UA57714C2 - A process for producing methanol - Google Patents

Abstract

A process for producing methanol by contacting the gas mixture containing 1.0 –33.7 % of volume of carbon oxide, 0.3-10.0 % of volume of carbon dioxide at the volume ratio of carbon to the sum of carbon oxides which is equal to 1.91-5.60 with a catalyst containing copper at temperature of 190-290оС, pressure 5.0-10.0 MPa and volume speed of 4500-15000 hours-1 in the cascade of flow reactors in one stage, at that methanol and water are isolated after each reactor. The process allows to completely eliminate the energy costs for gas circulation and simplify the technology of the process.

Description

Description of the invention

The invention relates to the field of basic organic synthesis, in particular to the production of methanol from carbon oxides and hydrogen.

There is a known method of obtaining methanol, which includes the reaction of carbon monoxide and dioxide with hydrogen under a pressure of 1.0 - 15.0 MPa (mainly from 190 to 2707), a volumetric speed of 7000 - 25000 h in the presence of a catalyst containing copper and zinc oxides and, at least one difficult-to-reduce metal oxide of the second - fourth groups of the periodic table, separation of methanol from the reaction mixture and recirculation of substances that did not react in the synthesis of methanol. As a raw material, a mixture of carbon oxides and water-day is used, in addition, carbon dioxide is kept in the amount of 1 - 2095 vol (mainly C - 1295 vol). In the reaction gas, which is in contact with the catalyst, the volume ratio of hydrogen to the sum of carbon oxides is 1.3 - 3.0 times greater than the stoichiometric, (patent of Great Britain

Mo. 1159095, MKI SO7S 31/00, from 08.18.65 to 07.23.69)

The disadvantage of this method is the low specific productivity of the catalyst (0.191 - 0.425 kg/l time), which contains copper, as well as significant energy costs for recirculation of the gas mixture.

There is also a known method of obtaining methanol from synthesis gas, which contains hydrogen and carbon oxides, where fresh gas is fed into a reactor that operates without circulation of the gas mixture, and gas that did not react after condensation of methanol is fed as fresh gas into a reactor with circulation fresh gas The flow reactor works isothermally (application of the Federal Republic of Germany 3518362 MKI СО7С 31/04 from 05.22.85, op. 11.27.86)

The disadvantage of the described method is the use of high-power compressors for the circulation of the gas mixture in the second stage, which means significant energy consumption.

The method of obtaining methanol by contacting a gas mixture containing carbon monoxide, carbon dioxide and hydrogen with a catalyst containing copper at a temperature of 190 - 290702 and a pressure of 5 - 10MPa in two stages is closer in terms of the set of features to the claimed invention. At the first stage, the catalyst containing copper is brought into contact with a gas mixture containing 5 - 309506. carbon monoxide, 10.3 - 20.095 vol. Ge) of carbon dioxide with a volume ratio of carbon monoxide to carbon dioxide of 0.25 - 87.6 and a volume ratio of hydrogen to the sum of carbon oxides of 2 - 3.65. This stage is carried out in a flow-type reactor in a cascade of hot-precision reactors at a volume velocity of the initial gas mixture of 4506-10000047, while obtaining a gas mixture that contains carbon monoxide, carbon dioxide, hydrogen, methanol vapors and 10.02 - 1 .3876 vol. of water vapor, indicated vapors of methanol and water are removed from the gas mixture. The excess of the gas mixture, which contains carbon monoxide, carbon dioxide and hydrogen, is fed to the second stage, which is carried out in the reactor during the circulation of the gas mixture with a volume velocity of 7000 - 1500047 m! receiving after the second stage a gas mixture containing carbon monoxide, carbon dioxide and hydrogen, methanol and water vapors, which are removed from the gas mixture (application ROT 88/00580, MKI - with СО7О 29/15. dated 23.07.87 r.op, 28.01 .88 years old) oh

The disadvantages of this method include the low specific productivity of the catalyst, which contains copper, in the second stage, which creates, depending on the synthesis conditions, 0.40 - 0.68 t/m3 time, a small contribution of methanol obtained in the first stage to the total amount, from 5.42 to 78, 33, high circulation rates of the gas mixture. This implies the use of high-power compressors and significant energy consumption for the circulation of the gas mixture, which significantly worsens the technical and economic indicators of the process. The second disadvantage of the specified method (pt) c is the limited range of changes in the concentrations of the components that are part of the initial gas mixtures.

The existing methods of hydrocarbon conversion make it possible to obtain gases with a higher content of carbon monoxide and nitrogen than stated in the prototype for processing into methanol. Thus, high-temperature conversion of hydrocarbons produces gas mixtures with a carbon monoxide content of more than 3395 vol., and steam-air conversion produces gases with a nitrogen content of more than 4095 vol. Using the method proposed in the prototype, it is uneconomical to process gases with a high content of carbon monoxide (more than 3095 vol.) and a high content of nitrogen into methanol, although there is such a need at industrial sites. In the first case, the ratio of reacting components becomes below stoichiometric

Ш- and the degree of conversion of carbon oxides into methanol decreases due to a lack of hydrogen in the cycle. In the second - first case, when using gases with a high nitrogen content, the specific productivity of the catalyst is sharply reduced due to the low content of reacting components of carbon monoxide, carbon dioxide, and hydrogen in the gas, which are in direct contact with the catalyst. At the same time, it is impossible to achieve acceptable economic indicators of the process due to high energy costs for gas circulation, which consists mainly of nitrogen - an inert component in the synthesis of methanol.

The basis of the invention is the task of improving the method of obtaining methanol in which, thanks to the process being carried out in a cascade of flow reactors in one stage, energy costs for the circulation of the gas mixture are eliminated and the technological scheme of the process is simplified while maintaining a high specific productivity (F) of the catalyst | high degree of conversion of carbon oxides into methanol. The problem is solved by the fact that in the specified method, methanol is obtained by contacting a gas mixture containing carbon and hydrogen oxides with a catalyst containing copper at a temperature of 190 - 2907C, with a pressure of 5 - 10 MPa and a volume velocity of 4500 - 18550h4. according to the invention, the initial gas mixture, which contains 1.0 - 33.795 vol. of carbon monoxide, 1.3 - 22.595 vol. of carbon dioxide with a volume ratio of hydrogen to the sum of carbon oxides of 1.91 - 5.650, as well as 0.5 - 50.095 vol. nitrogen and sequentially passed through a cascade of flow reactors, besides, methanol and water are released by condensation between the stages of the cascade.

The essential distinguishing features of the proposed method of obtaining methanol are as follows: 65 methanol is obtained in two or more reactors operating without circulation of the gas mixture, sequentially connected to each other in a cascade, with the release of methanol and water after each reactor;

the initial gas mixture, which is fed to the first plug reactor, contains 1.0 - 33.795 vol. of carbon monoxide, 0.3 - 22.595 vol. of carbon dioxide with a volume ratio of hydrogen to the sum of carbon oxides of 1.91 - 5.60, as well as 0.5 - 50.0965 vol. nitrogen

Gas mixtures obtained from various raw materials using various technological processes, as well as waste gases from other enterprises, can be used as raw materials for methanol synthesis. According to studies, for the production of methanol in a cascade of flow reactors, it is possible to process gases within a wide range of changes in the concentrations of reacting components, while achieving a high productivity of the catalyst of 0.45 - 2.85t snzone/m3 time with a high degree of conversion of carbon oxides from 69.50 to 93.8595. The proposed 70 limit of the volume ratio of H2/СО and СО», which is equal to 1.91 - 5.69, for the initial gas mixture was chosen for the following reasons. A decrease in the volume ratio of Но/СО and СО» to less than 1.91 leads to a decrease in the degree of conversion of carbon oxides into methanol due to a lack of hydrogen in the source gas, while in subsequent reactors the ratio of reacting components is sharply removed from the stoichiometric one. The upper limit of the volume ratio of Но/СО ж-СО" is equal to 5.60 and is determined by the fact that at higher ratios of 75, the specific productivity of the catalyst decreases due to the low amount of carbon oxides in the source gas. The lower limit of the amount of carbon monoxide in the initial gas mixture is 195 vol. is explained by the fact that at low concentrations of carbon monoxide, water sharply inhibits the synthesis of methanol, as it is formed by two reactions, both by reaction | and by reaction II, which, due to the lack of CO, proceeds in the direction of hydrogenation of carbon dioxide;

SO" and ZNo is" SNZON i NO (I)

SO" I No "in SO I NoO (1)

In the case of using gas with a low CO/CO 5 ratio, as can be seen from the table, the specific productivity of the catalyst decreases, the number of flow reactors in the cascade increases, which leads to an increase in Capital and operational costs. The upper limit of the amount of carbon monoxide is 33.77 vol. is explained by the fact that with a higher amount of O, the ratio of the reacting components is significantly lower than stoichiometric, which i) leads to a decrease in the degree of conversion of carbon oxides into methanol due to a lack of hydrogen in the source gas.

The lower limit of the amount of carbon dioxide in the initial gas mixture is 0.395 vol. is explained by the fact that with a further decrease in the amount of CO" in the gas, the rate of methanol synthesis decreases sharply, and in the absence of CO" the reaction of synthesis of methanol does not take place at all (Y.B. Kagan, O. Ya. Rozovsky, G. D. Lin and Dr. Kinetics and Catalysis, 1975, v. 66, Mo

Z, p. 809). Limiting the upper limit of carbon dioxide to 22,595 vol. is explained by the same reasons as - limitation of the upper limit on carbon monoxide. In addition, with a higher content of carbon dioxide in the source gas, the number of reactors in the cascade increases due to a decrease in the process speed, if it is necessary to ensure a high efficiency of carbon oxides. The upper limit for nitrogen is up to 5095 vol, explained by the fact that nitrogen -

It turns out to be an inert component, and an increase in its concentration in the source gas entails a decrease in the content of reactive components - carbon dioxide, carbon monoxide and hydrogen. Thus, the specific productivity of the catalyst decreases and it becomes economically impractical to process gases with a higher nitrogen content in the reactor cascade. These negative phenomena are even more apparent (with a high nitrogen content - up to 5095 vol.) in known circulation schemes, where greater energy expenditure is required for the circulation of gas, which consists "mainly of nitrogen." with c The search conducted on the sources of scientific and technical and patent information showed that the totality of all essential features of the proposed technical solution is unknown. Therefore, it can be considered that the proposed method for obtaining methanol meets the requirements of novelty, as it is unknown from the state of the art.

A comparative analysis of the essential distinguishing features of the proposed method and known features shows that these features are used for the first time. And the entire set of essential features of the proposed technical solution allows to obtain a new result - to simplify the technological scheme and improve the technical and economic indicators of the process with a high degree of conversion of carbon monoxide into methanol. Thus, it is possible to conclude that by declaring the method

Sh- meets the requirements of the inventive level. - and The essence of the proposed method is contained in the following why. The initial gas mixture, which contains 1.0 - 33.790 vol. of carbon monoxide, 0.3 - 22.595 vol. of carbon dioxide at a volume ratio of Но/СО - СО" - 1.91 - 5.60 under a pressure of 5 - 11MPa is fed into a heat exchanger, where it is heated to a temperature of 200"C. The heated gas mixture is fed into the first gas stream flow reactor with intensive heat removal, for example, in a tubular reactor. In the reactor, the outlet gas is in contact with a catalyst that contains copper, for example, with copper-zinc-aluminum (53.296 mass, SiO, 27.19 mass. 7pO, 5.595 mass. AI2O3) , or copper-zinc-chromium (56.095 wt. SiO, 25 - 2905 wt. 7p0, 550 17 and 275 wt. St2O3). In the process of the reaction, methanol and water are formed. The heat of the reaction is used, for example, to obtain steam, which can be used for technological purposes. At the same time, the temperature iF) of the gas mixture at the exit from the reactor slightly exceeds the temperature of the initial gas mixture at the entrance to the reactor. The gas mixture that leaves the flow reactor and contains carbon oxides, hydrogen, methanol vapors and water enters to the heat exchanger for heat removal, and then from it to separate methanol and boron water in a separator. The gas mixture that comes out of the separator and contains carbon and hydrogen oxides is heated. in the heat exchanger and fed into the second flow reactor. Depending on the process conditions (quantity and composition of the output gas, volume velocity, temperature, pressure), the cascade can include a different number of reactors - two or more. At the same time, it is advisable to keep the parameters of operation in all reactors of the cascade the same as in the first flow reactor. The following examples are proof of the implementation of the proposed method.

Example 1 (comparative).

Methanol is obtained in two sleep stages, the first stage in cascade 13 of three reactors, and the second stage in a reactor with gas mixture recycling. The initial gas mixture is fed into the first flow reactor, where it is at a temperature of 251 - 2652C, a pressure of 8.6 MPa and a volume velocity of 280604! contacts with 10mU of the catalyst, which

Contains copper. At the same time, 24 tons/hour of methanol is produced. The gas mixture that comes out of the first flow reactor, after separation of methanol and water, is sent to the second flow reactor, where at a temperature of 255 - 264 "C, a pressure of 8.0 MPa and a volume velocity of 22602х7, it comes into contact with 10 m3 of a catalyst containing copper. this produces 22t/h of methanol. After the second reactor, the gas mixture is sent to the third flow reactor. Here, at a temperature of 258 - 2647C, a pressure of 800MPa, and a volume velocity of 1784747, 18t/h of 70 methanol is obtained. A total of 4t/h of methanol is obtained at the first stage at thus, the degree of conversion of carbon oxides reaches 56.7495. The gas mixture that did not react in the first stage after the separation of methanol and water is fed to the second stage in a mine reactor working with recycle, where at a temperature of 200 - 278"C, a pressure of 8.0 MPa and at a volumetric rate of 1225047, 34 tons/hour of methanol are obtained. The total amount of methanol obtained in the first and second stages is OVt/hour, the specific productivity of them from the catalyst is 19097 methanol per hour. The degree of transformation of carbon oxides is equal to 9095. The composition of gas mixtures and the conditions of the process are given in the table.

Examples 2 - 12.

Methanol is obtained in a cascade of two (examples 2, 9), three (examples 3, 4, 8, 10), four (examples 5, 6) and six (example 7) flow reactors. The starting mixture is fed under pressure to a recuperative heat exchanger.

The heated gas mixture is fed into a flow tube reactor with intensive heat removal, where it contacts the copper-zinc-aluminum catalyst (examples 2, 4 - 10), which contains 53,295 wt. SiO, 27.095 wt. 7p0O, 5.595 wt. AI2Oz, or a copper-zinc-chromium catalyst (example 3), which contains 56.0956 wt. СцО, 26.0 - 295 wt. 2, 17.0 out of 295 masses of AI2O".

After cooling the gas stream and condensation of methanol and water gases, the mixture is heated in a predetermined amount of water and fed to the second flow reactor where it again contacts the catalyst and the like. The conditions (3) of the process, specific coefficient and specific productivity are given in the table.

From the examples given in the table, it can be seen that the claimed method opens up opportunities to process gas mixtures obtained by each known method of hydrocarbon conversion, or rejected gases, into methanol, while expanding the range of concentrations as reacting components up to 33.795 vol. of carbon monoxide against 3095 vol. in the prototype and up to 22,595 rpm. of carbon dioxide against 20905 vol. in the prototype, as well as inerts up to 5095 nitrogen in the original gas mixtures. It can also be seen from the examples that the specific productivity of the catalyst for methanol is 0.45 - 2.84 t/mh, i.e. it equals or exceeds the similar indicator of the prototype (0.52 - 1.09 t/m 2h) and several times exceeds the value of the specific productivity catalyst, which is achieved in modern technology. At about 35 modern industrial plants for the production of methanol, the specific productivity of the catalyst is relatively small, up to 0.3 tons/mhour under a pressure of 5 MPa and up to 0.4 tons/mhour under a pressure of 8 MPa. In addition, in the proposed method, in the absence of recirculation of the gas mixture, a high degree of processing of raw materials into methanol is achieved (70 - 9496), due to the fact that the removal of reaction products (methanol and water) between the stages of the cascade eliminates the thermodynamic inhibition of the process by them. In order to reduce the inhibition of carryover by reaction products in the traditional circulation scheme and to achieve almost complete (85 - 95965) conversion of carbon oxides into methanol, the synthesis must be carried out at high gas circulation rates and intensive withdrawal of liquid products from the cycle, which requires significant energy consumption. The number of reactors in the cascade and the volume of a single reactor depend on the composition of the gas and catalyst activity. The input or output of one of the reactors in the cascade makes it possible to easily adjust the power of the installation, taking into account the cyclical demand for methanol. Implementation of the proposed method in a cascade of flow reactors favorably distinguishes it from other known methods, as it allows to completely eliminate energy consumption for gas circulation, to simplify the process technology. - ; schi p reactors bo liuempya. 11111180 901 70180190 10011001 in your own | in ob. СО» 10,991 17,582 о 61,97 41,232 51,019 ) 5BO99 61,151 83,831 37,788 TATO 61401 ю о 11,194 19,800 ) 22,319 20,706 13,104

Gas consumption at the entrance of 280,000 | 137500/ 150О000/ | 1500007 / 150000/ ) 140000/ / 137500/ 140000/ | 150000/ | 137500/ 65 reactor, nmZ/time 78170 103842 | 99077 108087 | 102527 | 1210681 78786 114242 | 96532

NUSO I SO" vvyh. 2.40 2.23 2.18 2.18 2.18 2.94 3.19 1.91 5.60 2.86

Gas mixture

T-ra at the exit from the 265 250 220 280 250 250 250 250 250 250 reactor, "C and 28000 | BOSO 4500 4688 | 15000 | 5ОСО 004842 | 5ОФО | 4688 | 4842

Number of SNZON t/h 437 32.23 35.6 29.27 26.15 11.82 1 42.32 24.89. 28,38

Python products. t. 2,Ao0 1.58 0.97 1.12 1.93 0.93 ОА 1.55 0.78 1.0 / sНnzon/mZchas

Degree of conversion of SO 21.28 75.12 48.52 53.83 44.06 52.30 24.59 65.21 77 AA 56.65

Co2 into methanol 95

The second reactor

The composition of the gas mixture, 90 8.53/8.99) 2.105/ 1.588/ 2.187) 1.644/ 1.638/ 12.356/ 20.305/ 1.071/ 2.670/ 2.318/ vol. 02 2,634 2,222 1,836 9,840 16,444 1,787 0,690 2,655 19 вхід/вихід Но 67,05/ 69,527/ 68,286/ 68,570/ 68,205/ 78,340/ 74,645/ 61,729/ 93,294/ 77,606/ 61,07 53,847 54,368 54,308 56,663 68,835 64,203 35,082 90,965 70275 нг: o 0.01/0.88 0/0.522 0/0.094 0/0.160 0/0.121 10.13/5.71 0.962/ 0/0.47 0.01/2.204 0/0.38 6.859

Mo B, 45/ 6,31 2,101/ 1,479/ 2,124) 1,629/ 1,373/ 1,573/ 1,332/ 1,449/ 0,790/ 11,8/ 2,358 4.045 2,355/ 35 /1.156) 1.038/ 0.666/ 1.414/ 0.785/ 0.894, 9.448 1.455 1.252 0.762 2.399 0.847 1.172 so 18.56/ 18.806/ 27.07! 26.567/ 27.5921 6.234, 2121 33.7291 1.956/ 16.548/ 14.55 3.793 17.178 16.213 19.664 2.297 2.695 22.А63 0.353 6.556 0.40/8. 0.551/ 0.654/ 0.591/ 0.542/ 0.446, 0.268/ 0.607/ 0.494, 0.833/ s 25.7111 22.134 23.289 18.693 10.810 7.513 35.766 4.487 16.599 ha)

Gas consumption at the entrance to the 226020 44924, 80904/ 73540/ 87155/ 79881/ 103187/ 48000/ 94760/ 76286/ reactor, nmZ/time 30002 56344 5OvTA 64130 66267 90190 87285 28325

T-ra at the exit of the 264 250 220 280 250 250 250 250 250 250 reactor, "S chI zo Tov" - 22602. BOOO 4500 4903 15027 4993 BIB 4800 5BO23 4623

Petoma products. t. 2.20 0.94 1.710 2.88 0.62 0.47 1.43 0.33 0.vo0 che snazOn/mZchas 3 Degree of CO conversion 40.78 93.85 175.46 78.78 70, 74 72.20 44.82 84.75 93.68 83.12

CO2 into methanol in 2 reactors, 95

The third reactor

The composition of the gas mixture, 90 9.85/ 2.A97/ 3.365) 2.515/ 2.904, 11.107/ 18.782/ 2.185/ 2.983, « 20 vol. 02 10,25 3,074 2,90 6,684 15,102 3,293 217 - Entrance/ Entrance No 66.90/ 70,258/ 70,841/ 69,625/ 82,029/ 75,044/ 547471 84,92/ 69 with ng:o 0.01/1.19 0/0.49 0/0.355 0/0.215 0.033/ 0.054; 0/0.064 0.004; 6,301 6,561 1,035

Mo 6.70/ 8.05 2.7143/ 3.961) 3.069/ 2.093/ 2.2591 1.782/ 3.826/ 2.822! 4,173 3,087 2.635 2.050 5.858 3.259 1 SNA 0 1,681/ 2,429) 1,871/ 1,405/ 1,487/ 0,890/ 3,57 7.845/ -i 11.56 10,052 11,074 15,372 1,172 2,817 27,025 2.351 SNZON 0,44/ 2,59 0,651/ 0,586/ 0,539/ 0,348/ 0,298/ 0788

T» Gas consumption at the entrance to the 178470 435221 38834/ 520977 B55578/ 77147 18079/ 485927 reactor, nmZ/time 30138 28561 38686 47684 67080 11810 42083

T-ra at the exit from the 264 220 28 250 250 250 250 250 reactor, "C

Kletierumi 01911868 012181 361000106 yuyu Amount of methanol, time 180 100000000976 07480975 0575 007260 45601042

Petoma products. t. 1.80 1.01 0.88 2.19 0.48 0.48 1.27 0.46 snzone/mZtime 60 Degree of CO conversion 56.74 90.14 90.02 84.21 83.72 60 .55 91.46 92.76

CO2 into methanol in 3 reactors, 95

The fourth reactor

The composition of the gas mixture, 90 2.114/ 7.605/ 17.204/ 65 vol. 02 3,080 2,960 13,451 input/output No 71,930/ 85,554/ 75,786/ 7 63,415 77,964 65,927 nHg:o 0/0,422 0,043/ 0,051/ 5,709 6,348

Mo 3,770/ 3,097 2.397 4.856 3,510 2.150 SNA 2,2911 2,037 1,197/ 2.952 2.309 1.374 (9:60) 18,761/ 1,378/ 3,060/ 10,53

Gas consumption at the entrance to the 31605/ 40556/ 57343/ 76 reactor, nm/time 24535 37783 49975

T-ra at the exit from the 250 250 250 reactor, "S

Zhlstkvm MV beshevstchi 001101010010000rolvyu voi vyS 11 b o Klest ethno tee 00000105 vyv 05" 00000001

Petoma products. t. 2.45 0.43 0.5BO0 zone/mTime

The degree of CO conversion is 91.64 90.64 72/10

CO2 into methanol in 3 reactors, 95 7

The fifth reactor

The composition of the gas mixture, 90 15,260/ vol. СО2 11.304 input/output No 76.761/ 67.071 s no 0.o5O0/ 6.286 o

Ma 3,202/ 3,680 sleep 1,598/ "I 1,836 (9:60) 2,828/ h- 2,033 sNnzoN 0,301 - 7,191 M

Gas consumption at the entrance to 42913/reactor, nmZ/time 37351 And c)

T-ra at the outlet of the 250 reactor, "S zhlstyuvm 11111 bbshvotyai 1111 zhilste metu tya |101010101111111010111114»100111 s Specific products. t. 0.50 "from snzone/mZhs " Degree of CO conversion 80.80

CO2 into methanol in 3 reactors, 95 s

The composition of the gas mixture, 90 12,812/ - and vol. СО» 8,765 input/output No 78,062/ 69,341 - 20 Ngo 0,048/ 5,823

T» Ma 4,282 4,859 sleep 2,134, 2,423 (9:60) 2,366/ (F) 1,733 ka snzon 0,296/ 7,056

Gas consumption at the entrance to the 32085/ 60 reactor, nm/hour 28284

T-ra at the exit from the 250 reactor, "C klum 001011 cheap 111 09 Yulst methanol tche 10111111

Petoma products. t. 0.55 snazOn/mTime -8-

The degree of CO conversion is 86.76

CO2 into methanol in 3 reactors, 95

A reactor with gas mixture recirculation? AI

Obem kru, m syu 1 PI PIL POLON MON NOYA HORSE MON

The composition of the gas mixture, 90 9.64/ 8.77 vol. SO input/output"

But 62.03/ 57.90

Mo 18.95/ 20.26 syu here toovnyuno 0000 ozztt AI

Speed Gas circulation, nm! 735006

With/time as well

The specific product is 571 dlstrvat about 010400100500033 4451323

Hug? 00005000 3905 сч 05 о Amount of methanol, time 0098. BASES Beve | BOvO 6088 | 4532 | 4005 | 6219 Z0y1 | 4646 o

Petoma products. 1.09 1.39 0.98 1.09 2.84 0.71 0.Ab 1.49 0.63 0.84 catalyst, t/m Ztschas

Expenses circular. Mixtures 7500 per 1t of SNZON, nmUchas «t

The degree of translation CO - CO | 90.00 93.85 90.16 90.02 91.64 90.64 86.76 91.46 93.68 92.76 in methanol, l

Annual capacity of the plant 784000 434480 47.9120 478400 486840 362560 320040 497520 240880 371680 them (with 8000 hours of operation), t

SNZON! year cha

And c)

Continuation of Table

Number of flow reactors «

The first reactor - with Gas mixture composition, 95 06. СО» 0.500/0.544 | 2,200/2,514 h » inlet/outlet No 34,000/25,027|57,525/46,489 and snzone 0/6,780 0/12,703 -I Gas consumption at the entrance to the reactor, nm/hour 225000 225000 - 50 Ratio of H2g/CO ct CO» in outlet. Gas mixture

Number of SNZON t/h 17.64 31.39

Python products. t. sNnzOn/mZchas

F) Degree of conversion of CO « CO2 into methanol 95 ko Second reactor

The composition of the gas mixture, 95 06. СО» 0.560/0.578 | 2,658/2,710 60 input/output But 26,708/21,138|53,258/44,052 bo snzon 0,587/4,416 | 0.525/9.994

Gas consumption at the entrance to the reactor, nm'/hour 185533 156416

Petoma products. t. СНзЗОн/mЗхас

The degree of conversion of CO « CO2 into methanol in 2 reactors, 90 56.87 75.12

The third reactor 70 Gas mixture composition, 95 06. СО» 0.588/0.596 | 2.838/2.285 input/output No 21.995/17.852|149.030/42.979 snzone 0.597/3.260 | 0.520/5.682

Gas consumption at the entrance to the reactor, nm'/hour 165732 118244 2

Petoma products. t. SNzZOn/mZchas vv |v v

Degree of conv. СО "СО5 in SNZON in хр. act., 90 69.50 88.06 o

Total amount SNZON, t/h 33.12 57.35 "I

A particular product. K-ru t SNZON/mZchas h-

The degree of conversion of CO from "CO" to methanol, 95 69.50 88.06 them in

Claims (1)

35 Formula of the invention The method of obtaining methanol by contacting a gas mixture containing carbon oxides, hydrogen and inerts with a catalyst containing copper at a temperature of 190-2909C, a pressure of 5.0-10.0 MPa and a volume velocity of "20 4500-100000 h"!, which differs in that the initial gas mixture, which contains 1.0-33.795 vol. of carbon monoxide, -in s 0.3-22.595 vol. of carbon dioxide at the volume ratio of hydrogen to the sum of carbon oxides , which is equal to 1.91-5.60, as well as 0.5-50.095 vol. of nitrogen, are sequentially passed through a cascade of flow reactors in one "c" stage, moreover, methanol and water are separated after each reactor. Official bulletin "Industrial Property". Book 1 "Inventions, useful models, topographies of integrated circuit microcircuits", 2003, M 7, 15.07.2003. State Department of Intellectual Property of the Ministry of Education and Science of Ukraine. - and - and - 70 "g" co bo b5