Methanol synthesis method

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

 

The technical field to which the invention relates.

The present invention relates to a method and installation for the synthesis of methanol. In particular, the invention relates to energy recovery purge gas to the synthesis loop, working under high pressure.

The level of technology

Fresh synthesis gas for methanol production is usually obtained by steam reforming of the respective raw materials containing hydrocarbons, such as natural gas. Fresh synthesis gas is a mixture of carbon oxides (CO, CO2) and hydrogen (H2), usually under a pressure of about 20-40 bar. Steam reforming can be performed using different equipment; non-limiting examples are: separate (Autonomous) primary device for steam reforming; the main device for steam reforming consistently with the optional device for steam reforming, perhaps with a device for autothermal steam reforming or device for autothermal steam reforming.

Fresh synthesis gas is typically cooled to recover heat and using a multi-stage main compressor is served in the synthesis loop, working under high pressure (HP).

Reactions in the synthesis loop VD in General can be represented as follows: CO+2H2→SN3 HE and CO2+3H2→SN3HE+H2Oh, and a source of reagents CO, CO2and H2is the fresh synthesis gas. The ratio (molar) of hydrogen to carbon in the fresh synthesis gas is determined by the stoichiometric coefficient R:

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

and it is also known that the kinetics of reactions in the circuit VD requires the optimal value of R slightly greater than 2, preferably in the range of 2.05-2,3 depending on the relationship WITH/CO2. Higher or lower R means that the circuit VD operates below its potential.

However, the value of R fresh synthesis gas fed device (s) for steam reforming, can deviate considerably from the above optimal value of R. In particular, at the entrance, in the main device for steam reforming, get fresh synthesis gas with a considerable excess of hydrogen, for example, with a value of R equal to 3 or more, which means a surplus of not less than 50%. This excess hydrogen increases the power of the chief whom the spring and the total flow through the circuit VD without participation in the process of synthesis. Thus, it can be argued that the excess of hydrogen in the fresh synthesis gas has a negative impact on energy balance and performance (efficiency) installations for the production of methanol. In particular, the compression of excess hydrogen in the main compressor essentially means loss of energy.

At least part of the excess hydrogen is usually given from the synthesis loop together with inert gases, forming the so-called flow purge gas. On existing installations, the purge gas used as fuel for the steam reforming section. However, this energy recovery does not compensate for these shortcomings.

Known measure taken to address the problems associated with excess N2in the fresh synthesis gas, is adding carbon dioxide to adjust the values of the stoichiometric ratio R. However, carbon dioxide is not always available. Carbon dioxide can be captured from flue gas device for steam reforming, however, this method requires expensive equipment and large power consumption. The usual section for capturing CO2to this end includes an absorption column in which the exhaust gas is washed in countercurrent with a solution based on amine; a solution with a high content of CO2separated in the lower part of the column and iseut in the regenerator, in which the solution is heated by reboiler 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 to the main device for steam reforming. Another measure is to install additional devices for steam reforming operating on oxygen fuel, but this device is also expensive. A method of producing methanol is disclosed in GB-A-2 142331.

Disclosure of inventions

The technical goal of the invention is to eliminate the negative impact of excess hydrogen in the fresh synthesis gas in the total energy balance.

The idea underlying the invention is the efficient recovery of enthalpy of purge gas through the heated purge gas through heat exchange through the wall using a suitable high-temperature source of heat, which is provided in this way, and the expansion of the heated purge gas in the corresponding expander (expander) to produce mechanical energy. This mechanical energy or part of it can be used as such, for example, to actuate the compressor, or be converted into electrical energy. In addition, the purge gas on the exits the expander can be used as fuel.

Thus, the above-mentioned technical problem is solved in a method for the synthesis of methanol, in which the conversion of a feedstock containing hydrocarbons, getting fresh synthesis gas containing carbon oxides and hydrogen, and the reaction between the components of fresh synthesis gas in the synthesis loop, receiving crude methanol, and in which the purge gas containing hydrogen, away from the synthesis loop, characterized in that, in this method, the purge gas is heated by utilizing the heat obtained by the heat transfer through the wall using at least one high-temperature source of heat in this way, the heated purge gas, as such, extend in the corresponding expander, and based on the extension of the purge gas in the expander gain energy.

High temperature source of heat is any source adapted to heat the purge gas to temperatures above 200°C, and preferably above 350°C. the Preferred temperature range of the heated purge gas is from 200°C. to about 500°C., and more preferred is 350-500°C. the Purge gas can be heated to the temperature above 500°C, if in this way there is a corresponding source of warmth. Heated purge gas is also possible using low-temperature source (s)existing at the mouth of the information, for example, using any source of waste heat, such as condensed water vapor. Before the purge gas is heated to a high temperature, it is preferably heated to a temperature of about 100-120°C.

In accordance with the first feature of the invention, the purge gas is heated by heat exchange with hot flue gas conversion process. In the private embodiment of the invention at least one stage of the process of conversion of raw materials containing hydrocarbons, is mainly the conversion device, and the purge gas is withdrawn from the synthesis loop, passes through the coil in the convection section of the primary conversion. The use of exhaust gas as a heat source increases the temperature of the purge gas to approximately 500°C or more.

In accordance with another feature of the invention, the purge gas is heated by heat exchange with hot water vapor, for example, superheated steam of high pressure, which is usually available on the installation for the production of methanol. Hot steam can, for example, be selected from steam turbines that drive the main syngas compressor. The use of hot steam as a high temperature source of heat usually provides podagra the purge gas to a temperature of 320-380°C.

Variant implementation of the invention with the use of exhaust gas for heating, usually provides a higher temperature purge gas and, thus, obtaining more energy from the expander; a variant embodiment of the invention with the use of steam for heating, usually provides a lower temperature, but, on the other hand, has the advantage that the heater purge gas functionally does not depend on the partition of the conversion. In other words, in this embodiment of the invention from the purge gas get less power, but the influence on the heat balance of the unit of conversion decreases. This solution can be recommended to ensure a smooth and sustainable operation mode conversion device, for example, due to the fact that the flow rate of the purge gas is not constant and tends to increase, for example, due to aging of the catalyst synthesis and the associated performance degradation.

The selection of the preferred option for implementing the invention can also depend on the possibility of exporting electricity to the electrical network. Variant implementation of the invention with the use of exhaust gas for heating, it may be preferable, if there is a need in electric power limit and install or you can export excess electricity on acceptable terms.

In accordance with another feature of the invention before the implementation stage of heating the purge gas is withdrawn from the synthesis loop handle (clear) in the separator. This treatment can be used for the preparation of the purge gas (bring in the desired state) and extract some useful components, such as methane or hydrogen. In one embodiment of the invention a portion of the residual methane is recovered from the purge gas in the form of a gas stream with a high content of CH4that return to the stage of conversion. In another embodiment, the invention is isolated and returned to the process gas stream with a high content of N2.

The expander is preferably connected to a generator that supplies electricity. This electricity can be used to power the electric drive and auxiliary equipment installation for the production of methanol and / or export. In a preferred embodiment of the invention, the energy generated by the above generator is used for actuation of the circulation pump in the circuit VD, and the remainder, if any, export. The mechanical energy produced by the expander, or part of it can be used directly to actuate any on the walking equipment for example, a compressor. Preferably, the expander is an expander.

The purge gas expands as it is, i.e. without burning process. Thus, the above expander provides energy recovery without fire heating by energy conversion pressure purge gas into mechanical energy. Recuperation efficiency is enhanced by the previous stage heating using a high-temperature source of heat, which increases the enthalpy of the purge gas and, thus, the amount of recuperated energy. Extended purge gas at the outlet of the expander retains its calorific value and can be further used as fuel.

The outlet pressure of the expander for the purge gas, preferably, slightly above the pressure of the hydrocarbon feedstock fed to the conversion section. In preferred variants of the invention, the outlet pressure is 1-5 bar, and more preferably about 1.5-3 bar.

In a preferred embodiment of the invention the purge gas away from the pressure of 85 bar and a temperature of 45°C and is heated using steam condensate; part of the methane contained in the purge gas is separated in the corresponding separator and fuel products the intramural gas, having a low content of methane, with a pressure of about 40 bar to approximately 100-120°C by heat exchange with another low-temperature source, and then the flow is heated at least up to 200°C by heat exchange with the use of high-temperature source; then heated purge gas enters the expander under the pressure of 35-40 bar and exits under pressure of about 1.5-3 bar.

The object of the invention is also the setting for methanol synthesis, including the conversion section, in which you can carry out steam reforming containing hydrocarbon feedstock, getting fresh synthesis gas containing carbon oxides and hydrogen, and the synthesis loop, designed for making fresh synthesis gas in the crude methanol, which also includes the pipeline to drain purge gas containing hydrogen from the synthesis loop, characterized in that it includes high temperature, recuperating heat heater purge gas; an expander for the purge gas, which enters a heated purge gas supplied by the heater, and the means necessary for energy recovery from the expansion of the purge gas in the above expander.

The above mentioned means for energy recovery preferably include an electric generator driven detentional possible and direct the use of mechanical energy. In other embodiments of the invention the expander for the purge gas directly connected to the compressor, providing all or most of its power, or is directly connected with the circulation pump circuit synthesis.

Another object of the invention is the reconstruction of the plant for producing methanol by adding at least the following pieces of equipment: high-temperature heater purge gas; means for supplying heat to the heater vent gas using a heat source, available at the facility for the production of methanol; expander for purge gas and means for feeding the expander heated purge gas supplied by the heater; means for energy recovery from purge gas expansion in the expander. According to preferred variants of the invention, the heater purge gas may be in the form of a heating coil in the main conversion device or a heat exchanger that uses the heat of the water vapor, as described above.

The main advantage of the invention lies in the energy recovery pressure purge gas effective way. The amount of recovered energy is considerable, due to the high pressure of the corresponding flow rate of the purge gas. For example, on an installation for the production of methanol with a capacity of 5000 MTD (metric tons per day), you can recover up to 15-20 MW of electricity. Preparation of the purge gas prior to its heating leads to a loss of pressure, however, contributes to obtaining in this way a useful thread, as well as to reduce specific consumption for heating the purge gas, expressed in kcal/h to kW. A concrete example is given in the detailed description.

Recovered mechanical and (or) electric energy can be used on the same installation for the production of methanol for actuation of pumps, compressors, etc. In a preferred embodiment of the invention the electric power used to actuate the circulating pump circuit VD using a motor instead of a steam turbine. The drive does not require any additional supply of energy, as electricity produces the equipment for the production of methanol.

It may be noted that proposed in the invention, the energy recovery compensates for the energy consumption at the stage of compression of the synthesis gas that is associated with an excess of hydrogen. Advantages of the invention become more apparent in the subsequent detailed description of a preferred variant embodiment of the invention presented as a non-limiting example.

the quick description of figures

Below the invention is described in more detail with reference to the accompanying drawings on which is shown:

figure 1 - simplified block diagram of a plant for producing methanol, proposed in the first embodiment of the invention,

figure 2 - scheme, proposed in the second embodiment of the invention.

Detailed description of the invention

Fresh synthesis gas 1 supplied from the conversion section (not shown), compressed in the first stage 2 and secondary 3 main compressor driven by a steam turbine 4. Intermediate cooling and separation of the liquid fraction to provide through cooler 5 synthesis gas and the separator 6. Output stream 7 from the main compressor is sent to the circuit 10 high-pressure synthesis of methanol by the circulation pump 8 driven by an electric motor 9.

Fresh synthesis gas is heated in heat exchanger 11 and fed into the reactor 12 synthesis in which the catalytic conversion in the crude methanol. Hot thread 13 arising from reactor 12, is cooled in the recuperator 11, air the refrigerator 14 and the heat exchanger 15 water-cooled and fed into the separator 16. Liquid crude methanol 17 to receive the lower part of the separator 16, while in its upper part to receive the gas stream 18. Heat away from the reactor 12 in the doy 60, evaporating to form a pair 61.

The portion 19 facing the gas stream 18 are returned to the circulation pump 8, while the other part 20 is the purge gas is withdrawn from the circuit 10 VD. Part 20 is, as a rule, the smaller part, for example, 10-20% of the total mass flow rate of 18. This part preferably regulating valve 21.

The purge gas 20 is treated in the wash column 22 for separation of residual methanol in stream 23, which is mixed with the crude methanol 17. Wash water 62 enters the upper part of the column. Does not contain methanol purge gas obtained at the top of column 22, is first heated in the low temperature heater 24, receiving stream 25, which, in the choice process in the separator 26, for example, the membrane separator. To regulate the flow through the separator 26 is also provided a bypass 27.

From the separator 26 extends thread 28 with a high content of CH4, which is recycled to the conversion section, and the flow of 29 prepared by the purge gas, which is also heated by heat transfer through the wall in another capacitor 30. Then, the purge gas 31 at the outlet of the condenser 30 is heated in the heater 32 purge gas to the respective high temperature, preferably at least 200°C. the Heated purge gas 33 extend in the expander 34, connect nom with generator 35. The expander 34 preferably is a multi-stage expander. After this extended purge gas 36 at the exit of the expander 34 return as fuel for the partition of the conversion.

In one embodiment of the invention (figure 1) heater 32 purge gas is made in the form of a coil in the convection section of the device of the conversion in the conversion section, which produces synthesis gas 1. The purge gas 31 passing in the tube area of the coil is heated by heat exchange through the wall of the flue gas 40 device of the conversion.

In another embodiment of the invention (figure 2) heater 32 purge gas heat hot water vapor. As can be seen from the figures, the part 51 is included in the turbine 4 threads 50 of the hot-water high-pressure steam can be discharged into the heater 32 or, optionally, a stream of 53 water vapor medium pressure could be taken from the turbine 4, for example, on the output side of the first or intermediate stage. Or stream 51 high pressure, or flow 53 medium pressure flow 54 of hot water vapor, which is podogrevatelja purge gas. Water vapor 54 exits the heater 32 purge gas and condensate 55. For heat transfer between the steam 54 and the purge gas 31 you can use any suitable heat exchanger; a preference for the equipment variant of the invention, the purge gas 31 is preferably served in the annular zone shell-and-tube heat exchanger device.

The advantage of carrying out the invention with the use of steam for heating, as described above, is that the operation of the heater 32 gas largely depends on the device of the conversion.

It should be noted that up to the stage of heating in the heater 32 can prepare purge gas 20, for example, removing water, carbon oxides and impurities. Preparation of exhaust gas can be carried out in the separator 26 and / or other equipment. The advantage of preparing the exhaust gas is a reduction in heat rate. For example, heated untrained purge gas with the usual percentage of methane, co and CO2requires approximately 1078 kcal/h to kW, while the purge gas not containing SN4and oxides of carbon, would require about 980 kcal/h to kW.

The invention achieves the above goal the improvement of the energy balance of the installation. In the normal case, get energy savings of about 3.0 percent. Energy consumption can be defined in units: energy consumption (calorific value of raw materials) received tons of methanol. In the illustrative installation with a capacity of 5000 MTD heated purge gas to 360°C and the extension in the expander reduces the flow from 7.44 Gcal/t to 7,31. Heated purge gas up to 500°C by heat exchange with waste is Asim gas main unit conversions even reduces this figure to 7.257.

Example 1

The system produces approximately 5000 MTD methanol, the amount of purge gas circuit 20 having a pressure 84,2 bar (abs.) and a temperature of 45°C is the 9513 KMOL/h Molar composition of the purge gas: approximately 80% N2, 15,4% methane and small amounts of nitrogen (2%), carbon oxides, residual methanol (less than 1%) and water vapor.

Residual methanol and methane are removed, respectively, in the column 22 and the separator 26. Does not contain methanol purge gas is heated to 90°With the first capacitor 24 and injected into the separator under pressure 83,7 bar; the stream exiting the separator, optionally heated in the second condenser 30, receiving stream 31 with a temperature of 115°C and a pressure of 39.7 bar, containing 86% of hydrogen and 10.8% methane, plus nitrogen, oxides of carbon and water vapor, the Estimated molecular weight prepared by the purge gas 31 is equal 4,48.

Stream 31 is heated to approximately 500°C. while passing in the coil in the convection section of the primary conversion at the facility. The incoming stream 33 in the expander 34 at a temperature of 500°C and under pressure of 38.7 bar is 8046 of KMOL/h, while the output stream 36 has a temperature of 220°C and a pressure of 3 bars. The generator 35 generates 19775 kW. The motor consumes 9 9000 kW, thus received output electric power of the net 10775 kW.

Example 2

On the th same setup, as in the above example 1, the heater 32 purge gas for heating use superheated steam 54 high pressure with a temperature of 510°C, coming out of the heater 32 in the form of condensate 55 with a temperature of 320°C. the Parameters of the purge gas entering the expander 34 - 363°C and 38,7 bar, while the output is 127°C and 3 bars. Thus, there is a small reduction in the output electric power of the generator 35 to 16119 kW.

1. The method of synthesis of methanol, in which the conversion containing hydrocarbon feedstock, getting fresh synthesis gas (1)containing oxides of carbon and hydrogen, and the reaction between the components of fresh synthesis gas in the synthesis loop (10), obtaining the crude methanol, and in which the purge gas (20)containing hydrogen, away from the synthesis loop, wherein the purge gas is heated by heat recovery in indirect heat exchange with at least one high-temperature source of heat in the above method, adapted for heating the purge gas to a temperature of at least 200°With getting heated purge gas (33), and this heated purge gas, as such, extend in the corresponding expander (34) and based on the extension of the purge gas in the expander gain energy, and as specified vysokotemperaturno is th source of heat using the hot exhaust gas from the conversion process, which is the conversion of raw materials into fresh synthesis gas (1), or the flow of hot water vapor.

2. The method according to claim 1, in which the high-temperature heat source adapted to heat the purge gas to a temperature in the range from 200°C to about 500°C.

3. The method according to claim 1, wherein the purge gas is heated by passing through the coil in the convection section of the primary conversion.

4. The method according to one of the preceding paragraphs, in which the preparation of the purge gas to heating by heat exchange with the use of high-temperature source of heat.

5. The method according to claim 4, in which the purge gas is carried out by separation of the flow (28) with a high content of CH4.

6. The method according to claim 4, in which the purge gas is carried out by separation of the flow with a high content of N2.

7. The method according to claim 1, in which the mechanical energy received from the expander (34), is converted into electrical energy and at least part of this electrical energy is used in the implementation of this method for electric drive and auxiliary equipment, etc. and the rest of this power away to external customers.

8. The method according to claim 7, in which the above-mentioned electricity used to power the electric motor (9), Pref is included in the action of the circulation pump (8) for the synthesis gas in the circuit (10) synthesis.

9. The method according to claim 1, wherein the expander (34) directly connected to the compressor, providing all or most of its power.

10. The method according to claim 9, in which the expander is directly connected to the circulation pump (8) of the synthesis loop.

11. Installation for methanol synthesis, including the conversion section, in which you can implement the conversion containing hydrocarbon feedstock, getting fresh synthesis gas (1)containing oxides of carbon and hydrogen, the circuit (10) synthesis, intended for the conversion of fresh synthesis gas in the crude methanol, and the pipeline (20) purge gas outlet purge gas containing hydrogen from the synthesis loop, characterized in that it further includes:
high temperature recuperating heat heater (32) purge gas constituting the coil in the convection section of the device of the conversion in the conversion section or connected with a source of hot water vapor (51, 53), available on the installation for the production of methanol;
expander (34) for the purge gas, which enters a heated purge gas (33), supplied by a heater (32); and
means (35)adapted to recover energy from the expansion of the heated purge gas (33) in the expander (34).

12. Installation according to claim 11, further comprising a separator (26) for the preparation of prodovol the gas before entry into the heater purge gas.

13. The method of reconstruction of the plant for methanol synthesis, including the conversion section, in which you can implement the conversion containing hydrocarbon feedstock, getting fresh synthesis gas (1)containing oxides of carbon and hydrogen, the circuit (10) synthesis, intended for the conversion of fresh synthesis gas in the crude methanol, and the pipeline (20) purge gas outlet purge gas containing hydrogen from the synthesis loop, characterized in that:
add at least one high-temperature heater (32) purge gas;
provide a means to supply heat to the heater purge gas source (40, 54) heat available for the installation of methanol, and the heat source is the exhaust gas (40) at least one device for the conversion in the conversion section or the flow of hot water vapor;
provide expander (34) for the purge gas and means for feeding the expander heated purge gas (33), supplied by a heater (32); and
provide a means (35)adapted to recover energy from the expansion of the heated purge gas in the expander.



 

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3 cl

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: invention relates to a methanol synthesis method, during realisation of which natural gas and water vapour are fed into a primary conversion section where the two interact to form a gaseous mixture containing CO, CO2, H2 in stoichiometric excess and CH4. Said gaseous mixture containing CO, CO2, H2 in stoichiometric excess and CH4 is fed into a methanol synthesis section where a reaction takes place to produce methanol and the gas stream containing CO, CO2, H2 and CH4 is collected from the methanol synthesis section by blowing. H2 is extracted from the gas stream collected from the methanol synthesis section to obtain a first gaseous phase primarily consisting of H2, and a second gaseous phase containing CO, CO2, H2 and CH4 and essentially not containing H2. The second gaseous phase containing CO, CO2, H2 and CH4 and essentially not containing H2 is then recuperated for use in the conversion process in the primary conversion section. Nitrogen is first removed from natural gas before feeding the natural gas into the primary conversion section. The invention also relates to apparatus for realising the disclosed method.

EFFECT: obtaining end product with high efficiency at low operational and capital expenses and low power consumption.

8 cl, 1 dwg, 1 ex

Methanol synthesis // 2408567

FIELD: chemistry.

SUBSTANCE: present invention relates to a methanol synthesis method involving the following steps: (i) reforming hydrocarbon starting material and separation of water from the resulting mixture with gas reforming to obtain freshly prepared gas containing hydrogen and carbon oxides, where the said mixture with freshly prepared gas has stoichiometric coefficient R defined by the formula: R=([H2]-[CO2])/([CO2]+[CO]), which is less than 2.0; (ii) formation of a mixture of synthetic gas consisting of a stream of said freshly prepared gas, unreacted synthetic gas and hydrogen; (iii) passing the mixture with synthetic gas at high temperature and pressure through a methanol synthesis catalyst bed to obtain a stream of product containing methanol and unreacted synthetic gas; (iv) cooling said stream of product with extraction of a stream of crude methanol from said unreacted synthetic gas; (v) removal of a portion of said unreacted synthetic gas as blowout gas, and (vi) feeding the remaining unreacted synthetic gas to step (ii). Hydrogen is extracted from at least a portion of said blowout gas and a portion of said freshly prepared gas and the extracted hydrogen is added to the mixture with synthetic gas.

EFFECT: disclosed method lowers volume of catalyst and amount of wastes, reduces size of reactors and simplifies purification of crude methanol, which lowers cost of the process.

12 cl, 3 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: method of preparing a mixture of hydrogen and carbon monoxide from a gaseous mixture of hydrocarbons containing methane, ethane and optionally hydrocarbons with a large number of carbon atoms involves the following steps: (a) preliminary reforming of the mixture of hydrocarbons in the presence of a suitable reforming catalyst with conversion of ethane and optionally hydrocarbons with a large number of carbon atoms to methane, carbon dioxide and hydrogen, (b) heating the gaseous mixture obtained at step (a) to temperature of 750-900°C, (c) partial oxidation by bringing the heated mixture obtained at step (b) into contact with an oxygen source in the burner of the reactor to obtain a reaction stream. The mixture of hydrogen and carbon monoxide obtained at step (c) is used at step (d) for Fischer-Tropsch synthesis, in which gas containing hydrogen and carbon monoxide obtained at step (c) is converted at one or more steps at least partially to liquid hydrocarbons in the presence of a Fischer-Tropsch type catalyst which contains at least one metal or a metal compound selected from group eight of the periodic table of elements.

EFFECT: invention reduces oxygen consumption.

10 cl, 2 dwg, 4 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: claimed is method of obtaining ethylene copolymers in high pressure reactor with, at least, two spatially separated points of initiator introduction by ethylene polymerisation and, possibly, additional monomers in presence of, at least, two different mixtures of free-radical polymerisation initiators at temperature from 100°C to 350°C and pressure in the range from 160 MPa to 350 MPa, in which method contains the following stages: a) at least, two different initiators are supplied in form of solution in acceptable solvent or in liquid state, b) initiators and, possibly, additional solvents are mixed in at least two stationary mixers and c) each of mixtures is supplied to different points of initiator introduction of high pressure reactor, and installation for supply of initiator mixtures into high pressure reactor with at least two spatially separated points of initiator introduction.

EFFECT: invention makes it possible to find reliable and flexible method of dosed supply of various initiator mixtures into high pressure polymerisation reactor.

15 cl, 2 dwg

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