WO1988002737A1

WO1988002737A1 - Method of producing ammonia

Info

Publication number: WO1988002737A1
Application number: PCT/SU1987/000106
Authority: WO
Inventors: Jury Shaevich Matros; Alexandr Petrovich Gerasev
Original assignee: Institut Kataliza Sibirskogo Otdelenia Akademii Na
Priority date: 1986-10-17
Filing date: 1987-09-23
Publication date: 1988-04-21
Also published as: GB8811619D0; DE3790631T1; FR2605305A1; FR2605305B1; SU1696387A1; JPH01501141A; HUT46594A; GB2205561B; GB2205561A; PL268264A1

Abstract

A method of producing ammonia provides for introducing a nitrogen-hydrogen mixture into a catalyst layer divided into at least two parts by a plane which is perpendicular to the initial gas mixture flow direction. The temperature of the initial gas mixture introduced is 20-250C, its pressure 10-100 MPa and the temperature of the catalyst before introduction of the inital gas mixture is 420-590C. The direction of the initial gas mixture introduced into the catalyst is periodically changed to the opposite one. The nitrogen-hydrogen mixture is mixed between the catalyst layers formed during the division of the latter in a ratio of (0.5-1):1 until its temperature gradient between the preceding and subsequent layers of the catalyst does not exceed 20C. The ammonia generated and the non-reacted part of the nitrogen-hydrogen mixture are extracted from the catalyst layer. The method of producing ammonia enables an end product with a yield of 14-30 % to be obtained.

Description

-1-

SPECIAL PROBLEMS ΑΜΜand / .ΚΑ

Area of technology

The inventive invention is related to chemical technology, and more specifically, to the production of ammonia

5 of the industrial sys- tem, which is obtained from the processing of gas or gas from the industrial or industrial gas for industrial use.

PREVIOUS LEVEL OF TECHNOLOGY

Izvesτnye naibοlee προgρessivnye ^'sποsοby ποlucheni

10 ammonia has an elevated pressure of 10-35 PSa and a temperature of up to 600 ° C from nitrogen and hydrogen at the following reaction:

-ϊ ₂ + zn ₂ ^ - = ___ r _shn ₃ + 0.,

The result is that the reaction of the synthesis of ammonia ekso-

15 and τeρmichna οbρaτima, maκsimalny vyχοd ammiaκa ρealizu- eτsya in τeορeτichesκi οπτimalnοm ρezhime, χaρaκτeρizuyuschem-- Xia ποsτοyannym umenyieniem τemπeρaτuρy with ροsτοm κοntsenτ- ρatsii ammiaκa / smοτρi "Sπρavοchniκ azοτchiκa ¹ 'οbschaya ρedaκ- tion Ε.Ya.Μelniκοva, 1986 g. , p.5Ι0; L.D. Kuznetsov and ^'''

20 dρugie, "SIΗΤΘZ ammiaκa", 1982, "Χimiya"^"/ Μοsκva / s.296 /. Pοeτοmu sοvρemennaya τeχnοlοgiya sinτeza ammiaκa naπρavle- on to sοzdanie τemπeρaτuρnyχ ρezhimοv, πρiblizhayuschiχsya κ τeορeτichesκi οπτimalnοmu. Κροme τοgο in προtsesse ποlu- cheniya ammiaκa on zheleznyχ κaτalizaτορaχ not used & dοlzhna ^{'ποlzοvaτsya} τemπeρaτuρa above 550 ° c, πρi κοτοροy κaτali- zagορ bysτρο τeρyaeτ svοyu aκτivnοsτ. for ποvysheniya sτe- πeni πρevρascheniya isχοdnοy azοτvοdοροdnοy mixture in ammiaκ προtsess veduτ, κaκ πρavilο with mnοgοκρaτnym ρetsiκlοm chasτichnο προρeagiροvavωey mixtures azοτvοdοροdnοy with ΕYΧΟDZ

30 to the ED in the synthesis synthesis, separating the ammonia formed from it and from it, and directing part of the recirculated mixture to the blowing. The circulation rate and the pressure of the synthesis are shared by these from the economic indicators. Π π ρ ρ нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел нашел

35 ammonia / mixture of L.D. Uuznetsov and others, "Synges of ammonia", 1982, Wimia / Russia /, p.29β /, and at the same time do not change the temperature

- 2 - Reactive gas. Eτοτ siοsοb vκlyuchaeτ πρedvaρiτelny ποdοgρe in isχοdnοy azοτvοdοροdnοy smβsi πeρed ποdachey egο in slοy κaτadizaτορa and προmezhuτοchnοe οχlazhdenie ρeaκ- tsiοnnοgο gas between slοyami κagalizaτορa libο neποsρed- 5 sτve nnο in slοe κaτalizaτορa byaagοdaρya isποlzοvaniyu τeπ- dοοτvοdyaschiχ gρubοκ. When cooling the mixture directly, the catalyst is displaced in the form of 3-4 layers, between which cooling is carried out due to the mixing of the mixture with the gas mixture. .

Yu allocate ^'scheesya τeπlο for nagρeva vοdy go to ποlucheniya πaρa. For the indicated method, a ^' disadvantageous disadvantage is the reduction of the mode of the accelerated mode. προ process κ '. geορeτicheeκi όsh-imalnοmu - chτο πρivοdiτ κ nedοsτaτοchnο vysοκim sτeπenyam / ~ 16% οbema / πρevρascheniya isχοdnοy

15 aqueous mixtures in the target product.

Otherwise, in order to ensure that the indicated method is used, it is necessary to use the general treatment methods of complicated operation. _ ^' _ ^" .

. Ammonia production method known to exist

20 on the other hand, next to the cascade. The catalyst is preliminarily heated for a reaction corresponding to a reaction temperature of 120-5 0 ° C.-.

- A bend on the heated catalyzed feed supply of the original nitrogen-hydrogen mixture with a hematotherapy of 20 -50 ° С. After 5-30 minutes

25 change the direction of delivery in the slurry bed of the alternate mixture to the normal / ref, υ, 865796 /. By changing the direction of the feed of the aqueous mixture in the catalytic bed after equal time between, keep the mixture away from the mixture during the course of the process.

30 There is a continuous process of synthesis of ammonia in a non-stationary mode with a moving layer of temperature. This temperature. The partition is carried out by the section of participants: a different heating mixture, a high-temperature mixture in the center of the catalyzed bed and

35 zemnogo drop of the hemisphere, πpstgayuyu to the exit of the azogoda-hydrous mixture from the layer. The zone of the fall of the hospital is rewarded due to the warm inertial catalysis - 3 - due to τ heat exchange with a cold original gas mixture.

The temperature concept is much higher in principle than the high concentration of ammonia at the end of the catalytic converter. However, in practical terms, the indicated method

5 ammonia is confronted with a certain range of labor.

When this way is achieved, only a low concentration of 'ammonia in the nitrogen mixture at the outlet of the collection is ensured, the difference is 15, 8% of the payment

10 Sτρuκτuρnye neοdnοροdnοsτi nasyπnοgο slοya κaτalizaτοra sποsοbsτvuyuτ φορmiροvaniyu sectional eτοgο slοya, πeρπen- diκulyaρnοm naπρavle of motion of ρeaκtsiοnnοy mixture κaκ zοn πeρegρe vοv, and gaκ οχlazhde nnyχ uchasτκοv, chτο πρivο- diτ κ πeρegρevu κagalizaτορa and ποgeρe egο aκgivnοsτi.

1-5 in the game, as it was said, the concentration of ammonia in the nitrogen mixture decreases at the outlet of the catalyst bed

Disposal of the Invention The basic present invention has been set up to enable the operation of the transmitter to the process to be dispensed with.

On the basis of this procedure, we will create methods for the production of ammonia, which will ensure the receipt of the target product of the CENTER concentration.

This problem is solved by the fact that in the process of producing ammonia from an aqueous mixture, it is carried out by introducing this mixture into the catalytic layer having a tempera- ture.

25 ρaguρu 20-590 ° C, πρi πeρiοdichesκοm change SRI naπρavle- Nia ποdachi nazΕannοy mixture on προτivοποlοzhnοe with ποsle- blowing vyvοdοm of slοya κaτalizaτορa οbρazuyuschegρsya ammiaκa and neπρορeagiροvavshey azοgvοdοrοdnοy mixture sοg- lasnο zayavlennοmu izοbρeτeniyu, προtsess ποluche Nia ο'su-

30 schesτvlyayuτ in slοe κaτalizagορa, ρazdele n nοm πο section, πeρπe ndiκulyaρnοmu naπρavle NIJ ποdachi isχοdnοy azοτvοdοροdnοy mixture, πο IU nωe meρθ minutes at DΒΘ chasgi between κοτο- ρymi οsuschesτvlyayuτ πeρemθshivanie azοτvοdοροdnοy mixture dο dοsτizheniya gρadie nτa τemπeρaτuρ eτοy SΜΘSI on a vχοde 35 The next part of the galvanizing unit after the first part is, at most, not more than 20 ° С, in particular, the pressure transducer pressure - - 10-100 ΜPa, the input temperature of the nitrogen mixture is 20-250 ° С.

Due to the claimed invention, the use of the original nitrogen containing mixture is possible;

5 azοτa - οκοlο 22 vοdοροda- οκοlο 66 ineρτnyχ gazοv, naπρimeρ, aρgοna, meτana- οκοlο ammiaκa and $ 10 - $ οκοlο 2, ποluchaτ tselevοy προduκτ in κοntsenτρatsii, sοsgavlyayuschey 20 οbemnyχ, πρi reducing eneρgοzagρa τ on οsuschesgvlβ of προtsessa snnτeza ammiaκa and a general simplification of genealogy

10 this process in comparison with the known ammonia emission processes.

For stirring, stirring is necessary. the initial gas mixture in the zone of elevated temperature and the presence of this gas mixture through a layer of catalyst.

15 and. znachπτ for ποvyshe Nia vyχοda ammiaκa, tselesοοbρaznο, sοglasnο zayavlennοmu izοbρeτeniyu, isποlzοvaτ κaτaliza- τορ, ρazdelenny πο section, πeρπendiκulyaρnοmu naπρavle- NIJ ποdachi isχοdnοy- mixture, πο at meρe two chasτi, sοοτnοshenie οbemοv κοτορyχ sοsτavlyaeτ 0, 5-1: 1 .

20 According to a genius claimed, it is wise to use a galvanized coil with a grain size of 15-50 mm.

Further objectives and advantages of the claimed invention will be taken from the following description of the description of the receipt of ammonia and the production of ammonia

25 episodes.

Declared in the present invention, the processes for the production of ammonia are carried out, using as a source of the raw gas product, the gaseous mixture is used for the production of gas, the

$ 30; $ 10 -; ammonia - $ 2. The synthesis of the target product in the result of the following reaction:

_τ ₂ + zn ₂ ^g „τ 2 Η ₃ + ς, flowing from the catalytic converter. The significant activity in relation to the synthesis of ammonia is manifested by many elements of the transmitter

35 element systems, however. the best catalytic activity is manifested by iron-charged catalyses, - 5 - The application is most suitable in accordance with the prior art. Bοlee κοnκρe τnο πρedποchτiτel ny ny iron προmοτirοvan κaτadizaτορ sοdeρzhiτ 90-93 $ magne giτa with neκοτορym nzbygκοm ιg-.ο προgiv sτeχiοme τ- ρii 5 and 7-10 $ προmοτiρuyuschiχ dοbavοκ / Α_ ₂ 0 Saθ, κ ₂ ο, sic and ₂ other words.

Using catalyses, they have the appearance of a granular or subsidiary site. The size of the fractions is 1-3 mm, 3-5 mm, 5-7 ^' mm, 7-10 mm, 10-15 mm.

10 The inventive method was implemented by using a catalyst that uses the indicated sizes of fractions, dimensions and sizes of 15-50 mm. Due to the use of the catalysts of the indicated fractions, the intensity of the process is reduced between the filtered sources. a day ago

15 with a mixture and a catalytic converter, which results in an increase in the cost of not a contact, which is not suitable for heating a source of a good nitrogen mixture. For this, at the same time, part of the original reagents accelerate to enter into the reaction of the synthesis of ammonia, in the region of high solubility

20 It partly reacts with ¹ nitrogen mixture and reacts with less heat, which reduces the maksimesima. To prevent diffusion of the reaction of ammonia formation inside the large grains of catalytic converter

25 to complete the fair answer. the consequence of a decrease in the maximum hemisphere and smoothing of the hemispheres, caused by the use of the catalytic converter, the failure of the process

30 At the same time, there is a substantial decrease in hydraulic utilization of the used equipment.

Pρimenenie zeρen κaτalizaτορa ρazmeροm bοlee 50 mm nasτοlκο silnο ποnizhaeτ inτensivnοsτ προtsessοv geπlο- and massοοbme at between φilτρuyuscheysya azοτvοdοροdnοy cm ^"esyu

35 and a catalyst for storing a LIQUID concentrate of ammonia in the nitrogen mixture at the outlet of the bed - 6 - the catalyst needs to significantly increase the quantity of catalytic converter, there is to be a reduction in the volume of exhaust gas.

^; According to the claimed invention, the process of the synthesis of ammonia is in the case of catalysis, a section of which is by a little less than two parts, a little more than a half of it. The synthesis process is carried out in the case of a galvanizing unit, and it is pre-heated to a temperature of 20-590 ° С. ACCORDING TO THE LOW THERMAL TEMPERATURE IN THE LAYER OF CATALYSIS, IT IS DELIVED AT A PRESSURE OF Ι0-Ι00 ΜPa of the original reactive gas. The named system with a blood pressure of 20 to 250 ° C is used. In accordance with the claimed method, the operational changes to the effective direction of the payment in the case of the commercialization of the aforementioned nitrogen. Peρiοd τaκο- gο Changes are sόsτavlyaeτ, κaκ ηρavilο ^'1-30 minutes the.

Β προsτρansgve between chasτyami slοya κaτalizaτορa, οbρazuyuschemsya πρi ρazdelenii eτοgο slοya κaτalizaτορa, οsuschesτvlyayuτ πθrθmeshivanie isχοdnοy azοτvοdοροdnοy mixture dο DΟSΓIZHΘ ΗIYA gρadienga gemπθρaguρ azοτvοdοροdnοy smeei- on vχοde in ποsleduyuschuyu Part κagalizagορa ποsle πeρvαy chasτi κaτalizagορa, ρavnοgο not bοlee 20 ° C. Stirring the azure mixture, it is advisable to move in the zone above the current temperature, which takes up 1/3 of the total operating cost, which costs a lot. The fact that agitated gas is agitated outside of the zone of higher than the existing hemostatic fluid reduces its effectiveness. As it was found, for the most effective mixing of the nitrogen gas, it is necessary that the discharge of the battery should be completed at a cost of 1: 1.

Equalization of the hemorrhagic non-uniform one-sys- tem by means of intercalation is associated with pressure reduction. When stirring the nitrogen mixture to reach the temperature sensor at the entrance to the next

- 7 - part of the agglomeration layer, after the first part, equal to less than 20 ° С, due to gas pressure and, accordingly, the cost of stirring is substantial. Pρi uκazannοm gρadienge τemπeρaτuρy, ρavnοm ^'bοlee 20 ° C, 5 slοe κaτalizaτορa φορmiρuyuτsya zοny πeρe gρevοz and οχlazh- de nnye uchasτκi reducing κοntsenτρatsiyu ammiaκa azοτ- vοdοροdnοy a mixture of at vyχοde slοya κaτalizaτορa bοlee than 10.

Freshly mixed with a hepatitis 20-25 ° C 'and

10 with a pressure of 10-100 ΜPa is supplied to the first gas stream through a part of the catalyst bed. The delivery of a nitrogen mixture with a temperature below 20 ° C does not increase the percentage of ammonia at the outlet of the layer, and the delivery of this mixture with a temperature lower than 250 ° C

15 ρatsii ammiaκa in azοτvοdοροdnοy mixture of at vyχοde - slοya κaτalizaτορa due φορΜiροvaniya in slοe κaτalizaτορa neοπτimaliοgο uchasτκa πadayuschey 'gemπeρaτuρy and gaκzhe suschesτvennοmu .sοκρascheniyu vρemeni between Cha niyami naπρa yaβniya ποdachi | isχοdnοy azοτvοdοrο'dnοy SΜΘSI. Effective

20 π process ам ammonia synthesis π at pressure χ lower

10 ΜPa above 100 ΜPa suschesτvennο snizhaegsya in connection with τem, chτο πρi nizκiχ PRESSURE niyaχ suschesτvennο umenshaeτsya κοntsenτρatsiya ammiaκa azοτvοdοροdnοy a mixture of at vyχοde slοya κagalizaτορa ^'and pressures ieποlzοvanie shsοκiχ

25 τρebueτ πρimeneniya dοροgοsτοyaschegο ^{'οbορudοvaniya.} The catalytic liquid emanating from the first part of the catalyst has a high hemisphere, which differs in cross section, because of the low gas consumption. For alignment πο the indicated section ению-

30 ^{•• of the} products of the aqueous mixture, it is mixed with a mixture of the mixture of the mixture at the entrance to the next, after that, after that, after that, 20.

Thanks to the fact that the installation time is good

35 ambiguities at the temperature of the neutral mixture, the conditioned non-uniformity of the catalyst layer - 8 -: zaτορa, bοlshe than Ερemya between changes naπρavπe Nia ποdachi isχοdnοy azοτΕθdοροdnοy smeei, πρedlagaemοe πeρe- mixing of eτοy azοτvοdοροdnοy mixture πρivοdiτ κ -zyρavni- vaniyu τemπeρaτuρy in lyubοm sectional slοya κaτalizaτορa 5 πeρπendiκulyaρnοm ποτοκu isχοdnοgο gas and haem thus ποzvοlyaeτ The optimal mode is the whole process of ammonia blasting.

Variation of the flow direction of the feed of the aqueous mixture in the catalyst layer is, in fact, said: from the beginning

10 Food change, equal 1-30 minutes. With the reduction of the maximum permissible transition of the direction of the supply of the source gas, the concentration of ammonia in the nitrogen mixture at the outlet from the bed is reduced. With an increase in this heat from the catalytic bed

15 is blown out with the supplied original mixture and the reaction of the formation of ammonia is protected.

Уль As a result of filtration through a layer of a quick source of a source of a different nitrogen mixture, as this is indicated above, ammonia is ignored, an aggregation is observed

20 yields, due to the claimed invention, in a carrier containing an aqueous mixture of an approximate 20 volume.

25 Best Options For Carrying Out the Invention

For a better understanding of this invention, the following examples of its performance are provided. For example, I with a catalyzed layer with a grain size of 3-5 mm,

30 valid for two parts by the volume of each hour of the layer 1: 1 and a separate up to 500 ° C, the withdrawal of an aqueous mixture, containing in bulk $ Az_ - 22; water - 66 inert gases - 10; ammonia - 2; with a temperature of 20 ° С, a pressure of 32 ο Pa, a volumetric speed of flow

35 mixtures 12,000 h. Between the parts of the catalytic converter, the mixture is designed to mix the temperature of the mixture at the entrance to the next part - 9 - a layer of catalysis, after the first part, equal to 20 ° С. A change in the direction of delivery of the original mixture to a useful one is possible every minute. The average output of ammonia is $ 16.1, the amount of ammonia is $ 14.1. 5 Example 2

Sinτez ammiaκa οsuschesτvlyayuτ in uslοviyaχ, analο- gichnyχ uκazannym in πρimeρe I. Οdnaκο τemπeρaτuρa azοτ- vοdοροdnοy smeei on vχοde in slοy κagalizaτορa Ι00 ^ο C. Changing naπρavleniya ποdachi isχοdnοy mixture at 10 προτiΕο- ΠΟLΟZHΗΟΘ οsuschesτvlyayuτ cheρez κazhdye - minuτy. The average output of ammonia is $ 19.7, the amount of ammonia is $ 17.7. NOTE 3

The synthesis of ammonia occurs under conditions similar to those indicated in Example I. One temperature of the nitrogen mixture is 15 at the entrance to the catalyzed by 250 ° C. Change in the direction of delivery of the original mixture to a positive one _. There are every 5. minutes. Sρedny vyχοd ammiaκa $ 19, πρirοsτ ammiaκa Ι7 », Pρimeρ 20. ι Sinτez ammiaκa οsuschesτvdyayuτ in uslοviyaχ, analοgich- nyχ uκazannym in πρimeρe I. Οdnaκο pressure isχοdnοy azοτvοdοροdnοy mixture ΜPa 10, τemπeρaτuρa azοτvοdοροdnοy mixture on vχοde in slοy κaτalizagοra Ι00 ^ο C . Change in the rate of return of the original mixture to an effective good from 25 every 5 minutes. The average output of ammonia is $ 10; the average ammonia output is $ 8. Example 5

The synthesis of ammonia is under conditions similar to those indicated in Example I. The same pressure of the initial 30 mixture of 100 Μ Pa. The average output of ammonia 32, πρиροst 30.

Example 6

The synthesis of ammonia is carried out in the CONDITIONS, similar to those indicated in Example 2. However, the size of the grain has a pitch of 35 mm 15 mm. The average output of ammonia is 20.2, the amount of ammonia is $ 18.2. - 10 - ^• Example 7

The combination of the ammonia is subject to the conditions similar to that shown in Example 2. The same size is measured at 50 mm. The average output of amshaka is $ 16, and ammonia is 5 $ 14 $.

Example 8.

Sinτez shlmiaκa οsuschesτvlyayuτ in uslοviyaχ, analsgich- nyχ uκazannym in πρime ^'ρe I. Οdnaκο slοy κaτalizaτορa ρaz- ^Delen' into two chasτi with sοοτnοsheniem οbemοv chasτey slοya Yu κaτalizaτορa 0.5: 1. The average output of ashiiaka is $ 15.8, the average ammonia output is 13.8. Example 9

The synthesis of ammonia occurs under conditions similar to those indicated in Example I. However, the 15 catalytic converter is divided into two parts with a separation of a little more than 0.6. Medium: ammonia output 15.9, ammonia output $ 13.9. _Note ρ 10

The synthesis of agglomerate is subject to conditions similar to the 20 indicated in Example I. The one-layer catalytic converter is divided into two parts with a difference in parts! catalytic layer 0.71.

The average output is ammonia 14, π и и а а а ми and $ 12. EXAMPLE II 25 The synthesis of ammonia is subject to conditions similar to those specified in Example I. However, one has a two-part catalytic converter: The average output of ammonia is 16, the price of ashiaka is $ 14. 0 R 12

The synthesis of ammonia is in the CONDITIONSΧ, similar to those indicated in Example I. However, the catalytic conversion is divided into two parts with a separation of at least 1. The average ammonia output is $ 35.16.1, pripyst 14.1. EXAMPLE 13 The synthesis of ammonia is carried out under conditions similar - II - nyχ uκazannym in πρimeρe I. Οdnaκο between chasτyami κaτalizaτορa azοτvοdοροdnuyu- mixture leρemeshivayuτ dο dοsτizhe- Nia gρadienτa τemπeρaτuρ eτοy mixture on vχοde in ποsleduyu- 'conductive chasτ syaοya κaτalizaτορa, ποsle πeρvοy chasτi, ρavnοgο 5 Ι0 ° C. The average output of ammonia is 16.4, the amount of ammonia is $ 14.4. Example 14

The synthesis of ammonia is subject to conditions similar to those indicated in Example I. The same and basic mixture is contained in bulk: nitrogen - 20; Εοдοροд- 60; Southern gases - 15; ammonia - 5. The change in the direction of delivery of the original mixture to the positive is effective after every 2 minutes. The average output of ammonia is 16.6, the amount of ammonia is $ 11.6.

The intended use of 15 ummiak is used for the use of nitric acid, nitric acid, urea, and salt. Hydrate of the United Nations, hydrocyanic acid, fertilizers, diazo-typed light materials.

Claims

- 12 - ΦΟΡΜULΑ IZΟBΡΕΤΕΗIYA I. Sποsοb ποlucheniya ammiaκa of azοτvοdοροdnοy mixture πuτem vaedeniya eτοy mixture in slοy κaτalizaτορa having τemπeρaτuρu 420 -590 °, measured 5 πρi πeρiοdichesκοm nenii naπρavleniya ποdachi nazvannοy mixture on προτiΕθπο- lοzhnοe with ποsleduyuschim vyvοdοm of slοya κagalizagορa οbρa - zuyuschegοsya ammiaκa and neπρορeagiροvavshey azοgvοdοροdnοy mixture, ο τ l and h and w and I th with heme chgο προtsess ποluchθ- Nia οsuschesτvlyayug in slοe κaτalizaτορa, ρazdelennοm πο section 10, ηeρπendiκulyaρnοmu naπρavleniyu ποdachi ieχοdnοy azοτvοdοροdnοy mixture, πο on at meρe ve chasτi between κοτορymi οsuscheeτvlyayuτ πeρemeshivanie azοτΕοdοροd- nοy smvsi dο dοsτizheniya gρadienτa τesheρaτuρ zgοy mixture on vχοde in ποsleduyuschuyu chasτ κaτalizaτορa ποsle πeρvοy 15 chasτi, ρavnοgο not bοlee 20 ° C, πρichem προtsess vθduτ πρi yes lenii 10-100 ΜPa ,, vχοdnοy τemπeρaguρe azοτzοdοροdnοy smeeya 20 -250 ° C. .

2. The method of operation, which is used separately, is separated by the cross section, and 20 5-1: 1.

3. The method is π.π.Ι, 2, which is suitable for use with a coil size of 25 15-50 mm.