesis column with a start-up heater gas, Fu water heater, air cooling devices with a primary condensation separator and two low-temperature evaporators with absorption-refrigerating units for cooling the circulating air in the secondary condensation section, which is distinguished by the fact that, in order to increase efficiency, it is additionally equipped with a third high-temperature evaporator, the pipe space of which is connected to the circulation gas flow between the circulation compressor and the condensing column, its inter-pipe space is connected to the vapor ejector refrigeration system by the refrigerant flow, and each of the two is parallel in formed by the flow of circulation gas exit from the condensing column of low-temperature evaporators "CONNECTED WITH absorption-refrigeration unit. sv c The diagram shows the scheme of the ammonia production plant.

The installation consists of a desulfurization unit 1, reformer 2, steam generation 3, carbon monoxide conversion )» 4, monoethanolamine purification 5, methanation b, compression 7, which contains a steam turbine 8 for driving a process air compressor 9, a four-stage compressor 10 for compression of fresh nitrogen hydrogen mixture

With an air heat exchanger 11 for cooling this mixture and a circulating compressor 12 for compressing the circulating gas in the synthesis department 13 to ensure its continuous circulation through a high-temperature evaporator 14, a condensing column 15, two low-temperature evaporators 16 with absorption-refrigeration units 17 connected to each of them, remote heat exchanger 18, ammonia synthesis column 19 with a starter

Ge) heater (not shown in the diagram), water heater 20, external heat exchanger 18 (by return flow), 5p air cooling devices 21 with separator 22. Spent water steam from turbine 8 is connected to air condenser 24 with a collector through pipeline se) line 23 water condensate 25 and pump 26

It is returned to the steam generation department, and along the pipeline line 27 - to the entrance of the double-cavity steam generator 28, the steam ejector refrigeration system (SPC) 29, which, in addition to the steam generator 28, contains a jet compressor 30, an air condenser 31, a condensate collector 32, and an ammonia pump 33. Output from outlet of the steam generator 28 through the condensate cavity is connected by the pipeline 34 of the water condensate outlet for subcooling to the air condenser 24. The second outlet of the double-cavity steam generator 28 with the working ammonia steam supply pipeline 35 is connected to the steam jet compressor 30 for injecting refrigerant vapor from the high-temperature evaporator 14 and supplying compressed ammonia vapor to the air condenser 31 with the collector of ammonia condensate 32, the output of which through the pipeline 36 goes to the high-temperature evaporator 14 as a refrigerant, and through the pipeline 37 - to the pump 33, the return of ammonia condensate to the second inlet through the ammonia cavity of the steam generator and 28.

According to the scheme, the installation process is carried out as follows. Natural gas, for example, in quantity

ZBvOOnM h at a pressure of 4.4 MPa is mixed with a nitrogen-hydrogen mixture (ABS) in the amount of bobonm/h until the hydrogen content in the mixture is 10.795 vol. and is fed to the desulfurization department 1. In the desulfurization department 1, in the catalytic 65 reactor on a cobalt-molybdenum catalyst at a temperature of 3902, the sulfur compounds contained in natural gas are hydrogenated to hydrogen sulfide, and then hydrogen sulfide is absorbed on the oxide-zinc absorber until its content is no more 0.5 mg/cm3. The purified gas mixture is mixed with steam, the consumption of which is 132,000 nmU/h, and enters the reforming section 2 of the first stage, where the conversion of natural gas with steam obtained in the steam formation section takes place on a nickel catalyst at a temperature of 8002 and a pressure of 3.5 MPa , to the residual methane content in the gas of 1195 vol. After that, the gas enters the second stage of conversion, where at a temperature of 12002С, steam-air conversion of methane takes place to a residual methane content of 0.395 vol. The consumption of steam for steam-air conversion is 5000Onm Z/h and is provided by the steam formation department 3. The consumption of process air in the amount of 50400 nm Z/h is provided by the compressor 9. The converted gas after the reforming department 2 (in terms of dry gas, 90 rpm) is as follows: SNU/ -0.3; СО»5-11; No-57; M»-22.4; Ag-0.3; CO-9. Gas consumption after reforming is 185,000. nmU/h (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 3802С in the first stage, and at 2202С and a pressure of ZMPa in the second stage. The gas composition after 75 conversion of carbon monoxide (in terms of dry gas, 906 vol.) is as follows: СН/-0.3; СО2-17.3; But-61.6;. Mo-20;

Ag-0.3; CO-0.5. Wet gas consumption after carbon monoxide conversion is 292,000 nm ZU/h. (in terms of dry gas - 207,000 nmU/hour).

The resulting converted gas goes further for purification from carbon dioxide to the monoethanolamine purification department 5, where at a temperature of 409C and a pressure of 2.8 MPa, carbon dioxide 20 is absorbed by an aqueous solution of MEA to a CO content of 0.195 vol. The composition of the gas after purification from CO" (in terms of dry gas, 90 vol.) is as follows: СН.-0.4; СО5-0.1; No-74.5; Mo-24.1; Ag-0.3; CO-0.6. Degree of gas purification from

СО2-99,695. Consumption of purified gas after absorption - 171,Ztys.nm Z/h.

The gas purified from CO" enters for catalytic purification from oxygen-containing compounds in the methanation department 6, where at a temperature of 3502 and a pressure of 2.6 MPa, oxygen-containing compounds are reduced to 25 methane. After separation 6, the nitrogen-hydrogen mixture (ABS) has the following composition (95 vol.): СН /-1.1;. No-74; Mo-24.6; Swiss

Ag-0.3; bОЖСО" - traces. This ABC with a pressure of 2.5MPa and a temperature of 432С enters the compression department 7, where it is compressed by a four-stage compressor 10 to a pressure of 32MPa. 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. сч 30 Spent water steam after turbine 8 with a pressure of 0.4 MPa and a temperature of 80-90 "C (depending on the time of year) is divided into two streams. The first flow in the amount of 32.5t/h through the pipeline 23 enters the air condenser 24, and the second flow in the amount of 22t/h through the pipeline 27 goes to the two-cavity Ф steam generator 28, where it condenses due to the transfer of heat to the liquid, which at the same time av) evaporates, ammonia, which is supplied by the ammonia pump 33 through the pipeline 37 from the collector 32. The formed 35 water condensate of the second flow from the double-cavity steam generator 28 through the pipeline 34 goes to the condensers 24 for subcooling. From the condenser 24, the first and second flows, which have a temperature of 652, are collected in the water condensate collector 25, from where the water pump 26 supplies water for demineralization of oxygen-containing compounds to the steam generation department 3. is cooled in the air heat exchanger 11 to a temperature of 452C and enters the separation part of the condensation column of the synthesis department 13, where it bubbles through a layer of liquid ammonia, is additionally washed from traces of moisture and carbon dioxide and is mixed with the circulation gas. The mixture of ABC and circulating gas passes through the tubes of the heat exchanger of the condensing column 15, where it is cooled by the oncoming flow of circulating gas to a temperature of no more than 302 and then goes into the intertube space of the remote heat exchanger 18, in which it is heated to a temperature no higher than 1952 by the heat of the oncoming gas, which passes through the tubes, and then goes to the synthesis column 19. In the synthesis column, the gas passes from the bottom up through the annular gap between the casing of the column and the nozzle casing and then enters the intertube space of the heat exchanger located at the neck (Se) of the synthesis column. Here, the gas is heated by the heat of the converted gas coming out of the catalyst box to the reaction start temperature of 400-4402C, then the gas successively passes through four catalyst shelves, where at a pressure of no more than 32MPa, the volume velocity is 17900h! and at a temperature of 420 - 5302 there is an exothermic reaction of the formation of ammonia from a nitrogen-hydrogen gas mixture. To maintain a normal temperature regime in the reaction zone, a cold by-pass gas supply is provided in front of each shelf. After passing the fourth layer of the catalyst, the nitrogen-hydrogen-ammonia mixture with an ammonia content of at least 1295 vol. and with a temperature not higher than 5302 99 rises through the central pipe and then passes through the tubes of the intra-tube heat exchanger, cooling to a temperature of not more than 3302С. Next, the gas mixture goes into the pipe space of the heater 20, where the excess heat of the synthesis reaction is used to heat the feed water, which then flows to the steam collector of the waste water boilers of the steam generation department C to obtain steam with a pressure of 10.5 MPa. in Production ammonia from the nitrogen-hydrogen-ammonia mixture is separated by its condensation due to air cooling (primary condensation) and ammonia that evaporates (secondary condensation).

After the water heater 20, the gas mixture with a temperature of no more than 2402C passes through the pipe space of the external heat exchanger 18, being cooled to a temperature of no more than 702C by the gas that flows through the pipe space, and enters the air cooling apparatus 21, where part of the ammonia is condensed from the gas mixture at 65 temperature no more than 402C. Condensed ammonia is separated in separator 22, and the gas mixture containing up to 1195 vol. МНз, goes to the suction of the circulation compressor 12, where it is pressed to a pressure of no more

31.9 MPa, compensating for pressure losses in the system. After circulation compressor 12, circulation gas in the amount of no more than 6b7ths.nm/h. with a temperature of 502C passes through the pipe space of the high-temperature evaporator 14, cooling to a temperature of no more than 359C due to ammonia boiling in the inter-tube space of the high-temperature evaporator 14 at a temperature not higher than 309C, and enters in the amount of 24t/h through the pipeline 36 from the condensate collector 32 of the steam-ejector refrigerator systems.

Ammonia gas from the intertube space of the high-temperature evaporator 14 with a pressure of no more than 1.154 MPa is injected by the ZO jet compressor with working ammonia steam at a pressure of up to ZMPa and a temperature of 659C and is compressed to a pressure of at least 1.6 MPa. A mixture of working ammonia steam and injected gaseous with a temperature of 70.5ZeC after the jet compressor 30 in the amount of 72t/h enters the air condenser 31. The liquid ammonia obtained in the condenser with a temperature of no more than 402C goes further into the collector 32, after which it is divided into two streams. The first flow as a refrigerant in the amount of 24 t/h flows through the pipeline 36 to the high-temperature evaporator 14, and the second flow through the pipeline 37 in the amount of up to 48 t/h is fed by the ammonia pump 33 to the double-cavity steam generator 28, where working ammonia steam is obtained with a pressure of up to t ZMPa, which goes to the jet compressor 30 through the pipeline 35.

The circulating gas, partly with condensed ammonia with a temperature of 352C, after the high-temperature evaporator 14, is fed from above into the condensing column 15, passes through the inter-tube space of the heat exchanger, being cooled by the gas flowing through the tubes to a temperature of no more than 142C. Next, the circulating gas enters two low-temperature evaporators of liquid ammonia 16, where, passing through the tubes, it cools to a temperature not higher than 092 due to ammonia boiling in the intertube space of low-temperature evaporators 16 at a temperature not higher than -5960.

Low-temperature evaporators 16 for circulation gas are connected in parallel and each of them is connected via the ammonia system of the refrigerant to a separate AHU 17. Ammonia gas from the inter-tube space of the low-temperature evaporator 16 goes to the AHU, where liquefaction occurs, and is supplied again to the low-temperature evaporator 16. From the pipe space of the low-temperature evaporator of evaporators 16, a mixture of cooled circulation gas and condensed ammonia enters the separation part of the condensation column 15, where the liquid product ammonia is separated from the gas. In the separation part of the condensation column 15, fresh ABC is mixed with circulating gas, passes through a basket with Raschig rings, where Ge is additionally separated from liquid ammonia droplets. Next, the gas mixture rises through the pipes of the heat exchanger, cooling the circulating gas. The liquid production ammonia from the separator 22 and the condensation column 15 goes after throttling to a pressure of no more than 4MPa into the liquid ammonia collectors (not shown in the diagram). Gee!

Thus, the installation of the third high-temperature evaporator, the pipe space of which is connected to the circulation gas flow between the circulation compressor and the condensing column, and its pipe space to the refrigerant flow - to the vapor-ejector ammonia refrigeration system (PCS) with the connection of each of the two units installed in parallel of the circulating gas flow after the condensation column of low-temperature evaporators to the absorption-refrigeration unit, provides an increase in the efficiency of the ammonia production unit due to the exclusion from the scheme of 4 air-cooling condensers with the consumption of electricity to drive eight fans of 800kWh, an increase in the total cooling capacity of refrigeration systems to 12 Gcal/hour in the summer period and a decrease in the total metal capacity of the refrigeration systems at the secondary condensation section by almost 100,000 bOOt.

At the same time, the use of the third high-temperature evaporator installed according to this scheme )" ensures the winter temperature regime at the secondary condensation section, i.e. the temperature of the circulating gas at the inlet of the condensation column does not exceed 352C, which causes the exclusion of ATK from the scheme of the synthesis unit.

Lowering the temperature in the summer from 502C to 3592C requires the connection of a high-temperature evaporator to the PCS with cooling capacity according to calculations in accordance with the methodology confirmed in industrial conditions, see Efimov V.T., Eroshchenkov S.A., Babichenko A.K. Increase the efficiency of work! absorption refrigerating units in high-capacity ammonia synthesis units. / Refrigeration equipment. - 1979. - Mo2. - se) P.23-26) no more than 6.7 Gcal/h. Such a higher temperature level of circulating gas (50-35) allows

Ge) 20 to increase the boiling point of the ammonia refrigerant in the third evaporator to 292 at a sufficiently high boiling pressure of 1.154MPa. Increasing the pressure makes it possible to increase the injection coefficient of the PCS cycle, which is according to calculations made in accordance with the well-known algorithm E. Ya. Sokolov, N. M. Singer. Jet device. - M.: Znergiya, 1970. - P.86-94Y), is at least 0.5 and provides injection of ammonia refrigerant vapors from the high-temperature evaporator in the amount of 24 t/h with working ammonia steam with a pressure of 22 MPa in the amount of up to 48 t/h . The total amount of refrigerant vapors and working steam for air condensers of PCS will be 72t/h, the condensation of which can be provided by 6b-ma condensers with electricity consumption up to 1200kWh. To obtain working steam in the amount of 48t/h, you will need no more than (48:250/550)-22t/h of spent water vapor (where 250kcal/h is the specific heat of ammonia vaporization at a temperature of 652C and a pressure of ZMPa; 550kcal/kg is the specific heat condensation of spent water vapor of the turbine), due to which it is possible to turn off only one of the three air fans of the spent water vapor condenser of the turbine of the process air compressor with an electricity consumption of 324 kW h.

Therefore, lowering the temperature of the circulation gas to 35 °C at the entrance to the condensation column provides a reduction in the heat load on the secondary condensation unit and the winter temperature distribution in the secondary condensation section 65, which makes it possible to ensure, according to the technological regulations, the temperature of circulation gas cooling by two low-temperature evaporators at a level of no more 09 with only two

AHU with a total existing cooling capacity of up to 5.4 Gcal/h.

Thus, with the implementation of the proposed installation, the ammonia turbocompressor installation is completely removed, as in the prototype, the total cooling capacity increases to 12 Gcal/h, the electricity consumption decreases by 556 bkWh in the process of condensation of the working steam and refrigerant vapor and the supply of ammonia condensate by the pump to the double-cavity steam generator in cycles of the steam-ejector refrigeration system, as well as more than 600 tons of metal capacity of the ammonia production plant while ensuring the regulatory norm of the secondary condensation temperature.

The economic efficiency of using such a scheme, in comparison with the prototype, is ensured by a 70% decrease in electricity consumption due to the removal of four air-cooling capacitors from the synthesis unit scheme and a reduction in the load on the liquid ammonia supply pump in the PCS cycle and the metal capacity of the installation as a whole. At the same time, the reduction of electricity consumption from the use of the proposed installation will be:

MAM Mo M a3-MA-Mv-Mv, where M.-2000kWh. - electricity consumption for the drive of fans of air condensers for 75% condensation of ammonia vapors in the vapor ejector refrigeration system according to the old version;

Mo-324kWh. - consumption of electricity for the drive of fans of air condensers of spent steam turbines of process air compressor according to the old version;

M3-16OkWhd - electricity consumption to drive the liquid ammonia pump in the vapor ejector refrigeration system according to the old version;

MA-1200kWh - electricity consumption for the drive of fans of air condensers for the condensation of ammonia vapors in the vapor ejector refrigeration system according to the new version;

M5-648kWh - electricity consumption for the drive of the fans of the air condensers of the used steam turbines of the process air compressor according to the new version;

Me-8OkWhd - electricity consumption for the drive of the liquid ammonia pump in the steam-ejector refrigeration system according to the new version. -

M-2000-324--160-1200-648-80-556 kW h.

At the cost of electricity for an industrial enterprise 24 UAH. per Itis.kWh and the average annual operation of the unit of 4,000 hours in conditions of increased atmospheric air temperature (spring-summer period), the economic and "there is 3o" effect due to the reduction of electricity consumption will amount to more than O.5 million. hryvnias, and due to the reduction of the metal capacity by 0.000 g at the metal cost of 100 hryvnias. for 1t, costs will decrease by O.bmln. UAH For the active in o

Ukraine's ammonia synthesis unit (and three units operate according to this typical scheme in Ukraine) reduction of Ge"! electricity consumption will be even more and will amount to:

MM Mo Ma-MA-Mv-Mv, o de M.-3Z000OkWh - electricity consumption to ensure the operation of ATK according to the old version; Ge

Мо-972kWh - electricity consumption to drive the fans of the air condensers of the spent steam turbines of the process air compressor according to the old version;

M3-800kWh - electricity consumption for the drive of fans of air condensers for the condensation of ammonia vapors in the ATK cycle; 70 MA-vOkWt'h - electricity consumption for the drive of the liquid ammonia pump in the steam-ejector refrigeration system according to the new version; 1" М5-1200kW h - electricity consumption for the drive of fans of air condensers for the condensation of ammonia vapors in a steam-ejector refrigeration system according to the new version;

Me-648kWh - electricity consumption for the drive of the fans of the air condensers used from the water vapor of the process air compressor turbines according to the new version;

Mm-3000zh972--800-80-1200-648-2844kWh. o At the same time, the economic effect due to the reduction of electricity consumption for the unit operating in Ukraine

Ge) of synthesis will amount to more than 2.7 million hryvnias. at 50

Claims (1)

The formula of the invention Co.) An installation for the production of ammonia, containing sequentially connected by a pipeline system departments of desulfurization, reforming, steam generation, carbon monoxide conversion, monoethanolamine purification, methanation, compression with a steam turbine and a process air compressor for reforming, a compressor for compressing fresh nitrogen hydrogen mixture, an air heat exchanger for cooling the nitrogen-hydrogen mixture and a circulation compressor, an air condenser of the spent water vapor of the turbine and a collector of water condensate with a pump for returning it to the steam generation department, a steam ejector refrigeration system as part of a double-cavity steam generator, one of the inlets of which is connected to the pipeline output of the spent water vapor turbine of the process air compressor for reforming, and one of its outputs for condensed water vapor is connected to the inlet of the condensate supply to the air condenser for subcooling it in this condenser, the working steam to which n departs from the second outlet of the double-cavity steam generator, the air condenser of the turbo-compressor refrigeration unit, the collector of ammonia condensate and the pump for supplying liquid 65 ammonia to the second entrance of the double-cavity steam generator, the synthesis department with a condensing column, an external heat exchanger, a synthesis column with a gas start-up heater, a water heater, air cooling devices and a primary condensation separator and two low-temperature evaporators with absorption-refrigerating units for cooling the circulating gas in the secondary condensation section, which is distinguished by the fact that it is additionally equipped with a third high-temperature evaporator, the pipe space of which is included in the circulation gas flow between the circulating compressor and the condensation column, its the inter-tube space along the flow of the refrigerant is connected to the steam-ejector refrigeration system, and each of the two in parallel installed along the flow of the circulation gas exit from the condensation columns and low-temperature evaporators connected to the absorption-refrigeration unit. what with (o) (o) "c) c - i" name) (in) se) se) Co) 60 b5