The way co-production of ammonia and methanol, the installation for implementing the method, the way of modernization installation of ammonia synthesis

 

(57) Abstract:

The invention relates to a method and installation for the combined production of ammonia and methanol, as well as to upgrade the installation of the ammonia synthesis to ensure such co-production. The way co-production of ammonia and methanol are carried out by the sequential scheme in section synthesis of methanol from a gas stream, comprising monoxide, carbon dioxide and hydrogen, at a pressure of 50-100 bar, and in section synthesis of ammonia, which comes free of methanol gas flow generated after the separation of methanol, and the steam flow at high or medium pressure and at a temperature of 100-300oC. plant for combined production of ammonia and methanol sequentially includes a secondary reforming section, the high temperature section and a section of low-temperature conversion of carbon monoxide and section synthesis of ammonia, which is connected with the low-temperature section. Unreacted gas stream from section synthesis of methanol to the feed section of the low-temperature conversion of carbon monoxide predominantly saturated with fluid flow, including water heated through indirect heat exchange substance, free water from the gaseous stream from stage cooling and water separation. Upgrade installation of ammonia synthesis is designed for installation of joint production of ammonia and methanol, and in the known installation impose additional section of the cooling and separation of water contained in the gaseous stream from the secondary reforming section. This provides for the supply section of the low-temperature conversion of carbon monoxide stream comprising carbon monoxide, carbon dioxide, hydrogen and water. The methanol synthesis is done according to the scheme "in one pass". The technical result - the simplification of the technological design process, reducing capital costs. 3 S. and 11 C.p. f-crystals, 1 Il.

The invention relates to a method for joint production of ammonia and methanol at the facility, including the secondary section of the reformer, a high temperature section maturing and section of the low-temperature transformation, set in rows, and the section of the ammonia synthesis, this method involves the following stages:

trapping gaseous flow comprising CO, CO2N2and N2On emerging from the specified secondary section of the reformer;

supplying gaseous stream with theOh, contained in it, in the specified section of the cooling and separation of H2O;

supplying gaseous stream essentially free of H2On emerging from the specified section of the cooling and separation of N2On the section of methanol synthesis;

interaction specified gaseous stream essentially free of H2O, in the specified section of the synthesis of methanol production;

feeding a gaseous flow comprising CO, CO2N2and CH3HE's coming out of the specified partition of the methanol synthesis section of the separation of methanol;

separation of the liquid stream containing methanol, essentially free of methanol gaseous flow comprising CO, CO2and H2in the specified partition separating methanol;

submission specified gaseous stream essentially free of methanol, leaving the specified partition separating methanol, specified low-temperature section maturing.

The present invention relates also to an apparatus for combined production of ammonia and methanol for carrying out the above method and to a method of upgrading your installation of ammonia synthesis.

As you know, there is a growing poranenii, which allow to achieve the desired performance at low production costs and capital investment and lower energy consumption.

The prior art.

To meet the above requirements has recently been proposed a joint venture in the field of synthesis of ammonia and methanol, where the flow of gas enriched in CO, CO2and H2emerging from the secondary section of the reformer installation of ammonia synthesis, is given in section condensing and separating water contained in it, and then sent to the section of the synthesis of methanol production. Unreacted gas successively re-enter the bottom section of the high-temperature transformation WITH the installation of ammonia production.

Although in some sense the advantages of the place, the above methods have some disadvantages, the first of which is that unreacted gaseous stream exiting the section of methanol synthesis before it will be returned in the method of synthesis of ammonia, mixed with the steam flow at high or medium pressure, bringing the temperature and the concentration of H2About up to this size to facilitate subsequent prevrasheniya, resulting from the implementation of a process of co-production of ammonia and methanol in accordance with the previously known methods are those that eliminate the benefits arising from the use of gas that is present on the installation of ammonia to methanol production.

Besides, in the above method, the methanol produced in the reaction section, including synthetic loop, at a pressure typically between 50 and 100 bars, which is essentially higher than the pressure present in the secondary section of the reformer installation of ammonia production.

For this reason, the installation for carrying out the method according to the previously known in this area requires special equipment for recycling unreacted gas to synthetic reactor and to compress the gas flow coming from the secondary section of the reforming process, including, therefore, considerable structural complexity and high capital investment.

Summary of invention.

The problem underlying the present invention lies in the fact that there is a process of co-production of ammonia and methanol, which will be simple in execution AMI in manufacturing in addition to low power consumption.

The above-mentioned problem is solved according to the present invention by way of joint production of ammonia and methanol aforementioned type, which is characterized by the fact that it includes a step feed essentially free of methanol gaseous flow coming from the section of the separation of methanol from the liquid stream containing H2Oh, accordingly heated through indirect heat exchange with gaseous flow coming from the secondary section of the reformer.

Mainly it is possible to achieve effective water saturation and temperature control, essentially free of methanol gaseous stream that is directed into the low-temperature section of transformation through the use of indirect heat gaseous flow coming from the secondary reformer.

Thus, avoids the use of external energy sources in the process of co-production of ammonia and methanol, such as, for example, in the link previously known techniques, the introduction of water vapor, and therefore significantly reduces the consumption of energy.

Preferably the temperature of the liquid stream comprising H2Oh, supplied in essentially free from metrogo in the method of synthesis of ammonia, is this to avoid reactions of transformation in low-temperature section maturing.

In addition, in accordance with a particular preferred variant of the method according to the present invention a liquid stream containing H2O comes at least partly from the cooling and separation of H2O.

In this form of the method according to the present invention allows to allocate and use water obtained by condensation in the cooling section from the separation of N2On the upper-stream section of the synthesis of methanol by recycling it to the unreacted gaseous stream before it will return to the method of synthesis of ammonia.

Therefore, the concentration of H2About in the gaseous stream fed to the low-temperature section of the maturing, can mainly be controlled by limiting or even eliminating the need to add water from the outside in a way co-production of ammonia and methanol, thereby simplifying installation and reducing costs and capital investment and energy consumption.

Predominantly gaseous stream free, essentially, from H2Oh, reacts in section synthesis for the production of methanole, significantly lower capital investment compared to the installation, secure the reactionary section of methanol, including synthetic loop of the type described, with reference to the prior art.

In the following description and the attached claims the term: section synthesis of the type carried out in one pass" is understood as a reaction section in which unreacted resulting stream is not recyclized in the synthesis reactor.

For carrying out the above method, the present invention mainly makes available the installation of combined production of ammonia and methanol, including:

the section of the secondary reformer, a section of high pressure maturing and low-temperature section of the maturing, set in rows;

section synthesis of ammonia in liquid communication with the low temperature section maturing;

the cooling section and the separation of N2Oh, contained in the gaseous stream exiting the specified secondary section of the reformer, and including CO, CO2and H2;

section synthesis for the production of methanol feed essentially free of H2O gaseous flow coming from the specified section to the cooling of the specified partition of the methanol synthesis, for separating the liquid stream comprising methanol from a gaseous stream essentially free of methanol and including CO, CO2and H2;

section saturation of H2For this, essentially free of methanol gaseous stream in liquid communication with the low temperature section maturing;

which is characterized by the fact that it includes a heating section for fluid flow, including H2Oh, for indirect heat exchange with the specified gaseous flow coming from the specified secondary section of the reformer in fluid communication with the specified section of saturation.

In accordance with another aspect of the present invention is also an affordable way of upgrading your installation of ammonia synthesis of this type, which includes the secondary section of the reformer, a high temperature section maturing and low-temperature section of the maturing, set in rows, and the section of the ammonia synthesis, the method comprising the stage of:

ensure the cooling and separation of N2O contained in the gaseous stream exiting the specified secondary section reforming and including CO, CO2and H2;

ensure secceeded from the specified section and cooling section of the division of N2ABOUT;

ensure the section of the separation of methanol supplied gaseous flow coming from the specified partition of the synthesis of methanol to separate a liquid stream comprising methanol from a gaseous stream essentially free of methanol and including CO, CO2and H2;

ensure the section of saturation of the H2For this, essentially free of methanol gaseous stream;

ensure the section of heat fluid flow, including2O, for indirect heat exchange with the specified gaseous flow coming from the specified secondary section of the reformer;

providing connecting means between the specified section of the heat and the specified section of saturation for flow of fluid, comprising respectively heated H2About in the specified partition saturation;

providing connecting means between the specified section of saturation and the specified low temperature section for filing in the above section, the transformation FROM a gaseous stream containing CO, CO2and H2and H2O.

Due to this way of upgrading an existing installation of ammonia synthesis becomes possible to conduct the process of joint and low production costs and capital investment and low energy consumption.

Characteristics and advantages of the present invention arise in future from the description of its options below as an example and not limiting of the invention, with reference to the attached drawing, which shows a block diagram of the process of co-production of ammonia and methanol according to the present invention.

A detailed description of the preferred option.

The drawing shows a block diagram illustrating the stages of the process of co-production of ammonia and methanol in accordance with the present invention.

Reference number 10 indicates generally a portion of a block diagram, illustrating manufacturing process steps of the ammonia.

In this part 10 blocks 11-17 indicate, respectively, on the primary section of the reformer and the secondary section of the reformer and a high temperature section maturing, low-temperature section maturing, the section of the Department of CO2the section holding the methanolysis and the section of the ammonia synthesis.

Blocks 11-17 intersect a flow line 1 representing the gaseous stream with a composition that changes when passing through different reaction section.

For example, at the entrance to the primary section of OC on the exit section of the synthesis of ammonia, represented by block 17, it includes mainly ammonia.

Working conditions in the production process of ammonia as this is the sort of reactions that take place during the passage of the gaseous flow through the different sections are the usual conditions of high temperature and pressure plant producing ammonia, well-known specialist in this field and is therefore not described further.

Reference 20 indicates generally a portion of a block diagram, illustrating manufacturing process steps of methanol.

In this part of the 20 blocks 21-25 indicate respectively the cooling section section division H2Oh, the partition of the methanol synthesis, the section of the separation of methanol and the section of the water saturation unreacted gaseous stream essentially free of methanol.

Line 2 stream is a gaseous stream coming from the line 1, leave the secondary section of the reformer shown by block 12, and including CO, CO2N2and H2O.

Production line 2 crosses the cooling section is represented by block 21, where most of the vapor contained in the gaseous stream is condensed and fed into the section of the division of N2O shows a block CO2and H2.

Production line 3 crosses the section of methanol synthesis, represented by block 23, where part of the reagents contained in the gaseous stream interacts with the formation of methanol and served in the partition separating shown side 24, which is separated unreacted gas stream comprising CO, CO2and H2from methanol.

The line 6 specifies the thus obtained stream of methanol, while the line 5 represents unreacted gaseous stream essentially free of methanol, which is fed into the section of saturation represented by block 25.

Mainly at the inlet of the block 25 is also fed production line 4 fluid stream comprising H2Oh, which was preheated in the block 21 through indirect heat exchange with gaseous flow coming from the secondary section of the reformer.

As shown in the drawing, the flow coming out of the block 25, which represents a section of saturation unreacted gaseous stream essentially free of methanol, leads the conveyor line 7 gaseous stream containing CO, CO2and H2and H2Oh, who served back in the conveyor line 1 sposoby block 25 is also given to the line 8 of the fluid flow, including H2O, which is recycled in the production line 4 upstream of the block 21.

According to the method of the present invention a gaseous flow comprising CO, CO2and H2and H2O, is removed from the secondary section of the reforming process (block 12) and is fed into the cooling section (block 21) and section separation2O (block 22). Here the gaseous stream is cooled and the contained water is separated. Gaseous stream essentially free of H2Oh, is drained from the cooling and separation of N2Oh and then served in the partition synthesis (block 23) methanol, where it reacts in order to turn into methanol. The gaseous stream leaving sections of the synthesis of methanol, and then is fed into the section of the separation of methanol (block 24) for separating the liquid stream comprising methanol from a gaseous stream essentially free of methanol, including CO, CO2and H2that in turn is fed into the section conversion WITH low pressure (block 14).

Mainly in accordance with another phase of the present method, the liquid stream comprising H2Oh, accordingly heated through indirect heat exchange of the gas stream leaving the secondary section Ref is Nola.

Operating in this manner, at least part of the heat of the gas stream leaving the secondary reformer, mostly returned with saturation in N2O and heating the gas stream, which moves in the low-temperature section maturing.

In the example shown in the drawing, the heated fluid stream comprising H2Oh, occurs in the cooling section indicated by block 21.

Preferably the fluid flow, including H2Oh, filed in section saturation (block 25), pre-heated according to the present invention to a temperature between 150 and 280oWith so as to bring the temperature of the gaseous stream essentially free of methanol, which will be fed back into the process for the synthesis of ammonia, until such values, to contribute to the successful transformation FROM. These values are usually between 180 and 250oC.

In specific and preferred embodiment of the method according to the present invention, but not shown here, the liquid stream comprising H2Oh, respectively subjected to compression before being heated and undergoes after heating stage expansion to achieve flash-evaporating part of the H2Oh, SS="ptx2">

Operating in this manner, fluid flow, which is fed into the section of saturation (block 25), consists mainly of steam at high temperature, which facilitates the feeding of the water and the heated gaseous stream leaving the section of the separation of methanol (block 24).

Predominantly liquid stream comprising H2Oh, outgoing from block 22, is compressed to a pressure between 20 and 100 bars, and preferably 60 bar.

In an alternative and particularly advantageous variant of the method according to the present invention, the liquid stream comprising H2Oh, leaves, at least part of the cooling sections and sections of division H2On (blocks 21 and 22).

In the drawing, the alternative seems to be intermittent flow line 4'.

Operating in this manner, it becomes possible to use the2Oh, contained in a gaseous stream, passing from the secondary section of the reformer, respectively condensed and separated in the upper stream section of methanol synthesis, for saturation of unreacted gaseous stream essentially free of methanol to be fed back to the mode of production of ammonia.

The chilled section is e, part of the H2Oh, contained in the gaseous reactants before the reaction occurs synthesis, to prevent the action of H2About (reaction product) as an inhibitor reaction conversion and enrich gazoobraznye the flow of water, which is fed back into the method for the synthesis of ammonia to facilitate reaction conversion.

Thanks to the present invention, it becomes possible to carry out the feeding of the gaseous stream, which is fed into the section maturing through direct use of pre-obtained H2O in the cooling and separation of N2O.

In an alternative method according to the present invention, the liquid stream comprising H2Oh, served in a gaseous stream essentially free of methanol, completely away from the cooling and separation of N2Oh, eliminating thus the need to use a saturation flux supplied from the outside.

According to the present invention a gaseous stream essentially free of methanol, leaving sections of division indicated by block 22, interacts in section synthesis for the production of methanol (block 23), comprising mainly the reactor and methanol, known in this area that use section of methanol synthesis types including synthetic loop, the present invention eliminates all the piece of equipment that is associated with recycling in synthetic reactor, at least part of the unreacted gaseous components, thus significantly reducing capital investment and energy consumption.

In an alternative process of the present invention not shown, it becomes possible to provide a section of methanol synthesis (block 23), including many reactors of the type carried out in one pass, placed in series to achieve a high degree of conversion of gaseous reactants. This option is especially suitable in cases where there is a requirement for large quantities of methanol.

Section division of methanol, represented in the drawing by the block 24, to separate unreacted gas stream from a stream of produced methanol is usually provided by the vessel for separation, in which the gas is cooled to respectively of room temperature by condensation of the methanol contained therein.

Mainly the pressure used in the synthesis process metadee process for producing methanol according to the present invention is mainly between 20 and 50 bars.

In fact, it was found that it is possible to obtain a satisfactory conversion section for methanol synthesis (block 23), even when working with a pressure similar to the pressure stage of the production process of ammonia.

Operating in this manner, the apparatus for carrying out the process can be further simplified with the reduction of operating costs and capital investment and energy consumption, as in this case, it is not necessary to use a compressor, as it was used in the process of co-production of methanol and ammonia in accordance with the prior art.

Finally, according to the method of the present invention, the gaseous stream leaving the secondary section of the reformer is cooled in the cooling section (block 21) to a temperature preferably below the 50oC.

It was found that below this temperature there is almost complete condensation of the steam contained in the gaseous stream passing from the secondary section of the reforming process (block 12), with relief subsequent stages of the synthesis of methanol (block 23) and in the case of at least partial return of the condensed water, the water saturation (block 25) a gaseous stream essentially free of metal is Miaka and methanol, easy implementation, low cost and investment and low energy consumption.

With reference to the drawing, the installation of combined production of ammonia and methanol includes the partitions specified blocks 11-17 and 21-25.

Primarily installation according to the present invention also provides a section for heating a liquid stream comprising H2O, by indirect heat exchange with a liquid stream comprising H2Oh, before filing it in the gas stream essentially free of methanol.

In the drawing section, as indicated by block 21 also performs the function of heating the liquid stream containing H2Oh, before filing it in a gaseous stream essentially free of methanol.

Section cooling or heating block (21) may exclude one or more heat exchangers arranged in a row, and the upper thread section of the division of N2On (block 22) to remove due to the indirect heat exchange with a flow of coolant, including H2Oh, at least part of the heat present in the gas stream passing from the secondary section of the reforming process (block 12) of the process of synthesis of ammonia, thus, to achieve condensation of the steam contained the situation according to the present invention also includes the corresponding connecting means (conveying line 4'), to make liquid communication between the section of the division of N2Oh and by the heating section so as to permit the use of at least part of the H2O contained in a gaseous stream, passing from the secondary section of the reforming process (block 12), to saturate the unreacted gas stream, which is returned in the section of low-temperature transformation (block 14).

Section 23 synthesis for the production of methanol is predominantly a section of the type carried out in one pass".

With reference to the method of upgrading an existing installation of ammonia synthesis according to the present invention,it is important to note that at least part of the gaseous stream leaving the secondary reformer and rich in CO, CO2and H2can be advantageously used for production of commercial value, such as methanol, with relief at the same time sections of transformation and separation of CO2installation of ammonia production.

In accordance with the various stages of this upgrade to install synthesis of ammonia, provided the cooling section (block 21) and section separation (block 22) for the water contained Wei section synthesis for the production of methanol (block 23) is supplied in a gaseous stream, essentially free of H2O leaving the cooling and separation of N2The acting is section of the separation of methanol (block 24) supplied gaseous stream leaving the section of the synthesis of methanol, to separate a liquid stream containing methanol from a gaseous stream comprising CO, CO2and H2essentially free of methanol, which is saturated with water in an appropriately secure sections of saturation (block 25).

Mainly is also provided a heating section (block 21) for fluid flow, including H2O, for indirect heat exchange with the gas stream leaving the secondary section of the reforming process (block 12), and connecting means between the heating section and section saturation (flow line 4).

Finally, between the section of saturation and a low temperature section maturing (block 14) are the connecting means (continuous line 7) for submission to the section turning WITH a gaseous flow comprising CO, CO2and H2and H2O.

In a particularly preferred variant of the preferential way of modernization in accordance with the present invention also includes a step of connecting location at the last of the fluid flow, including H2O.

From the above it is clear numerous advantages achieved with the present invention. In particular, it provides a method for simultaneous production of ammonia and methanol, simple in execution, is able to achieve the desired performance of the synthesis of methanol and ammonia at low cost and capital investment and low energy consumption.

1. The way co-production of ammonia and methanol at the facility, including the secondary reforming section, the section of the high-temperature conversion of carbon monoxide, the section of the low-temperature conversion of carbon monoxide, located in the series section of methanol synthesis and the section of the ammonia synthesis, characterized in that the catch gaseous stream containing carbon monoxide, carbon dioxide, hydrogen and water coming out of the specified secondary reforming section, serves a specified gas flow in the cooling section and the division of water, cooled specified gaseous stream and separate water, serves essentially free from water gas flow in the section of methanol synthesis, serves gaseous stream containing carbon monoxide, carbon dioxide, hydrogen and metanational, from essentially free of methanol gaseous stream containing carbon monoxide, carbon dioxide and hydrogen, in the specified partition separating methanol fed indicated, essentially free of methanol gaseous flow coming from the specified partition separating methanol, specified low-temperature section of the conversion of methanol is injected into the specified essentially free of methanol gaseous flow coming from the specified partition separating methanol, a liquid stream comprising water, respectively heated through indirect heat exchange with the specified gaseous flow coming from the secondary reforming section.

2. The method according to p. 1, characterized in that the liquid, including water, in the gas stream essentially free of methane, served at a temperature of from 100 to 300oC.

3. The method according to p. 1, characterized in that, in addition to heating the stream comprising water by indirect heat exchange with the gaseous flow coming from the secondary reforming section, carry out the compression of the specified fluid flow with a subsequent extension of the specified fluid flow to the specified feeding into the gaseous stream essentially free of methanol for dostigeniyu fluid is compressed up to the pressure of the stream from 20 to 100 bar.

5. The method according to p. 1, characterized in that the fluid flow at least partially deviates from the specified section of the cooling and separation of water.

6. The method according to p. 1, characterized in that said gaseous stream essentially free from water, interacts in section synthesis of methanol type carried out in one pass".

7. The method according to p. 1, characterized in that the specified partition of the methanol synthesis using a pressure of from 20 to 50 bar.

8. The method according to p. 1, characterized in that the gaseous stream coming from the specified secondary reforming section, is cooled in the specified section of the cooling and separation of the water to a temperature below the 50oC.

9. Installation for the combined production of ammonia and methanol, comprising the secondary reforming section, the section of the high-temperature conversion of carbon monoxide, the section of the low-temperature conversion of carbon monoxide, arranged in a row, the section of methanol synthesis and the section of the ammonia synthesis, characterized in that it further comprises a cooling section and the separation of water contained in the gaseous stream exiting the specified secondary reforming section and comprising monoxide from the from the specified partition of the methanol synthesis, designed to separate liquid stream comprising methanol, and gaseous stream essentially free of methanol and containing carbon monoxide, carbon dioxide and hydrogen, section saturation water specified gaseous stream essentially free of methanol, United by a liquid stream with specified low temperature section of the conversion of carbon monoxide, and the heating section liquid stream containing water by indirect heat exchange with the specified gaseous flow coming from the specified secondary reforming section and the heating section of the fluid flow in the liquid flow connected with section saturation, the section of the ammonia synthesis connected with the low temperature section of the conversion of carbon monoxide and the specified section of methanol synthesis feed essentially free from water gaseous flow coming from the specified partition cooling and water separation.

10. Installation under item 9, characterized in that it further comprises a connecting means located between the cooling section and the separation of the water and the heating section, and specified the connecting means is arranged to feed into the heating compartment, the flow of the Intesa methanol type carried out in one pass".

12. Upgrade installation of ammonia synthesis, aimed at obtaining plants for combined production of ammonia and methanol, and specified the installation of ammonia synthesis includes a secondary reforming section, the section of the high-temperature conversion of carbon monoxide and a section of low-temperature conversion of carbon monoxide, located in the series section of the synthesis of ammonia, characterized in that in the known installation impose additional section of the cooling and separation of water contained in the gaseous stream exiting the specified secondary reforming section and containing carbon monoxide, carbon dioxide and hydrogen, section synthesis of methanol supplied from a gaseous stream essentially free of water, released from the specified section of the cooling and separation of the water, the sections of the separation of methanol supplied gaseous flow coming from the specified partition of the methanol synthesis with receiving a fluid stream containing methanol, and gaseous stream comprising carbon monoxide, carbon dioxide and hydrogen and essentially free of methanol, section saturation water specified gaseous stream essentially free of methanol, heating section potim from the specified secondary reforming section, the connecting means between the specified section of the heat and the specified section of saturation, is arranged to feed fluid stream containing the heated water in the specified partition saturation, and connecting means between the specified section of saturation and the specified section of the low-temperature conversion of carbon monoxide, executed with a possibility of a specified section of the low-temperature conversion of carbon monoxide gaseous stream containing carbon monoxide, carbon dioxide, hydrogen and water.

13. The method according to p. 12, characterized in that impose additional connecting means between the said cooling section and the separation of the water and the specified heating compartment, made with the possibility of filing in the last stream of liquid, including water.

14. The method according to p. 12, characterized in that the used section of methanol synthesis type carried out in one pass".

 

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