Trapping co2 in process of methanol synthesis

FIELD: chemistry.

SUBSTANCE: claimed invention relates to method of obtaining methanol, which includes the following stages: a) conversion of hydrocarbon raw material at the stage of conversion process to obtain fresh synthesis-gas, which contains carbon oxides and hydrogen; b) reaction between components of fresh synthesis-gas in the circuit of methanol synthesis to obtain raw methanol; c) processing raw methanol to obtain methanol with required purity degree, characterised by the fact that it additionally includes the following stages: d) trapping at least one flow with high content of CO2 in the process of raw methanol processing and e) recirculation of said at least one flow with high content of CO2 in form of input flow for conversion process. Invention also relates to installation for claimed method realisation and to method of reconstructing installation for obtaining methanol.

EFFECT: claimed inventions make it possible to correct stoichiometric factor of synthesis gas.

15 cl, 3 dwg, 6 tbl, 1 ex

 

The technical field to which the invention relates.

The present invention relates to the synthesis of methanol by conversion of hydrocarbons.

The level of technology

Many existing installations for the production of methanol (Meon) work using synthesis gas (syngas), obtained by conversion (reforming) of the hydrocarbon feedstock, usually a light hydrocarbon, such as natural gas. Product conversion is fresh synthesis gas mainly containing carbon oxides (CO, CO2) and hydrogen (H2), which in the circuit of methanol synthesis, working under high pressure, react with methanol obtaining. The original hydrocarbon may be any hydrocarbon or mixture; a simple example is natural gas.

The basis of the known method are the following stages: initial (raw) gas, for example natural gas, is subjected to desulfurization and conversion, getting hot synthesis gas is usually under a pressure of about 20-40 bar; synthesis gas is cooled to recover heat and served in the main syngas compressor to increase the pressure to the set point in the synthesis loop (usually not less than 100 bar); then in the above circuit components in the synthesis gas react with obtaining the so-called raw (untreated) methanol; after that, the crude methanol cleaned the Ute in section distillation order to obtain the required degree of purity.

Steam reforming can be performed with different equipment; non-limiting examples are: separate (Autonomous) primary device for the conversion; the main device for the conversion consistently with the optional device for the conversion, perhaps, a device for autothermal conversion; a separate device for autothermal conversion.

Reactions in the synthesis loop as a whole can be represented as follows:

1)CO+2H2CH3OH

2)CO2+3H2CH3OH+H2O

Source of reagents CO, CO2and H2is the fresh synthesis gas. From the above reactions can be concluded that the concentration of carbon oxides (CO and CO2and hydrogen in the fresh synthesis gas is crucial. The molar ratio of hydrogen to carbon in the synthesis gas obtained in the conversion process, usually determined by the stoichiometric coefficient R:

R=[H2]-[CO2][CO2]+[CO2]

The corresponding thermodynamic value of R equal to 2; however, it is known that the kinetics of reactions in the synthesis loop high pressure (HP) requires the optimal value of R, which is a little greater than 2, preferably in the range of 2.05-2,3 depending on the relationship WITH/CO2. The increase or decrease in the value of R synthesis gas means that the circuit VD operates in accordance with its capabilities.

The stoichiometric ratio of the synthesis gas supplied by the device (s) for conversion, may significantly deviate from the optimal value of R, so you need to modify it to obtain optimal value close to 2.

To well-known measures taken to adjust the value of R include: recycling hydrogen from the purge gas circuit synthesis based on the use of membranes or devices for swing adsorption (PSA) and recycling of the carbon dioxide contained in the exhaust (flue) gas conversion process. Recirculation stream containing H2or CO 2contributes to, respectively, increase or reduce the magnitude of R.

For example, in the method based on autothermal conversion usually receive the synthesis gas with an excess content of carbon oxides (R less than 2); in this case, the recovery of hydrogen from the purge gas circuit VD and adding the selected hydrogen in the fresh synthesis gas helps to adjust (i.e. increase) the value of R. conversely, the host device for the conversion produces a synthesis gas with high hydrogen content; in this case, the stoichiometric coefficient R to be brought into compliance by the capture of carbon dioxide from the exhaust gas of the device for the conversion.

However, the capture of carbon dioxide contained in the exhaust gas is expensive. Normal partition recovery CO2this purpose is largely concerned with the absorption column, in which the flue gas is washed in countercurrent appropriate solution, such as solution-based amine; a solution with a high content of CO2separated in the lower part of the column and purified in the regenerator, in which reboiler lead to the solution heat with the purpose of separation of carbon dioxide from the solution; gaseous stream with a high content of CO2separated in the upper part of the regenerator, is compressed in the respective compressor and return in snowmountain for the conversion.

This partition recovery is usually very expensive and consumes a large amount of energy. To separate carbon dioxide from other components of the exhaust gas does require a significant amount of energy. The effect of this method of trapping CO2the whole process from the point of view of profitability are not to be taken into account.

Most of the existing plants for Meon and many new installations based on the conversion of gaseous source materials, using the main unit for the conversion and, therefore, faced with the problem of excess hydrogen in the fresh synthesis gas. In the conversion process at these facilities usually get fresh synthesis gas with a value of R greater than 3. As mentioned above, the capture of carbon dioxide contained in the exhaust gas, can help to solve the problem, however, is really expensive from the point of view of capital cost and energy consumption. It is therefore necessary to find a less expensive way to determine the balance of chemicals in the fresh synthesis gas, which is close to the optimum value on the output side of circuit synthesis.

In Fig.3 shows a simplified layout of the facility for the production of methanol, the relevant prior art, include the it device 100 for conversion the circuit 103 synthesis section 105 trapping CO2and section 107 of trapping hydrogen. Crude methanol obtained in the circuit 103, is subjected to degassing in the separator 104 is instantly dissolved gas. Carbon dioxide capture from flue gas of the device 100 for the conversion and through the compressor 106 for CO2return in the same device for the conversion. Instantly eye-catching gas 9 from the separator 104 and light fractions 10 released during distillation of crude methanol, return to the main device 100 for conversion as fuel, along with part 13 of the raw material 1 and the thread 18 of section 107 of trapping hydrogen.

Disclosure of inventions

The technical goal of the invention is to design for a method of synthesis of methanol, a simple and inexpensive way to regulate the content of carbon oxides and hydrogen in the fresh synthesis gas, in particular in the fresh synthesis gas with high hydrogen content.

The basic idea underlying the invention is to capture the carbon dioxide dissolved in the crude methanol. It was found that carbon dioxide can be captured using relatively inexpensive equipment in comparison with the equipment used to capture from flue gas devices (steam) conversion. Thus, the invention with Naiman what they cost produces a stream with a high content of CO 2that can be used, at least partially, to match the stoichiometric ratio R of fresh synthesis gas.

In accordance with the invention, the above-mentioned technical problem is solved in the method of producing methanol, comprising the following stages:

a) conversion of hydrocarbons under conversion with fresh synthesis gas containing carbon oxides and hydrogen;

b) the reaction between the components of fresh synthesis gas in the synthesis loop of methanol to obtain a crude methanol;

C) processing of crude methanol to obtain a methanol with the required degree of purity;

different implementation stages:

g) capturing at least one stream containing CO2in the processing of crude methanol and

d) recycling at least one stream containing CO2as the incoming stream on the stage of the conversion.

In this description, the expression "a stream containing CO2"that means a stream containing oxides of carbon, mainly carbon dioxide CO2. With the same value is also used the phrase "stream of CO2".

In preferred embodiments of the invention stage capture stream containing CO2from the crude methanol is carried out using at least one of mireuksa the different technological methods, and preferably with the use of these two techniques:

- capture flow instantly dissolved gas produced when the discharge pressure of the crude methanol obtained in the synthesis loop;

- capture gas stream containing carbon dioxide released during distillation of crude methanol.

Stream instantly dissolved gas produced when the discharge pressure of the crude methanol, contains a significant amount of CO2due to the high solubility of CO2in methanol. The gas flow released during distillation, usually called "light fractions". Light fractions, as a rule, are allocated from the top of the first column (column distillation light ends) section of the distillation and also have a high content of carbon dioxide.

In the private embodiment of the invention, the flow instantly dissolved gas and the flow of light fractions are mixed, forming one stream containing CO2that return in section conversion as input to stage d) of the method above.

The present invention can be applied to the method for the synthesis of methanol, comprising the usual way to capture carbon dioxide from flue gas device for the conversion. In some embodiments of the invention described how dioxide trapping operadis crude methanol is used in conjunction with the method of capture from flue gas device (means) for conversion; in other embodiments of the invention the capture of carbon dioxide from the crude methanol may be the only way to capture carbon dioxide.

The allocated stream containing CO2you can apply to the conversion process directly or indirectly. In a preferred embodiment of the invention a stream containing CO2, squeeze in the appropriate compressor for CO2and at the entrance to a device for the conversion in the conversion section is mixed with the hydrocarbon feedstock. Device for the conversion can be a device for autothermal conversion or primary device for the conversion of, for example, in the form of a catalytic tubular reactor, it is possible, consistently with the optional device for the conversion.

The present invention preferably, but not exclusively, can be used for methods and systems with a separate (standalone) primary device for the conversion of producing synthesis gas with a considerable excess of hydrogen, for example, with the stoichiometric ratio R equal to approximately 3 or more than 3; the capture of carbon dioxide dissolved in the crude methanol, and its recirculation in the device for conversion helps to adjust the stoichiometric ratio to obtain the proper values close to 2.

p> The main advantage of the inventive method lies in the fact that at least part of the carbon dioxide trap far less expensive way as compared with the known method of selection of exhaust gas device for the conversion. It should be noted that in known installations instantly escaping gas and light fractions are used as fuel or disposed of, whereas the present invention provides more efficient use of process flows. Recirculation flows above gives the opportunity to improve lower heating value (LHV) of the fuel gas used at the facility, providing improved performance (efficiency) of the main device for the conversion. This improved performance of the main device for the conversion can be explained by the higher temperature reached in the coils of the device for the conversion, and lower temperature and flow rate of the exhaust gas in the exhaust pipe. In addition, the increased efficiency of the main device for the conversion means lower emissions of pollutants into the atmosphere.

As can be seen further from the embodiments of the invention describing a method of capturing carbon dioxide from flue gas device for the conversion, more sweat is to, containing CO2separated from the crude methanol, for example, instantly dissolved gas and(or) light fractions, served in the compressor for carbon dioxide, mounted on the output side section of the capture, working with the exhaust gas device for the conversion. Recirculation gas to the suction side of the compressor for CO2reduces the amount of carbon dioxide required in energy-intensive way of catching CO2of the exhaust gas, resulting in a gain significant energy savings for the entire method.

In the end, the recycling of carbon oxides (mainly CO2) on the suction side of the compressor for CO2provides the following advantages (economic effect): reduction of costs and energy consumption for conventional partition recovery CO2(if it has one); improving the energy efficiency of the installation and particularly preferred device for the conversion; the reduction of pollutant emissions.

It should be noted that carbon dioxide is a reactant in the synthesis loop, therefore, recirculation of carbon dioxide dissolved in the crude methanol is a positive factor for the synthesis loop.

If necessary, the process may also include the recovery of hydrogen from the purge gas to the synthesis loop. The resulting stream with high content of H 2preferably introduced on the inlet side of the main compressor for the synthesis gas.

The invention relates also to an apparatus for implementation of the method described above. In particular, the invention relates to a device for producing methanol, comprising a conversion section that receives hydrocarbons and produces converted fresh synthesis gas containing carbon oxides and hydrogen; the outline of the synthesis of methanol, which receives fresh synthesis gas and produces crude methanol; the section where the processed crude methanol to obtain a methanol with the required degree of purity; characterized by the presence of

means for capturing at least one stream containing CO2allocated during the processing of crude methanol, and

- means for feeding at least one stream containing CO2in the section of the conversion.

Preferably, the system includes a separator instantly dissolved gas, which, by pressure relief of the crude methanol receive instantly the emitted gas containing CO2. Means for capturing instantly dissolved gas and feed it into the conversion section is made in the form of injection pipeline pumping instantly escaping gas at the compressor inlet for CO2and the feed flow from the compressor to the input section of the type field is AI. In addition, the above means may include a pipeline adapted for trapping gaseous stream of light fractions, eye-catching section of the distillation of crude methanol.

Another object of the invention is a method of reconstruction of an existing installation. Thus, one feature of the invention is a method of reconstruction of the plant for producing methanol, comprising at least a section of the conversion, which takes hydrocarbons and produces fresh synthesis gas containing carbon oxides and hydrogen; the outline of the synthesis of methanol, which receives fresh synthesis gas and produces crude methanol, and the section in which treatment (cleaning) of crude methanol to obtain mainly pure methanol; characterized by providing at least

means for capturing at least one stream containing CO2separated from the crude methanol, and

- means for feeding a stream containing CO2in the section of the conversion.

The first opportunity of application of the invention in the plant for production of methanol with the usual partition recovery CO2includes capture instantly dissolved gas and(or) light fractions and supplying them to the input current compressor for CO2. In this case, energy consumption is reduced in caccialanza CO 2of the exhaust gas, because it uses a cheaper source of CO2from the stream instantly dissolved gas and light fractions. The second application of the plant without capture CO2includes the installation of a new compressor for carbon dioxide. Specialist in the art it is obvious that the reconstruction also includes the provision of necessary equipment and auxiliary devices, such as pipes, pipe fittings and so on

Advantages of the invention will be more apparent in the subsequent detailed description of a preferred variant embodiment of the invention presented as a non-limiting example:

Brief description of figures

Fig.1 is a simplified block diagram of a plant for producing methanol, proposed in the first embodiment of the invention and including the capture of carbon dioxide from the exhaust gas of the main device for conversion

Fig.2 is a simplified block diagram of the setup proposed in the second embodiment of the invention.

Detailed description of the invention

Installation of Fig.1 includes, first of all, the host device 100 for the conversion, the gas cooler 101, the compressor 102 to the synthesis gas, the circuit 103 synthesis of methanol. The main device 100 for the conversion is part of the section 110 converse is, also includes a section (zone) 105 trapping CO2and the compressor 106 for CO2.

The main device 100 for conversion is, for example, catalytic tubular reactor well known type. All of the above equipment in the art it is known and therefore not described in detail. In other embodiments of the invention section 110 conversion may include a device for autothermal conversion or primary device for the conversion consistently with the optional device for the conversion.

In section 110 of the conversion is served containing hydrocarbon raw material 1, for example natural gas. In this example, the natural gas enters the device 100 for conversion to a stream 3, after mixing with stream 12 containing recycle carbon dioxide. Converted hot synthesis gas 4 obtained in the main device 100 for the conversion, is cooled in the gas cooler 101, for example, about 800°C to 100°C or to a lower temperature and through the compressor 102 serves to path 103. Thread 5 means the product coming out of the cooler 101, a stream of 6 - product at the inlet of the compressor 102, and the flow 7 - compressed fresh synthesis gas high pressure supplied to the circuit 103.

The circuit 103 is typically operates under a pressure of about 100 bar, releasing crude methanol 8. Crude methanol 8 is the offer of methanol and water, plus some amount of CO2(usually about 1.5%), and is sent to the distillation section (not shown) for the production of methanol with a given degree of purity or the specified range.

The separator 104 is instantly eye-catching low pressure gas splits the stream 8 of crude methanol to instantly escaping gas 9 and degassed crude methanol 19. The pressure of the crude methanol 8 through a pressure reducer (not shown) to reduce the operating pressure of the separator 104, for example up to about 5 to 10 bar, preferably 6 bar. Thread 19 of the direct methanol located on the output side section of the distillation.

Instantly eye-catching gas 9 containing carbon dioxide, previously dissolved in the crude methanol 8, recycle section 110 of the conversion. Thread 10 light fractions obtained in the distillation section, this example also recycle in section 110 of the conversion.

When more detailed consideration of the circuit of Fig.1 shows that the section 110 conversion fitted with the usual section (area) 105 for capturing CO2and the corresponding compressor 106 with recirculation of carbon dioxide contained in the exhaust gas 11 device 100 for the conversion. Of section 105 of the capture stream 14 with a high content of CO2obtained from the exhaust gas 11, is input to the compressor 106. The compressor 106 issues a stream 12, which mixes the raw material 1 or part 2, as shown in Fig.1, thereby increasing the content of carbon dioxide in the raw material 3 for the device 100 of the conversion.

Instantly eye-catching gas 9 and light fractions 10 mix for the formation of one thread 15, which is fed to the suction side of the compressor 106 and, thus, return to the main device 100 for conversion in the same way as the thread 14 with a high content of CO2. In alternative embodiments of the invention, the threads 9 and 10 can be returned to the section 110 conversion using a separate pressure lines.

Both streams 9 and 10 contain significant amounts of oxides of carbon, mainly carbon dioxide. As an example, instantly eye-catching gas 9 typically has the following composition: 60% CO2about 25% of CH4and 10% hydrogen, with a small percentage of nitrogen (2%), water vapor (2%), carbon monoxide (less than 1%), plus a small amount (less than 0.01%), Ar, methanol. Light fractions 10 may contain, for example, 75% CO2, 20% water vapor, a little methanol and methane, plus inert components and impurities.

In the present embodiment of the invention, the installation also includes a section 107 of trapping hydrogen, designed to capture H2from the stream 16 purge gas withdrawn from the circuit 103. Of section 107 extends thread 17 with a high content is the use of hydrogen, which is mixed with stream 5 out of the gas cooler 101, for the formation of the thread 6 on the input to the compressor 102 gas. It should be noted that hydrogen is a reactant for the synthesis of methanol, as is apparent from the above reactions (1) and (2) thus, the recirculation flow 17 increases the overall efficiency of the installation. The preferred location of the input, as shown, is located between the gas cooler compressor 101 and 102 synthesis gas on the suction side of the above compressor.

In addition, section 107 receives the stream 18 of the fuel gas containing oxides of carbon, which recirculates in the device 100 for the conversion, possibly in a mixture with part 13 of the feedstock 1. The rest of part 2 of the feedstock 1, in this example, mixed with containing CO2thread 12 supplied by a compressor 106, to form the initial reaction mixture 3 device 100 for the conversion. The mixing part 13 depends on the specific needs and can be, for example, about 30% of the total number of raw materials 1.

In Fig.2 presents a simplified diagram of section 110 conversion does not have a section (zone) to capture CO2and the exhaust gas 11 assign. In this case, the flow at the inlet of the compressor 106 is a thread 15 formed instantly eye-catching gas 9 and(or) light fractions 10. The rest of the equipment is the same as in Fig.1.

As Asano above, the invention can also be used to retrofit existing installations. In this case, the invention is most applicable for installation of methanol, the hallmark of which is the capture of CO2of the exhaust gas device for the conversion, as shown in Fig.1. Provided that the installation of methanol already includes section 105 and the compressor 106, the reconstruction is carried out mainly by laying a new pipeline to instantly dissolved gas 9 and(or) light fractions 10 to the suction side of the compressor 106. To receive this additional input compressor usually does not require substantial changes.

For example, a known circuit shown in Fig.3 can be modified in accordance with the scheme of Fig.1, provided in the invention, primarily through the construction of a new pipeline routes to instantly dissolved gas 9 and light fractions 10 to the inlet side of the compressor 106. Thus, the preferred alternative reconstruction in accordance with the invention includes a step of laying a new pipeline to instantly dissolved gas discharged from the synthesis loop when the discharge pressure of the crude methanol, and laying a new pipeline for the secondary stream containing CO2obtained from the section of the distillation of crude methanol, in the direction is to the compressor CO 2feeding section of the conversion.

However, the present invention can be applied to the reconstruction of facilities for the production of methanol without trapping CO2of the exhaust gas, see Fig.2. In this case, the renovation includes the installation of a new compressor 106.

The present invention achieves the above purposes. For example, it was found that the recirculation instantly dissolved gas 9 and light fractions 10 for a given output of fresh synthesis gas in the circuit 103 requires 20% less CO2of section 105 of the capture. Accordingly, a new installation, proposed in Fig.1, can be performed with a saving of around 20% of the cost of section 105.

Example

Below is a comparison between a normal installation for the production of methanol with carbon capture CO2of the exhaust gas 11, shown in Fig.3, and the installation of the proposed invention, in accordance with the scheme of Fig.1. Tables 1A and 1B refer to the typical installation (Fig.3), and tables 2A-2B refers to installing the proposed invention. The comparison is carried out to ensure approximately the same final output.

The power consumption can be calculated as the calorific value of the feedstock 1 (based on LHV) per metric tonne (t) of the obtained methanol. In this example, energopotrebleniya with 7,33 Gcal/t for an existing installation to 7.29 Gcal/t; moreover, tables 1 and 2 show the decrease of temperature and flow rate of the exhaust gas in the exhaust pipe, which increases efficiency and reduces environmental impact. It is possible to calculate that the increase in efficiency of the main device for the conversion reduces carbon dioxide emissions by more than 6500 tons/year.

If radiant Luggage and(or) section capture CO2works with almost maximum capacity, the invention can be used to increase production at the facility by 0.4-0.6% of the final volume of methanol production.

The following tables 1A and 1B include data for the basic setup is shown in Fig.3.

Table 1A (base set)
Stream1234567
The proportion of steam (molar)1,001,001,001,000,850,861,00
Temperature°C15,0192.5 kg198,1870,082,081,3147,9
Pressurebar16,0123,7123,7119,7116,5116,5196,47
The molar flow ratekmole/hour4115,56816,17797,317243,014072,514434,612004,7
Mass flowkg/h68057,1118261,6160969,2240367,3183237,7186369,1142557,9
Compositionmol.% rawthe
CO-0,027%0,024%13,311%16,309%15,916%19,138%
CO21,030%0,579%12,845%7,118%8,718%8,814%10,586%
H20,010%0,632%0,553%45,248%55,440%56,030%67,371%
H2O-57,874%50,823%32,621%17,449%17,017%0,233%
CH497,560% 40,275%35,207%1,559%1,911%2,035%2,447%
Ethan0,520%0,212%0,186%---
Propane0.080%0,033%0,029%----
n-butane0,040%0,016%0,014%----
n-Pentane0,020%0,008%0,007%----
N2 determined as 0.720%0,331%0,292%0,132%rate £ 0.162%0,174%0,209%
O2-------
No0,020%0,009%0,008%0,004%0,004%0,005%0,006%
CH3HE-0,001%0,001%----
Ar-0,002%0,013%0,006%0,007%0,009%0,010%

Table 1B (basic installation)
Stream891011121314
The proportion of steam (molar)0,031,000,811,001,001,001,00
Temperature°C42,149,563,3136,6233,015,040,0
Pressurebar6,00to 4.415,410,9726,5116,011,26
The molar flow ratekmole/hour4719,8148,5 84,919349,2981,21331,51024,0
Mass flowkg/h135319,74646,83215,0534540,742707,622018,743480,3
Compositionmol.% raw
CO0,021%0,641%0,023%----
CO23,214%58,728%74,215%9,284%98,049%1,030%93,959%
H2 0,358%11,242%0,242%--0,010%-
H2O25,048%2,275%18,882%20,339%1.835 squa%-5,930%
CH40,817%24,781%2,087%--97,560%-
Ethan-----0,520%-
Propane-----0,080%-
and-Bhutan -----0,040%-
n-Pentane-----0,020%-
N20,072%2,176%0,188%67,913%0,021%determined as 0.720%0,020%
O2-0,001%-1,653%0,001%-0,001%
No0,002%0,068%-0,004%-0,020%-
CH2OH 70,466%0,002%4,362%.---
Ar0,003%0,085%-0,807%0,094%-0,090%

Table 1B (basic installation)
Stream1516171819
The proportion of steam (molar)0,931,001,001,000,00
Temperature°C51,943,550,050,044,0
Pressure barto 4.4193,5735,0135,016,00
The molar flow ratekmole/hour233,5659,1362,1297,04848,8
Mass flowkg/h7861,88293,03131,35161,7135672,9
Compositionmol.% raw
CO0,416%2,071%0,641%3,815%-
CO264,361%10,390%12,557%7,748%1,329%
H2 7,242%49,858%78,951%14,385%0,004%
H2About8,316%of) 0.157%0,251%0,042%30,035%
CH416,526%34,359%6,879%67,866%being 0.036%
Ethan-----
Propane----
n-butane-----
n-Pentane- ----
N21,453%2,929%0,640%5,720%0,003%
About20,001%0,001%-0,003%-
No0,043%0,085%0,029%0,153%-
CH2OH1,588%---68,592%
Ar0,054%0,150%0,052%0,269%-

The following tables 2A-2B include data reconstructed for installation.

td align="left"> n-butane
Table 2A (reconstructed setting)
Stream1234567
The proportion of steam (molar)1,001,001,001,000,850,861,00
Temperature°C15,0193,0198,9870,082,081,3147,9
Pressurebar16,0123,7123,7119,7116,5116,5196,47
The molar flow ratekmole/hour4098,46812,478531 17243,214076,214458,712028,2
Mass flowkg/h67774,3118236,4161706,0240250,6183185,0186372,8142550,8
Compositionmol.% raw
CO-0,027%0,035%13,295%16,286%15,871%19,079%
CO21,030%0,566%12,726%7,103%8,696%8,779%10,542%
H2the 0,010%0,644%0,776%45,271%55,453%56,098%67,433%
H2About-58,468%50,950%32,604%17,449%16,994%0,233%
CH497,560%39,686%34,898%1,561%1,912%2,038%2,449%
Ethan0,520%0,209%of 0.182%----
Propane0,080%to 0.032%0,028%----
0,040%0,016%0,014%----
n-Pentane0,020%0,008%0,007%----
N2determined as 0.720%of 0.332%0,343%0,156%0,191%0,206%0,247%
O2-------
No0,020%0,009%0,010%0,004%0,005%0,006%0,07%
CH2OH-0,001%0,019%----
Ar-0,002%0,013%0,006%0,007%0,008%0,010%

Table 2B (reconstructed setting)
Stream891011121314
The proportion of steam (molar)0,031,000,811,001,001,001,00
Temperature°C 42,249,563,3133,7234,315,040,0
Pressurebar6,00to 4.415,410,9726,5116,011,26
The molar flow ratekmole/hour4718,7141,884,918986,71040,71356,4870,0
Mass flowkg/h135138,24373,93215,0522389,043469,622430,536941,3
Compositionmol.% raw
CO0,020%0,643%0,023%-0,089%--
CO23,051%57,301%74,215%8,598%92,321%1,030%93,959%
H20,362%11,886%0,242%-1,639%0,010%-
H2O25,155%2,262%18,882%20,380%1,743%-5,930%
CH40,792%25,109%2,087%-,558% 97,560%-
Ethan-----0,520%-
Propane------0,080%-
n-butane------0,040%-
n-Pentane------0,020%-
N20,083%2,628%0,188%68,535% 0,412%determined as 0.720%0,020%
O2-0,001%-1,668%0,001%-0,001%
No0,003%0,083%-0,004%0,012%0,020%-
CH2OH70,532%0,002%4,362%-0,136%--
Ar0,003%0,085%-0,814%0,088%-0,090%

Table 2B (reconstructed setting)
the Otok 1516171819
The proportion of steam (molar)0,931,001,001,000,00
Temperature°C52,043,550,050,044,2
Pressurebarto 4.4193,5735,0135,016,00
The molar flow ratekmole/hourof 226.7691,0382,5308,54854,5
Mass flowkg/h7588,98536,53187,85348,7135764,3
Compositionmol.% raw
CO0,411%1,999%0,614%3,716%-
CO263,636%9,871%11,842%7,428%1,292%
H27,525%50,772%79,805%14,782%0,005%
H2About8,487%0,156%0,249%0,042%30,102%
CH416,485%33,552%6,668%66,877%being 0.036%
E is EN -----
Propane-----
n-butane-----
n-Pentane-----
N21,714%3,402%0,738%6,705%0,004%
O20,001%0,001%-0,003%-
No0,052% 0,101%0,035%0,184%-
CH2OH1,635%---68,560%
Ar0,053%0,145%0,050%to 0.263%-

1. A method of producing methanol, comprising the following stages:
a) conversion of hydrocarbons under conversion process to obtain fresh synthesis gas containing carbon oxides and hydrogen;
b) the reaction between the components of fresh synthesis gas in the synthesis loop of methanol to obtain a crude methanol;
C) processing of crude methanol to obtain a methanol with the required degree of purity;
characterized in that it further includes the following stages:
g) capturing at least one thread with a high content of CO2when processing crude methanol; and
d) recycling that at least one thread with a high content of CO2as input to the conversion process.

2. The method according to p. 1, in which stage (d) capture of flow from the high to the holding CO 2from the crude methanol involves the capture stream instantly dissolved gas in the discharge pressure of the crude methanol.

3. The method according to p. 1, in which stage (g) capture stream with a high content of CO2from the crude methanol involves trapping a gas stream containing carbon dioxide emitted crude methanol distillation process.

4. The method according to p. 1, in which the flow instantly dissolved gas and the flow of light fractions are mixed into a single stream with a high content of CO2forming the incoming stream, recirculating for the conversion.

5. The method according to p. 1, in which the flow with a high content of CO2squeeze in the appropriate compressor for CO2and mixed with the hydrocarbon feedstock at the inlet of the device for the conversion in the conversion section.

6. The method according to p. 1, in which the first stream containing carbon dioxide capture from flue gas conversion; moreover, the flow through the compressor for CO2return to the conversion section; and a stream containing carbon dioxide capture from crude methanol and serves on the suction side of the compressor, and then together with the first flux return section of the conversion.

7. The method according to one of the preceding paragraphs, further comprising the following stages: capture the purge gas from the synthesis loop of methanol; the stream was received with high containing the receiving hydrogen and a flow of fuel gas in the processing purge gas; recirculation flow with a high content of hydrogen in the synthesis loop; recirculation flow of the fuel gas in the section of the conversion.

8. Device for producing methanol, comprising:
the conversion section receiving hydrocarbons and producing converted fresh synthesis gas containing carbon oxides and hydrogen;
the outline of the synthesis of methanol, receiving fresh synthesis gas and producing crude methanol;
section processing of crude methanol to obtain a methanol with the required degree of purity;
characterized in that it also includes:
means for capturing at least one thread with a high content of CO2released during the processing of crude methanol; and
means for feeding at least one stream with a high content of CO2in the section of the conversion.

9. Installation under item 8, comprising a separator instantly dissolved gas to get from a crude methanol instantly dissolved gas containing CO2and the pipeline for submission instantly dissolved gas in the compressor, the feed stream with a high content of CO2to the input section of the conversion.

10. Installation under item 9, further comprising a pipe adapted to supply an additional stream with a high content of CO2highlighted by distillation of crude methanol, to the input of the compressor.

11. The mouth is mounting on p. 9, including additional partition recovery CO2designed to capture the stream with a high content of CO2of the exhaust gas conversion process, and flow with a high content of CO2in the compressor.

12. Installation according to one of paragraphs.8-11, in which the conversion section includes a separate base unit for the conversion, or the main unit for the conversion consistently with the optional device for the conversion of, or device for autothermal conversion.

13. The method of reconstruction of the plant for producing methanol, comprising at least:
the conversion section receiving hydrocarbons and producing converted fresh synthesis gas containing carbon oxides and hydrogen;
the outline of the synthesis of methanol, receiving fresh synthesis gas and producing crude methanol;
section processing of crude methanol to obtain a methanol with the required degree of purity;
characterized in that provide:
means for capturing at least one thread with a high content of CO2released during the processing of crude methanol; and
means for flow with a high content of CO2in the section of the conversion.

14. The method according to p. 13, which provide a means for intercepting a stream with a high content of CO2and this is Otok in partition conversion, paving the route of the pipeline to instantly dissolved gas, the discharge from the synthesis loop when the discharge pressure of the crude methanol, and paving the route of the pipeline for an additional stream with a high content of CO2obtained by distillation of crude methanol, in the direction of the compressor for CO2feeding section of the conversion.

15. The method according to p. 13 or 14, further comprising a stage of Assembly of the compressor for the selected stream with a high content of CO2.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention can be used in the chemical industry. A method of the combined methanol and ammonia production from an initial raw material is realised by means of the following stages. First, synthesis-gas of the methanol production, which contains hydrogen, carbon oxides and nitrogen, is obtained by steam reforming of an initial hydrocarbon raw material at the first stage of reforming and then at the second stage of reforming with air blast. After that, carried out are: catalytic conversion of the synthesis-gas carbon and hydrogen oxides at a single-pass stage of methanol synthesis and the discharge of the methanol-containing output product, and an effluent gas flow, containing nitrogen, hydrogen and non-converted carbon oxides. The non-converted carbon oxides of the gas flow from the preceding stage are removed by hydrogenation to methane at the stage of the catalytic methanation with the formation of synthesis-gas, which has a molar ratio H2:N2, equal 3:1. Ammonia is synthesised by the catalytic conversion of nitrogen and hydrogen, with the discharge of the ammonia-containing product and effluent gas flow, containing hydrogen, nitrogen and methane.

EFFECT: claimed invention provides the creation of a simple and cheap method of the combined production of methanol and ammonia.

7 cl, 1 dwg, 1 tbl

FIELD: oil and gas industry.

SUBSTANCE: invention is related to the method of methanol recovery from gas-vapour mixture at its storage and transhipment and may be used in chemical industry, petrochemical industry, oil and gas producing and processing industries. The method includes extraction of vapours from the gas-vapour mixture in the plant vessel, cooling of the gas-vapour mixture and condensation of vapours in the vapour-condensing unit, condensate return to the vessel and emptying of the vessel. At that cooling of the gas-vapour mixture in the vapour-condensing unit consisting of a vessel for cooled methanol and a packed column installed on it is made to counter-flow interaction of the gas-vapour mixture containing vapours of methanol cooled up to the temperature within the range of minus 25 up to minus 36°C at pressure close to atmosphere pressure when condensed methanol is returned to the vessel for cooled methanol.

EFFECT: method allows increasing quality of storage due to recovery and return of methanol vapours to the vessel.

1 dwg, 1 tbl

FIELD: chemistry.

SUBSTANCE: method is realised by a contact of a feeding flow, enriched with hydrogen and carbon monoxide, with a catalyst of methanol synthesis. The obtained in this way technological flow is cooled, condensed and subjected to separation into a gas phase and a liquid phase with raw methanol. As the feeding flow used is synthesis-gas, obtained by steam gasification of charcoal, representing a product of pyrolysis of preliminarily dried wood wastes. Before the contact of the feeding flow with the catalyst, containing in a mole ratio CuO:ZnO:Cr2O3:MnO:MgO:Al2O3:BaO, equal to 1:0.3:(0.15-0.2):(0.05-0.1):(0.05-0.1):(0.25-0.3):0.05 respectively, its compressing to pressure 3.5-4.5 MPa is performed. After that the flow is supplied into a reactor, where a temperature of 250-300°C is supported due to evaporation of recycled water, released from raw methanol, with steam from recycled water from the reactor being directed to charcoal gasification. Cooling of the technological flow is realised conductively from the feeding flow, and condensation is performed by throttling. After separation the gas phase is divided into two flows, one flow is directed for combustion into a pyrolysis chamber, and the second flow is directed to ejection with a ratio of the gas flow to the feeding flow equal to 10:1, respectively.

EFFECT: invention makes it possible to obtain methanol in a waste-free environmentally friendly way without application of additional energy resources.

1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method of producing methanol, dimethyl ether and low-carbon olefin from synthesis gas. The method includes a step of contacting synthesis gas with a catalyst under conditions for converting the synthesis gas into methanol, dimethyl ether, and low-carbon olefins, characterised, wherein the catalyst contains an amorphous alloy consisting of components M-P, M-B or M-B-P, wherein component M represents two or more elements selected from lanthanides and the third, fourth and fifth series of groups IIIA, IVA, VA, IB, IIB, IVB, VB, VIB, VIIB and VIII of the Periodic Table of Elements.

EFFECT: method increases selectivity of the target product by conducting the process in conditions which ensure high conversion of CO and availability of carbon.

16 cl, 3 dwg, 3 tbl, 11 ex

FIELD: chemistry.

SUBSTANCE: invention describes a methanol synthesis method which comprises conversion of hydrocarbon-containing material to obtain synthesis gas (1) containing carbon monoxide and hydrogen and a reaction between components of fresh synthesis gas in a synthesis loop (10) to obtain raw methanol and removing hydrogen-containing purge gas (20) from the synthesis loop. The purge gas is heated by heat recuperation via indirect heat exchange with at least one high-temperature heat source in said method, said heat source being adapted to heat purge gas to temperature not lower than 200°C to obtain a heated purge gas (33), and said heated purge gas, as such, is expanded in a corresponding expander (34), and energy is obtained due to expansion of the purge gas in the expander, wherein said high-temperature heat source used is hot waste gas from the conversion process, wherein the material is converted to fresh synthesis gas (1) or a stream of hot steam. The invention also relates to a methanol synthesis apparatus and a method of reconstructing a methanol synthesis apparatus.

EFFECT: disclosed objects improve overall energy balance of the process.

13 cl, 2 dwg, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method for synthesis of methanol, wherein raw methanol (101) is obtained in a synthesis section and purified in a distillation section (D) to obtain pure methanol (104), a stream (103) of instantaneously escaping gas and by-products (105, 106). At least a portion of said stream (103) of instantaneously escaping gas is treated to separate from said gas a stream (110) containing methanol, and that methanol-containing stream (110) is returned to the distillation section (D) to increase pure methanol production volume, wherein pressure of at least a portion of the stream (103) of the instantaneously escaping gas is raised before treating the stream (103) of the instantaneously escaping gas to separate the methanol-containing stream. The invention also relates to an apparatus for carrying out said method and a method of renovating said apparatus.

EFFECT: method enables to increase pure methanol production volume, safe power consumption and reduce emission of pollutants.

10 cl, 3 dwg, 2 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: method includes heating of source natural gas, mixing of superheated steam with source natural gas, one-stage conversion of gas and steam mixture in reformer to converted gas, cooling of converted gas and its division into two flows. The first flow is subject to one-stage catalytic conversion to methanol while the second flow is subject to catalytic synthesis with production of liquefied hydrocarbon gas which is sent to conversion together with source natural gas and liquid hydrocarbons subjected to stabilisation in rectification tower. Plant for implementation of the above method is suggested also in order to produce synthetic liquid hydrocarbons and methanol; the plant is integrated into production train facilities.

EFFECT: effective coproduction of methanol and synthetic liquid hydrocarbons in the same flow diagram during processing.

15 cl, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention refers to a method and a plant for methanol production from gas of gas deposits and gas-condensate deposits through synthesis gas using excess heat of the main process of methanol recovery from water-methanol solution returned after inhibition of hydrate formation in a system of collection, treatment and further transport of gas of a complex gas treatment plant (CGTP). Method involves catalytic steam reforming process of gas, heat recovery of converted and flue gases, separation, drying, compression of synthesis gas, synthesis of methanol from synthesis gas on low-temperature catalyst, separation of crude methanol and rectification of methanol, and in addition, stages of methanol recovery from water-methanol solution used in the complex gas treatment plant as a hydrate formation inhibitor and mixing of methanol-rectificate with recovered methanol. In addition, the plant includes a methanol recovery unit and a mixing assembly of synthesised methanol-rectificate and recovered methanol.

EFFECT: creation of an efficient method combining production and recovery of methanol within the framework of a single complex plant; improvement of economic indices of the methanol plant; improvement of quality and reduction of prime cost of methanol production, and elimination of additional environmental gas production risks.

24 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for direct conversion of lower C1-C4 paraffins to oxygenates such as alcohols and aldehydes, which are valuable intermediate products of organic synthesis and can be used as components of engine fuel and/or starting material for producing synthetic gasoline and other engine fuels. The method involves passing a mixture consisting of a lower paraffin or oxygen, diluted with an inert gas or air or pure oxygen, through a catalyst bed at temperature not higher than 350°C. The catalyst used is a catalyst system for heterogeneous reactions, which contains microfibre of a high-silica support and at least one active element, the active element being in form of either a MeOxHalv composite or a EwMezOxHaly composite, wherein the element Me in both composites is selected from a group which includes transition metals of groups 5-12 and periods 4 and 5, or elements of lanthanum or lanthanide groups or, preferably, ruthenium; element Hal is one of the halogens: fluorine, chlorine, bromine, iodine, but preferably chlorine; element E in the EwMezOxHaly composite is selected from a group which includes alkali, alkali-earth elements, or hydrogen, and indices w, z, x and y are weight fractions of elements in given composites and can vary in the following ranges: z - from 0.12 to 0.80, x - from 0.013 to 0.34, y - from 0.14 to 0.74, w - from 0 to 0.50.

EFFECT: method enables to achieve high degree of conversion of starting reactants and high selectivity of formation of alcohols.

4 cl, 15 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing methanol by bringing a feed stream rich in hydrogen and carbon monoxide in a reactor into contact with a methanol synthesis catalyst to obtain a process stream, followed by cooling thereof, condensation and separation into a gas phase and a liquid phase with crude methanol. The feed stream used is cleaned gas which is obtained by direct-flow gasification of wood processing wastes. The feed stream is enriched with hydrogen by controlled electrolysis of recycled water before bringing the feed stream into contact with a catalyst containing the following, wt %: copper oxide 62, zinc oxide 31, aluminium oxide 7. The feed stream is compressed to pressure of 4.5-5 MPa and then divided into two streams. One stream is fed into the reactor onto the catalyst for contacting through a heat exchanger which simultaneously cools the process stream. The other stream is fed directed onto the catalyst for contacting and reaction temperature is maintained at 250-270°C. After final cooling of the process stream in the still residue of the distillation apparatus, it is separated by throttling into a gas phase and a liquid phase. After separation, the gas phase is divided into two streams. One stream is fed for oxidation into a direct-flow gasifier and the other is mixed with the feed stream before compression.

EFFECT: invention enables to obtain the desired product via a wasteless method using one readily available catalyst.

1 dwg

FIELD: chemistry.

SUBSTANCE: invention can be applied in chemical industry. Method of simultaneous obtaining hydrogen flow A, suitable for obtaining product A; enriched with hydrogen flow of synthesis-gas B, suitable for obtaining product B, depleted of hydrogen flow of synthesis-gas C, suitable for obtaining product C; and optionally, flow of carbon monoxide D, suitable for obtaining product D, from single flow of synthesis-gas X, characterised by the fact that single flow of synthesis-gas has optimised for production of product B molar ratio of synthesis-gas, determined as ratio H2/CO. Single flow of synthesis-gas X is divided into flow of synthesis-gas X1, flow of synthesis-gas X2, flow of synthesis-gas X3 and, optionally flow of synthesis-gas X4. Flow of synthesis-gas X1 is subjected to stage of realising reaction of water gas conversion aimed at conversion of CO, present in flow of synthesis-gas X1, and water in CO2 and H2. After that, CO2 and H2 are separated and discharged. Part of obtained H2 is applied as flow of hydrogen A. The other part of H2 is connected with flow of synthesis-gas X2, which after that is applied as hydrogen-enriched flow of synthesis-gas B. Flow of synthesis-gas X3 is applied as depleted of hydrogen flow of synthesis-gas C. Optionally flow of synthesis-gas X4 is processed in order to remove carbon dioxide and hydrogen from it. Obtained flow of carbon monoxide is applied as source of carbon monoxide of flow D.

EFFECT: invention makes it possible to reduce total emissions of carbon dioxide.

20 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: method is realised by a contact of a feeding flow, enriched with hydrogen and carbon monoxide, with a catalyst of methanol synthesis. The obtained in this way technological flow is cooled, condensed and subjected to separation into a gas phase and a liquid phase with raw methanol. As the feeding flow used is synthesis-gas, obtained by steam gasification of charcoal, representing a product of pyrolysis of preliminarily dried wood wastes. Before the contact of the feeding flow with the catalyst, containing in a mole ratio CuO:ZnO:Cr2O3:MnO:MgO:Al2O3:BaO, equal to 1:0.3:(0.15-0.2):(0.05-0.1):(0.05-0.1):(0.25-0.3):0.05 respectively, its compressing to pressure 3.5-4.5 MPa is performed. After that the flow is supplied into a reactor, where a temperature of 250-300°C is supported due to evaporation of recycled water, released from raw methanol, with steam from recycled water from the reactor being directed to charcoal gasification. Cooling of the technological flow is realised conductively from the feeding flow, and condensation is performed by throttling. After separation the gas phase is divided into two flows, one flow is directed for combustion into a pyrolysis chamber, and the second flow is directed to ejection with a ratio of the gas flow to the feeding flow equal to 10:1, respectively.

EFFECT: invention makes it possible to obtain methanol in a waste-free environmentally friendly way without application of additional energy resources.

1 dwg

FIELD: chemistry.

SUBSTANCE: invention describes a methanol synthesis method which comprises conversion of hydrocarbon-containing material to obtain synthesis gas (1) containing carbon monoxide and hydrogen and a reaction between components of fresh synthesis gas in a synthesis loop (10) to obtain raw methanol and removing hydrogen-containing purge gas (20) from the synthesis loop. The purge gas is heated by heat recuperation via indirect heat exchange with at least one high-temperature heat source in said method, said heat source being adapted to heat purge gas to temperature not lower than 200°C to obtain a heated purge gas (33), and said heated purge gas, as such, is expanded in a corresponding expander (34), and energy is obtained due to expansion of the purge gas in the expander, wherein said high-temperature heat source used is hot waste gas from the conversion process, wherein the material is converted to fresh synthesis gas (1) or a stream of hot steam. The invention also relates to a methanol synthesis apparatus and a method of reconstructing a methanol synthesis apparatus.

EFFECT: disclosed objects improve overall energy balance of the process.

13 cl, 2 dwg, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: invention refers to a method and a plant for methanol production from gas of gas deposits and gas-condensate deposits through synthesis gas using excess heat of the main process of methanol recovery from water-methanol solution returned after inhibition of hydrate formation in a system of collection, treatment and further transport of gas of a complex gas treatment plant (CGTP). Method involves catalytic steam reforming process of gas, heat recovery of converted and flue gases, separation, drying, compression of synthesis gas, synthesis of methanol from synthesis gas on low-temperature catalyst, separation of crude methanol and rectification of methanol, and in addition, stages of methanol recovery from water-methanol solution used in the complex gas treatment plant as a hydrate formation inhibitor and mixing of methanol-rectificate with recovered methanol. In addition, the plant includes a methanol recovery unit and a mixing assembly of synthesised methanol-rectificate and recovered methanol.

EFFECT: creation of an efficient method combining production and recovery of methanol within the framework of a single complex plant; improvement of economic indices of the methanol plant; improvement of quality and reduction of prime cost of methanol production, and elimination of additional environmental gas production risks.

24 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing methanol by bringing a feed stream rich in hydrogen and carbon monoxide in a reactor into contact with a methanol synthesis catalyst to obtain a process stream, followed by cooling thereof, condensation and separation into a gas phase and a liquid phase with crude methanol. The feed stream used is cleaned gas which is obtained by direct-flow gasification of wood processing wastes. The feed stream is enriched with hydrogen by controlled electrolysis of recycled water before bringing the feed stream into contact with a catalyst containing the following, wt %: copper oxide 62, zinc oxide 31, aluminium oxide 7. The feed stream is compressed to pressure of 4.5-5 MPa and then divided into two streams. One stream is fed into the reactor onto the catalyst for contacting through a heat exchanger which simultaneously cools the process stream. The other stream is fed directed onto the catalyst for contacting and reaction temperature is maintained at 250-270°C. After final cooling of the process stream in the still residue of the distillation apparatus, it is separated by throttling into a gas phase and a liquid phase. After separation, the gas phase is divided into two streams. One stream is fed for oxidation into a direct-flow gasifier and the other is mixed with the feed stream before compression.

EFFECT: invention enables to obtain the desired product via a wasteless method using one readily available catalyst.

1 dwg

FIELD: explosives.

SUBSTANCE: invention relates to the method for production of methanol from synthesis gas, including a stage of synthesis gas compression, a stage of catalytic conversion of synthesis gas into methanol in a reactor unit, comprising several catalytic reactors, including operations of heating and conversion of synthesis gas into methanol in each reactor, an operation of reaction products cooling and methanol release after each reactor, an operation of end gases recycling. Besides, the process is carried out under various pressures and with catalysts loaded into reactors with alternating activity under axial and/or radial direction of reagent flow in catalytic reactors in the temperature range of 160-290°C, pressure range of 3-15 MPa, volume speeds of flow 500-10000 hr-1.

EFFECT: method makes it possible to increase efficiency of the process and to produce raw methanol of high quality.

5 cl, 2 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an oil medium which is suitable for producing dimethyl ether and/or methanol which is used in a synthesis reaction with a suspended layer as a medium which contains a basic component in form of a branched saturated aliphatic hydrocarbon containing 16-50 carbon atoms, 1-7 tertiary carbon atoms, 0 quaternary carbon atoms and 1-16 carbon atoms in branched chains bonded with tertiary carbon atoms; wherein at least one tertiary carbon atom is bonded with hydrocarbon chains with length of 4 or more carbon atoms, lying in three directions. The invention also relates to a method of producing dimethyl ether and a mixture of dimethyl ether and methanol using said oil medium.

EFFECT: use of the present oil medium ensures high efficiency of synthesis.

9 cl, 4 ex, 1 tbl, 1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to multireactor system and method of production by equilibrium-limited reaction. System comprises reaction vessel to sustain working temperatures and pressures of reactions. Note here that said vessel has multiple reaction zones made by separation walls, separation tank to sustain said temperatures and pressures. Note also that said separation tank has multiple separation zones made by separation walls and reaction sets comprising multiple heat exchangers for feed-and-discharge flows. Note that heat exchanger of first reactor set interacts with reaction zone via feed flow while heat exchangers of the other reactor sets interact with reaction zone via return flow.

EFFECT: higher efficiency of methanol cascade system.

20 cl, 7 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing methanol from natural gas, involving heating starting natural gas, obtaining superheated steam from prepared water and mixture thereof with the starting natural gas, single-step conversion of the vapour-gas mixture in a reforming furnace into converted gas, cooling the converted gas and single-step catalytic conversion of the converted gas into methanol in a synthesis reactor, wherein the heat of flue gases from the reforming furnace is used to heat the starting natural gas and the prepared water, superheating the steam and vapour-gas mixture, as well as heating the converted gas before inlet into the synthesis reactor. The invention also relates to apparatus for realising the described method.

EFFECT: use of the present invention increases efficiency of recycling energy from heat flux while simultaneously simplifying the conversion and synthesis processes.

11 cl, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: in order to produce synthetic gas containing hydrogen and carbon monoxide, starting material containing methane undergoes partial oxidation using a multichannel burner fitted with a system of separate channels. Methane-containing material, at temperature higher than 500°C, flows through one channel of the burner and oxidising gas flows through another channel. The channel for the methane-containing material and the channel for the oxidising gas are separated from each other by a channel through which a second gas containing hydrogen, carbon monoxide and/or hydrocarbon flows, where the second gas is at temperature 10°C lower than its spontaneous ignition temperature. The second gas is obtained from gaseous by-products of a Fischer-Tropsch synthesis process or from gaseous by-products of a methanol synthesis process.

EFFECT: improved process.

22 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: method includes the supply of diluents and the first monomer into the first polymerisation reactor, formation of the first polyolefin in the first suspension, continuous discharge of the transported suspension from the first polymerisation reactor into the second polymerisation reactor. After that, the polymerisation of the second monomer is performed in the second polymerisation reactor with the formation of the second polyolefin. By means of the first discharge device of a continuous action, located on the second polymerisation reactor, pressure regulation in the second polymerisation reactor is realised and the rate of the suspension flow, discharged from the first polymerisation reactor, is supported higher than 4 ft/sec (1.2 m/s).

EFFECT: prevention of the reactor clogging and support of the suspension in a stable state in transportation makes it possible to increase efficiency, reduce the time of the system standstill and increase the total amount of production.

20 cl, 6 dwg

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