Method of ammonia production and superheater

FIELD: chemistry.

SUBSTANCE: ammonia is produced from synthesis-gas, obtained as a result of reforming hydrocarbon raw material. Partially reformed gas, after stage of primary reforming, passes through stage of heat-exchange reforming and stage of secondary reforming. Partially reformed gas at the stage of heat-exchange reforming is reformed by indirect heat-exchange with synthesis-gas, removed from stage of secondary reforming. All steam, produced in steam recovery boilers of reforming and at enterprise sector of ammonia production, is heated in one or more superheaters, located behind ammonia converter of enterprise sector of ammonia production.

EFFECT: invention makes it possible to improve thermal integration of ammonia obtaining process, reduce predisposition to metal dusting, nitration and stress corrosion in steam recovery boilers and superheaters of enterprise.

9 cl, 2 dwg

 

This invention relates to a method of production of ammonia from a hydrocarbon feedstock with improved heat integration, where hydrocarbons initially using prereforming is converted into synthesis gas, and then the synthesis gas is converted into ammonia. The invention also relates to a new superheater, suitable in particular for use in large ammonia plants with a capacity of at least 2,000 tons per day (MTPD).

Traditional enterprises for the production of ammonia is usually divided into two main sections: the section of the reforming process in which a hydrocarbon feedstock, such as natural gas, is converted into synthesis gas, a mixture of carbon and nitrogen under pressure in the range from 30 to 80 bar, often 30-40 bar, and the site of synthesis of ammonia, in which the synthesis gas (synthesis gas for ammonia production), with the correct ratio of hydrogen and nitrogen and, after compression up to 120-200 bar, catalytically convert into ammonia, which is then condensed by cooling.

On the section of the reformer, when using the traditional technological schemes with primary Autoterminal, or secondary reformer furnaces containing hydrogen synthesis gas is produced at high temperatures, for example, at 1000C or higher. Produced in said furnace reformer synthesis gas must be cooled, andit is usually carried out by passing the gas through a series of steam waste-heat boilers and superheaters. These machines are expensive and very complex heat exchangers that must be carefully calculated to minimize the risks related to the failure mechanics and materials related to metal dusting, hydrogen corrosion and corrosion under tension. In particular superheaters at the site of the reforming process are costly installations, in which, despite great care in their design work, it is difficult to prevent metal dusting. When applied to the area of reforming superheaters metal dusting almost fatal.

At the site of synthesis of ammonia is produced catalytically from a mixture contained in the synthesis gas of hydrogen and nitrogen. Conversion to ammonia occurs when the production of heat, which is utilized in boilers and, optionally, in the superheaters, to produce high-pressure steam, which is then used to drive compressors for ammonia synthesis shop. Steam waste heat boilers and superheaters at the site of synthesis of ammonia are also expensive and very complex heat exchangers, which are carefully calculated to minimize the risks related to the failure mechanics and materials associated with hydrogen nitride corrosion and corrosion under tension. Steam recovery boilers in which lastnosti exposed nitride corrosion, because these plants are usually installed after the ammonia Converter.

Metal dusting, corrosion under tension and nitride corrosion are catastrophic, or at least serious types of corrosion, which should be excluded by appropriate calculations and material selection. Metal dusting is generally the case in the presence of carbon monoxide in the gas which is in contact with the metal, and when the temperature of the metal is so low, usually from 400C to 800C, in particular from 500C to 750C, the interaction with the gas leads to the disintegration of the metal fine particles.

The nitriding of the metal occurs when the nitrogen from the gas in contact with the metal diffuses into the material of metal and forms nitrides. A solid surface layer, which splits easily and during the worst of the cracks continue inside the metal. Thus, the materials subjected to nitriding, become more susceptible to crumbling. The thickness of the nitride layer depends on temperature, time, and metal alloy. In General, it is known that metal temperatures above about 380C for thin metal sheets and above approximately 400C for thick metal sheets of low-alloy carbon steel significantly increases the susceptibility of the metal to azotirovannye higher temperatures necessary materials such as stainless steel or Inconel (Inconel).

Stress corrosion is a risk when austenitic materials such as stainless steel, come in contact with water, particularly when water contains impurities, for example, chlorine. When applying low-alloy steels the risk of stress corrosion is much lower.

Since the capacity of enterprises for the production of ammonia has been steadily increasing at the expense of enterprises, designed for a production capacity of up to 2000, 3000, 5000 tons of ammonia per day, or even more, the development of superheaters more and more power has become a difficult task. On such large enterprises for the production of ammonia problem is the size of the superheaters, because according to the standard calculation of the diameter and thickness of the tube plates superheaters become so large that their production is technically or economically impractical.

This trend for the construction of more powerful enterprises leads to the need to ensure the drive compressors enterprise ferry. It requires a higher pressure for steam and thus higher temperatures. In order to cope with higher temperatures, for superheaters should be applied expensive materials, such as stainless steel or Inconel.

In U.S. patent No. 4,213,95 described method for the production of ammonia, contains the plot of reforming and ammonia synthesis shop. Both plots share a conventional steam drum, which serves as a steam separator for steam recovery boilers at the site of reforming and ammonia synthesis company. Produced thereby on the site of the steam reforming process used at the site of synthesis of ammonia, while the process gas from the secondary reformer furnace is cooled by passing through the system not only steam waste-heat boilers, but also superheater. For utilization of the energy of the steam is also used in the expanders.

In U.S. patent No. 4,545,976 described method for the production of ammonia synthesis gas by reforming hydrocarbon by removal of the reduced pair, while the process gas from the furnace secondary reformer is cooled by applying a number of superheaters.

Our European patent application EP-A-1,610,081 discloses a heat exchanger for use directly after stage reforming process. The heat exchanger contains a first cooler, a heating zone comprising a bundle of tubes of low-alloy steel, and a second, more hot, the heating zone containing a tube bundle made of heat-resistant and corrosion-resistant alloy, for example, austenitic alloy, Nickel/chromium/iron". Steam is passed through line space of the heat exchanger, and the converted g is C (synthesis gas) in the annular space. More cold and more hot heating zones are connected in series in relation to the flow of steam and the flow of the converted gas.

The objective of the invention is to provide a method of ammonia production with improved heat integration and reduced susceptibility to metal dusting, nitriding and stress corrosion in boilers and, in particular, in the superheaters of the company.

Another object of the invention is to provide a method for production of ammonia with improved heat integration, with the removal of the reduced pair, and which is much more cost-effective known methods.

The next task of the invention is to provide a method that was both robust and less sensitive to the stops of the enterprise on a plot of ammonia.

Another object of the invention is to develop a superheater, suitable for use on large ammonia plants, which also resists corrosion, in particular the nitriding and stress corrosion.

These and other problems are solved by the present invention.

As the first object we propose a method for the production of ammonia from hydrocarbons containing the following steps:

(a) passing the hydrocarbon feedstock through a section of the reformer and the lead synth is C-gas of the above-mentioned section of the reformer;

(b) passing the said synthesis gas through one or more steam boilers steam generators without the use of the superheater, in which the synthesis gas is in indirect heat exchange with steam-water mixture, the lead pair of the above-mentioned heat-recovery boilers and the direction mentioned a couple in one or more steam drums;

(c) passing the cooled stage (b) synthesis gas through a stage of transformation, for the conversion of carbon monoxide in the synthesis gas into hydrogen, and then through the flotation process to remove remaining in the synthesis gas, carbon dioxide, carbon monoxide and methane, and removing synthesis gas containing nitrogen and hydrogen;

(d) transmittance obtained in step (C) of the synthesis gas through the section of the ammonia synthesis, which involves the catalytic conversion of synthesis gas to ammonia by passing through one or more catalytic layers in an ammonia Converter and removing the process gas containing ammonia, one or more catalytic layers;

(e) transmission mentioned process gas containing ammonia, through one or more superheaters, which overheat the steam from one or more steam drums, stage (b), and removing a stream of superheated steam from the aforementioned one or more superheaters;

(f) passing the cooled is thus at stage (e) of process gas through one or more steam boilers-steam generators in which process, the gas is in indirect heat exchange with steam-water mixture, removing a pair of these one or more steam recovery boilers and conduct of said pair to one or more steam drums of step (b).

As a result, the steam produced in waste heat boilers steam in step (b) and step (f) overheat in one or more superheaters at the step (e). Thus, as far as possible, the cooling is carried out at the site of synthesis of ammonia.

We found that by combining one or more superheaters for ammonia Converter, which is designed for cooling the ammonia process gas and overheating just steam produced in the HRSG section of the steam reforming process, it is possible to provide a simpler and less expensive design otherwise demand in the area of steam reforming of waste heat boilers and steam boilers heat recovery steam generators and in particular of the superheater(s) at the site of synthesis of ammonia enterprise. Accordingly, the invention has the essential advantage that for heating the synthesis gas is not necessary in the superheater heating the process gas superheater), or simply, in the superheaters in the area of reforming the enterprise for cooling the generated C the MES-gas.

The cooling capacity is essentially transferred from the site reforming of enterprises in the area of synthesis of ammonia. Thus, completely eliminating the risk of metal dusting, which in the application of the superheaters in the area of reforming almost fatal.

Additionally, since the cooling, as far as possible, carried out at the site of synthesis of ammonia, the process of cooling the process gas can be transferred from the ammonia Converter in the superheater, preferably in a heat exchanger in the form of a U-shaped tube at a temperature below about 380C. this eliminates the nitriding set forth steam boiler(s)-exchanger(s). As noted above, the temperature of the metal above about 380C significantly increases the susceptibility to nitriding. When this steam boiler(boilers)heat(s) at the site of synthesis of ammonia, is now cooling the process gas can in this case be designed accordingly in the form of a U-shaped tubular heat exchanger, for example, of stainless steel, thereby eliminating the problems associated with corrosion under tension, requiring otherwise austenitic materials. Thus, by design, in other cases very expensive steam waste-heat boilers and superheaters, can be applied more cheap the materials.

A significant advantage of the invention is that company with the area of reforming and synthesis of ammonia becomes more resistant to emergency shutdown situations in which, for example, the production of ammonia at the site of synthesis of ammonia is stopped, while the plot of the reforming process continues. When traditional technological schemes, where such production stop at the site of synthesis of ammonia, under their influence immediately turns the steam generation at the site of the reforming process. To compensate for this impact is usually significantly overstate the size of the steam boiler for cooling the synthesis gas for the furnace secondary reformer. Using the method according to this invention can reduce such an effect on steam production at the site of the reforming process. Now, in the case of emergency shutdown of the enterprise at the site of synthesis of ammonia, you can balance the steam production at the site reformer and, as a result, there is no need for a substantial increase in the size of the steam boiler(s)-exchanger(s) on this site for the furnace secondary reformer. Thus can be applied to smaller and cheaper steam recovery boilers.

Plot reformer may include the reforming of hydrocarbons in one or more stages, as is customary in proceed. of the local experience. Therefore, the source of the hydrocarbon feedstock may be subjected, for example, the pre-reformer before the primary and secondary reforming, or the original hydrocarbons, such as natural gas, may be filed directly at step autothermal reformer for the production of hot synthesis gas. The synthesis gas is extracted from stage autothermal or secondary stage reforming process at temperatures above 1000C before cooling in the production of high pressure steam in one or more boilers.

Used herein, the term "synthesis gas containing nitrogen and hydrogen, means synthesis gas for ammonia production, i.e. synthesis gas having the proper proportions of hydrogen and nitrogen, is used as feedstock for the ammonia Converter.

Used herein, the terms "secondary reforming" and "autothermal reforming" equivalent, because the secondary reforming is usually carried out in Autoterminal furnace reformer (ATR). However, strictly speaking, the term "autothermal reforming" has a corresponding meaning only in the absence of the primary reformer.

Used herein, the term "primary reforming" means the reforming of hydrocarbons in the ordinary fiery tubular reformer furnace (the fiery furnace).

It is also clear that solenoidality process gas, leaving the catalytic ammonia Converter, first passes through the superheater(s) and then through a steam boiler(boilers)heat(s). All steam produced in the steam boiler(s), heat exchanger(s) section of the reformer and the steam produced in the steam boiler(s), heat exchanger(s) of the site of synthesis of ammonia is carried out in the first superheater mounted behind the catalytic ammonia Converter. At least part of a couple of these heaters can also be used as process steam in the area of reforming the enterprise, preferably as process steam at the site steam recovery boilers-primary stage reforming process.

In a preferred embodiment of the invention, step (a)includes passing the hydrocarbon feedstock through the area of reforming and removing synthesis gas from the above-mentioned section of the reformer contains stage: passing the hydrocarbon feedstock through a stage of primary reformer for receiving the partially converted gas transmission mentioned partially converted gas through the step of heat-exchange reformer and the level of the secondary reformer, and retrieving the target stream of synthesis gas of the above-mentioned stage of the heat exchange reformer, and partially converted gas, noise che the ez step of heat-exchange reformer, transform by indirect heat exchange with synthesis gas extracted from the mentioned stage of the secondary reformer.

Heat exchange reforming process permits the use of heat from the stage of primary and secondary reforming process for the secondary reformer gas, instead of simply applying heat to produce steam. Thus, it can also significantly reduce the production of steam, and in fact to the number that corresponds to the needs of the site of synthesis of ammonia. The result is eliminated inappropriate steaming.

As noted above, it is generally assumed that the risk of metal dusting is highest when the metal temperature in the range from 400C to 800C, especially from 500C to 750C. Thus, the flow of the synthesis gas that is extracted from a part of the reforming process, in particular the flow of synthesis gas, extracted from the mentioned stage heat exchange reformer, the temperature is preferably about 800C. or higher, which is high enough to reduce the risk of metal dusting in the heat exchanger, and also to prevent metal dusting placed in the steam boilers recovery.

Heat-exchange reforming is conducted preferably in one or more heat exchange reactor containing a double pipe. Double pipe is in there is the device of two concentric pipes. The space between the walls of the tube forms an annular cavity through which can flow the hot expanding environment (synthesis gas extracted from the mentioned stage secondary reformer). The solid catalyst in the form of a layer, can be placed outside and/or inside the double tubes.

Accordingly, in another embodiment, the invention provides for the processing of the mixed gas within one or more heat exchange reactors, with many dual pipes, and which are used for carrying out the mentioned stage heat exchange reformer by mixing, preferably in the lower part of one or more heat exchange reactor, the synthesis gas that is extracted from the mentioned stage secondary reformer, with the converted gas leaving the catalytic layer placed at least outside the double tubes of one or more heat exchange reactors, and the transmission of the aforementioned mixed gas through the annulus mentioned double tubes for indirect heating mentioned catalytic layer. The final stream of synthesis gas is then extracted and passed through one or more steam boilers-boiler set forth in the section of the reformer.

The particles of the solid catalyst catalytic layer of one or more heat exchange reactors preferably place is not only outside the double tubes, but inside, i.e. also in the inner pipe of the double pipe.

In another embodiment, the step of heat-exchange reforming is carried out in the reactor of the bayonet type. In particular, in the embodiment, a bayonet, a tubular type reactor, at least one pipe in this reformer furnace is made outside of the inner pipe, the outer pipe is provided with an inlet for introducing a process gas used for the conversion, and closed to release the inner tube is open at both ends and mounted coaxially within the outer tube and spaced from it, the annular space between the outer and inner tube filled with a catalyst for the reforming process, the inner tube is made to retrieve the discharge flow of the converted gas, and the outer tube additionally concentrically surrounded posted with her pipeline and completed for transmission the stream of hot synthesis gas from the secondary of the Converter, which is in thermal communication with the process gas, intended for conversion (reacts raw materials), in the outer tube, by carrying out the synthesis gas from the furnace secondary reformer in the space between the pipe and the outer pipe. Concrete option implementation of this bayonet reactor of the type disclosed, for example, in our bid, medium, small the EP-A-0 535 505.

In another embodiment of the invention the hydrocarbon raw material, intended for conversion in step (a), is passed in parallel in one or more stages of heat exchange reforming and stage autothermal or secondary reforming process and extracted from above mentioned stage autothermal or secondary reformer synthesis gas used as a heat transfer medium on said one or more stages of heat exchange reforming, as described in our U.S. patent No. 6,726,851.

As another object of the invention we provide a superheater for use in the method, in particular the superheater for use according to step (e) of the method, i.e. after the catalytic ammonia Converter.

Accordingly, the invention also includes a superheater 30, containing:

the first and second branch 301, 302, and the first compartment 301 is equipped with a shell 305, pipe plate 303, a rear wall 307, beam pipes 309, reflective walls 317 and propuskom 315, made on the shell 305, and thus the second compartment 302 is equipped with a shell 306, tube plate 304, a back wall 308, a bundle of tubes 310, reflective walls 317 and steam dispenser 316, which is made on the shell 306;

transitional office 311, which separates the first and second branch, and which is formed a space is between the tube plates 303,304;

waste pipe 312 passing through the tube plate 303, 304 and, therefore, through the Department of transitional 311, which extends from the first compartment 301 in the second part 302-axis 320 of the length of the superheater 30;

the separating wall 321 disposed between the inlet chamber 318 and outlet chamber 319;

referred to transitional office 311 provided with inlet 313 process gas, which is included in the inlet chamber 318 of the transition compartment, and an inlet chamber 318 is formed between the wall of the waste pipe 312, the wall of the tube plate 303 on the one hand, and which continues the beam pipe 309 of the first compartment 301, and a wall of the tube plate 304 on the opposite side, and which continues the beam pipe 310 of the second compartment 302;

referred to transitional office 311 provided with a release 314 process gas that comes out of the exhaust chamber 319 transitional compartment, and the exhaust chamber 319 is formed between the wall of the waste pipe 312, the wall of the tube plate 303 on the one hand, and which continues the beam pipe 309 of the first compartment 301, and a wall of the tube plate 304 on the opposite side, which continues the beam pipe 310 of the second compartment 302;

while the first and second branches 301, 302 are connected in series relative to the flow of steam and parallel to the flow of process gas is.

Steam is passed through the annular space of the superheater, while the process gas from the ammonia Converter is passed through line space.

Inlet 313 process gas and the release of 314 process gas transition branch 313 preferably located diametrically opposite each other on the shell 305, 306 superheater, and more preferably, when the above-mentioned suction and discharge 313, 314 are located diametrically opposite each other and in the same place along the axis 320 of the length of the superheater.

The separating wall 321, located between the inlet chamber 318 and outlet chamber 319, preferably continues along and across the direction of the length of sewer pipe 312. This wall serves to prevent direct process gas passes from the inlet chamber 318 in the discharge chamber 319. The tube bundle in each Department superheater preferably presents a U-shaped tube bundle.

The tube bundle continues in each tube plate and thereby fixed in it. It is clear that the pipes penetrate through the tubular plate. Thus, the tubes are in fluid communication with the inlet chamber of the transition office, which accepts the incoming hot process gas from the ammonia Converter, or exhaust chamber transitional separated the I, from which to extract the cooled process gas.

In a specific embodiment, the exhaust chamber 319 further comprises valves 322, 323, installed inside, and which are in fluid communication with beam pipes 309, 310 of the first and second compartments 301, 302. The valves are preferably represented by the throttle valve. Providing valves to the exhaust chamber contributes to the flow in the first (cold) and the second (hot) Department of superheater correct proportions process gas from the ammonia Converter, and thereby, it is possible with simple means to adjust the temperature coming out of the steam dispenser 316. Preferably 40% by weight of the process gas is passed through the first branch and 60% by weight on the second branch. By regulating the exhaust steam temperature in the superheater, which may be about 375C, can also be adjusted final superheat temperature of this steam, after passing it through a plot of steam boilers-boiler furnace primary reformer, where it is additionally heated to a final temperature of overheating, for example, 515C. This final temperature of steam in practice is the temperature, which should be regulated, and this regulation is now feasible by simple adjustment of the temperature coming out paratwada superheater. Eliminated the undesirable alternatives of regulation this final temperature of overheating, such as adding make-up water for the boiler (BFW) with the purpose of rapid cooling of steam during its passage through the area of waste heat boilers heat furnace primary reformer.

The method according to the invention contributes to the fact that saturated steam is introduced into the first part of the superheater at a relatively low temperature (323). Such pairs will include some transfer from the steam drum in the form of water droplets. This can lead to stress corrosion of internal metal parts of the superheater, if they are made of austenitic material, such as stainless steel. However, the internal metal parts of the superheater according to this invention, primarily, the tube bundle in the first part, preferably made of low alloy steel. Since the first (cold) separation can be maintained at temperatures below 380C, due to the cold incoming pair (323C), it is possible to apply low-alloyed steel, for example, low carbon steel, and without the risk of manifestations of nitriding. Internal metal parts in the second (hot) Department, mainly, the beam pipe is made of stainless steel, because of the risk of nitriding, when the temperature may not fall below 80C throughout this Department. The risk of stress corrosion in this division no longer relevant, because the drops of water transferred from the incoming steam evaporate when it is passing in the first compartment and, hence, the steam dry.

Therefore, according to an additional variant of the invention, the tube bundle in the first part is made of low-alloy steels, for example, ferritic cast iron, chromium, molybdenum and carbon steel, and the tube bundle in the second part are made of stainless steel. Low-alloy steel preferably presents microalloyed steel.

Along with solving the problems of corrosion of the superheater according to the invention is in particular preferred for large enterprises for the production of ammonia, where the size of the superheaters standard project becomes so large that it is simply impossible to make. Using a superheater according to this invention the process gas stream from the ammonia Converter is shared between the first and second compartment. In other words, each tube plate transmits only a portion of the process gas stream, and at the same time the tube plates are supported by a waste pipe which extends from one compartment to another along the axis of the length of the superheater. This leads to a significant reduction in the thickness of labor is different plates in comparison with the situation when traditional single tube plate. Thus the invention also provides a simpler and cheaper design. The superheater can be made in almost any specialized shop.

Used herein, the term "large ammonia enterprise characterizes enterprise ammonia production with a capacity equal to or more than 2000 tons/day, for example, 3000, 5000 tons/day or more.

For convenience, the orientation of the superheaters usually horizontal, because of heavy pipe plate and the main areas are usually located near the rear wall of the superheater. However, this horizontal orientation can bring problems of corrosion, in particular in metal parts that are installed in the middle section of the superheater. In particular when starting, when the metal parts of the superheater is not yet heated, they can accumulate and condense water droplets containing impurities, for example, chlorine.

Since such metal parts are frequently not made of corrosion-resistant materials, this can cause serious problems with corrosion.

Using the invention it is possible to additionally prevent these problems corrosion easy installation superheater in a vertical position. This situation is easier to achieve with a superheater according to this invention, since the heavy metal parts, materialschlacht mostly a tube plate, installed around the middle part of the installation. The potential drop of water containing impurities accumulate and gather in the bottom of the superheater in the first or second part. So nakoplennoy water just to extract a set here the drain.

Therefore, in another embodiment of the invention, the orientation of the vertical superheater, and the first or the second part additionally has at its rear wall outlet for removal of the collected water. In this vertical orientation, the lower section of the superheater is preferably the second (hot) Department.

Figure 1 is a block diagram of a particular variant of the method in the enterprise ammonia synthesis, showing the plot of the first reforming process, consisting of the installation of the heat exchange reformer and install the secondary reformer, and the second area II of the synthesis of ammonia.

Figure 2 presents a diagram of the superheater according to the invention for use in ammonia synthesis shop of the enterprise.

Figure 1 is a hydrocarbon raw material 1, for example, natural gas, passed through the stage of primary reformer with the addition of steam into the oven 20 primary reformer. Partially converted gas 2 is extracted from the furnace primary reformer 20 and is divided into separate streams 3 and 4. Stream 3 is conducted in the upper part of the furnace warm the exchange reformer 21, with dual pipes placed in them by the catalyst particles arranged outside and inside the double tubes, while a separate stream 4 is passed through the furnace 22 secondary reformer. In the lower part of the furnace heat exchange reformer 21 resulting from the furnace secondary reformer hot gas is mixed with the converted in the furnace heat exchange reformer process gas, which exits the catalytic layers in the lower part of the reformer furnace. The mixed gas used for indirect heating her placed in a catalytic layers, providing rise above mentioned mixed gas up into the furnace reformer. The mixed gas passing through the furnace heat exchange reformer is cooled and exits as stream 5 synthesis gas. Stream 5 is further cooled in a steam recovery boiler 23 and makeup water 6, and thus the synthesis gas is in indirect heat exchange with the stream. At this section of the superheater not PrimeOutput a mixture of steam boiler 23 is carried out in the steam drum 24. The cooled stream of synthesis gas enriched with hydrogen at site 25 conversion of water vapor and then passed through leaching section 26 to remove remaining in the synthesis gas of carbon monoxide, carbon dioxide and methane. Thus, creating a stream of 8 synthesis gas for ammonia production, the content is the future right proportions of hydrogen and nitrogen, and spend in the catalytic ammonia Converter 27 plot of ammonia synthesis company, containing many layers 28 for the catalysis of ammonia. Ammonia 9 process gas at a temperature of 460C is extracted from the catalytic Converter and is cooled by passing through the superheater 30 and steam boiler 29. After superheater 30 process gas is cooled to approximately 380C. Produced superheated steam 10 out at a temperature of about 375C and can be used for driving compressors in the enterprise, while pairs 11 of the steam boiler 29 are in the steam drum 24. Make-up water for the boiler (BFW) is added in the form of thread 12, while the stream 13 from the steam drum 24 is used to produce steam in a steam recovery boiler 29. The steam produced in the steam recovery boiler 23 land reformer and a steam recovery boiler 29 plot of ammonia synthesis using flow 14 in the form of high pressure steam from the boiling point of 323C overheat in the superheater 30 ammonia synthesis shop. The cooled process gas containing ammonia, extracted in the form of thread 15.

Now refer to figure 2, which presents the scheme of the superheater 30 of figure 1. The superheater contains the first (cold) Department 301 and the second (hot) office 302, two of Trubin the e plate 303, 304, two shell 305, 306 with the respective rear walls 307, 308, two U-shaped tube bundle 309, 310, and transitional compartment 311 and sewer pipe 312. This drain continues in the center of the superheater from the first compartment 301 in the second part 302-axis 320 of the length of the superheater. The superheater includes inlet 313 process gas and the release of 314 process gas, performed as part of the transition compartment 311 and propusk 315, made on the shell 305 of the first compartment 301, and the steam dispenser 316, which is made on the shell 306 of the second compartment 302. In the first and second branches are reflective walls 317 to reflect the flow of steam and thereby increase the heat transfer. Reflectors also provide support for the beam pipe. Transitional office 311 includes an inlet chamber

318 in direct continuation to the inlet 313 process gas and in communication through a fluid medium with the beam pipe 309, 310, continuing in the tube plates 303, 304. Transitional office 311 also includes the discharge chamber 319, which continues directly in issue 314 process gas; an exhaust chamber 319 is also in communication through liquid messages with beam pipes 309, 310, continuing in the tube plates 303, 304. The separating wall 321, the ongoing volucella sewer pipes 312, separates the inlet and outlet chambers 318, 319. Thus, the first and second branches are connected in series relative to the flow of steam and parallel to the flow of process gas. Throttle valves 322 and 323, placed in the exhaust chamber 319, serve to control the amount of flow through the first (cold) and the second (hot) Department of process gas, and the temperature of the steam in the steam dispenser 316.

The method according to the invention allows in other words to provide saturated steam superheater at a relatively low temperature (323). Vapor at a given temperature enters through propusk 315 near the rear wall of the first (cold) unit, which then flows through the annular space. Here the steam is superheated to 345C and held at this temperature through the drain 312 in the second (hot) Department of the superheater. Couples additionally overheats and goes through the steam dispenser 316 in the form of superheated steam at 375C. the Process gas from the ammonia Converter includes at 460C in the superheater through the inlet 313 process gas in the inlet chamber 318 of the transition branch 311. Process gas are separated and passed into first and second compartments through the tube plate 303, 304 in the U-shaped bundles of pipes 309, 310. After passing through the U-shaped pipe technologically the gas enters through pipe plate 303, 304 into the exhaust chamber 319 through throttle valves 322, 323. Process gas from the first compartment enters the exhaust chamber 319 at 373C, while the process gas from the second compartment includes at 403C. the Mixed gas in the chamber reaches a temperature of 380C and goes through the issue 314 process gas for additional cooling located in the steam boiler (boilers)heat(s).

1. Method for the production of ammonia from a hydrocarbon containing phase:
(a) passing the hydrocarbon feedstock through the area of reforming and removing synthesis gas from the above-mentioned section of the reformer;
(b) passing the said synthesis gas through one or more steam boilers heat recovery steam generators without the use of the superheater, and in which the synthesis gas is in indirect heat exchange with steam-water mixture, removing a pair of the above-mentioned heat-recovery boilers and conduct of said pair to one or more steam drums;
(c) passing the cooled stage (b) synthesis gas through a stage of transformation for the conversion of carbon monoxide in the synthesis gas into hydrogen, and then through a washing process to remove remaining in the synthesis gas, carbon dioxide, carbon monoxide and methane, and removing synthesis gas containing nitrogen and hydrogen;
(d) transmittance obtained in stage (C) syngas through the site of synthesis of ammonia, which includes the catalytic conversion of synthesis gas to ammonia by passing through one or more catalytic layers in an ammonia Converter and removing the process gas containing ammonia, one or more catalytic layers;
(e) transmission mentioned process gas containing ammonia, through one or more superheaters, which overheat the steam from one or more steam drums stage (b), and removing a stream of superheated steam from the aforementioned one or more superheaters;
(f) passing the cooled stage (e) of process gas through one or more steam recovery boilers, in which the process gas is in indirect heat exchange with steam-water mixture, removing a pair of these one or more steam recovery boilers and conduct of said pair to one or more steam drums stage (b), characterized in that
stage (a) comprises the stage of: passing the hydrocarbon feedstock through a stage of primary reformer for receiving the partially converted gas transmission mentioned partially converted gas through a stage of heat exchange reforming stage and the secondary reformer, and retrieving the target stream of synthesis gas of the above-mentioned stage of the heat exchange reformer, being the m partially converted gas, passed through the stage of the heat exchange reformer transform by indirect heat exchange with synthesis gas extracted from the mentioned stage of the secondary reformer.

2. The method according to claim 1, further comprising processing the mixed gas in one or more heat exchange reactors, with many dual pipes, and which are used for carrying out the mentioned stage heat exchange reformer by mixing the synthesis gas extracted at the above-mentioned stage Autoterminal reforming stage or secondary reformer, with the converted gas leaving the catalytic layer placed at least outside the double tubes of one or more heat exchange reactors, and the transmission of the aforementioned mixed gas through the annulus mentioned double tubes for indirect heating mentioned catalytic layer.

3. The method according to claim 1, characterized in that stage of heat exchange reforming is carried out in the reactor of the bayonet type.

4. The method according to claim 1, characterized in that the hydrocarbon feedstock provided to the transform stage (a), is passed in parallel in one or more stages of heat exchange reforming stage and Autoterminal or secondary reformer, and in which the hot synthesis gas is extracted at the above-mentioned stage Autoterminal or secondary reformer, remaneat as a heat transfer medium on said one or more stages of heat exchange reformer.

5. Superheater (30)containing:
the first and second branch (301, 302), and the first branch (301) sheathed (305), pipe plate (303), rear wall (307), the tubular beam (309), reflective walls (317) and propuskom (315)performed on the shell (305), while the second part (302) is provided with a sheath (306), the tube plate (304), rear wall (308), the tubular beam (310), reflective walls (317) and steam dispenser (316)performed on the shell (306); a transition unit (311), which separates the first and second branch, and which is formed by the space between the tube plates (303, 304); sewer (312)passing through the tube plate (303, 304) and, consequently, through the transitional section (311), and which extends from the first branch (301) in the second branch (302) along the axis (320) the length of the superheater (30);
the separating wall (321)disposed between the inlet chamber (318) and an outlet chamber (319);
referred to transitional office (311) is provided with inlet (313) process gas, which is included in the inlet chamber (318) transition office, and the inlet chamber (318) is formed between the wall of the waste pipe (312), the wall of the tube plate (303) on the one hand, and which continues tubular beam (309) of the first branch (301), and the wall of the tube plate (304) from the opposite side, and in which prodolzhaet the tubular beam (310) of the second branch (302);
referred to transitional office (311) is provided with a release (314) process gas that comes out of the exhaust chamber (319) transition office, and the exhaust chamber (319) formed between the wall of the waste pipe (312), the wall of the tube plate (303) on the one hand, and which continues tubular beam (309) of the first branch (301), and the wall of the tube plate (304) from the opposite side, which continues tubular beam (310) of the second branch (302); and
while the first and second branches (301, 302) are connected in series relative to the flow of steam and parallel to the flow of process gas.

6. Superheater according to claim 5, characterized in that the discharge chamber (319) further comprises valves (322, 323)installed inside, and being in fluid communication with the beam pipe (309, 310) of the first and second branch (301, 302).

7. Superheater according to claim 5, characterized in that the tube bundle in the first part is made of low alloy steel, and the tube bundle in the second part are made of stainless steel.

8. Superheater according to any one of pp.5-7, characterized in that the adopted vertical orientation of the superheater, and the first and second branch further comprises at its rear wall release for removal of the accumulated water.

9. Superheater according to claim 5 for use in the method p is 1.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention deals with method and device for ammonia synthesis from synthesis-gas, which contains nitrogen and hydrogen. Device with, at least, one reactor (1), includes first non-cooled unit of catalyst layers (2), at least, one heat exchanging device (3), at least, two cooled units of catalyst layers (3, 41, 42), and each of units (4, 41, 42) is provided with aggregate of cooling pipes (5), and circulation line (6), at least, with one supplying device (61) and, at least, one discharge device (62). Line (6), starting from supplying device (61), passes successively down on flow of aggregate of cooling pipes (5), first non-cooled unit (2), heat exchanging device (3) and, at least, two cooled units (4, 41, 42) up to discharge device (62). Aggregate of cooling pipes (5) from each of cooled units (4, 41, 42) on discharge side of cooling pipes in each case are connected with assembled discharge device (10). Line (6) has, at least, in each case one bypass line (7) for each cooled unit (4, 41, 42), which in each case is placed between supplying device (61) and assembled discharge device (10) of aggregate of cooling pipes (5) from each cooled unit (4, 41, 42). Invention also represents synthesis of ammonia from synthesis-gas with application of claimed device.

EFFECT: method makes it possible to effectively apply possibilities of catalyst with obtaining high discharge concentration of ammonia.

19 cl, 7 dwg, 4 tbl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention can be used in chemical industry. The method of producing ammonia involves compressing steam, hydrocarbon material and air. Before the air compression step, the air is cooled, while ensuring stoichiometric ratio of nitrogen and hydrogen in the process. The material is cleaned from sulphur compounds. Steam and steam-air conversion of methane and carbon oxide conversion steps then follow. The obtained nitrogen-hydrogen mixture is cleaned from oxygen-containing compounds, compressed and fed for ammonia synthesis in a closed cycle from which the ammonia product is separated in liquid form.

EFFECT: invention increases efficiency of the process and increases output of the end product.

2 cl, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to chemistry. The method of producing synthesis gas for ammonia synthesis involves feeding a gas stream containing hydrocarbons and a gas stream containing steam into a primary conversion apparatus which is equipped with a plurality of externally heated catalyst tubes, reaction of said hydrocarbons with steam in the catalyst tubes of the primary conversion apparatus at operating pressure therein of at least 45 bar to obtain a product gas, feeding the product gas and a stream of oxidative gas into a secondary conversion apparatus, reaction of the product gas with the oxidative gas and subsequent secondary conversion while providing conversion of all hydrocarbons contained in the product gas coming from the primary conversion apparatus to obtain converted gas which contains hydrogen, carbon oxides and unreacted steam, removing carbon oxides from the converted gas and obtaining synthesis gas which is suitable for synthesis of ammonia. The oxidative gas used is oxygen-rich air with molar ratio N2/O2 which enables to obtain converted gas with nitrogen content which corresponds to content which is required for stoichiometric molar ratio H2/N2 for ammonia synthesis.

EFFECT: method enables to achieve high production capacity of synthesis gas and lower capital costs and power consumption.

5 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: ammonia converter can include first shell (108), with located in it two or more separate catalyst layers (134, 136, 138, 140), second shell (106), located around first shell. First heat exchanger (168) is located outside first shell (108) and is connected with it by flowing medium (166) via flow channel (124), located inside first shell (108). Second heat exchanger (104) is located outside second shell (106) and is connected with it by flowing medium (116).

EFFECT: invention makes it possible to increase efficiency of ammonia obtaining.

20 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: coal undergoes gasification via partial oxidation in a gasification furnace 2 consisting of a hearth 2a and a gasification chamber 2b. In a desulphurisation apparatus 3, having a wet cleaning 3a and a dry cleaning section 3b, hydrogen sulphide is removed from gas generated in the gasification furnace 2. In a shift reaction reactor 4, carbon oxide contained in the gas coming out of the desulphurisation apparatus 3 is converted to carbon dioxide. A carbon dioxide scrubber 5 serves to remove carbon dioxide contained in the gas coming out of the shift reaction reactor 4. In a denitration apparatus 6, molar ratio of nitrogen to hydrogen in the gas coming out of the carbon dioxide scrubber 5 is brought to about 1:3 by removing nitrogen. Ammonia is obtained as a result of a reaction in generator 7 between nitrogen and hydrogen contained in the gas coming out of the denitration apparatus 6.

EFFECT: invention enables continuous operation of a gasification furnace for a long period of time.

2 cl, 5 dwg

FIELD: blasting.

SUBSTANCE: device to produce porous granulated ammonium nitrate comprises a drum, arranged as capable of installation as inclined relative to the horizontal line and as capable of rotation around its central axis, a feeder-batcher, a tray for supply of granulated ammonium nitrate into a loading neck of a drum and a receiving hopper. The drum is made with two internal longitudinal through cylindrical working cavities, is equipped with heat insulation along the side external surface and is arranged in a heat-protective jacket at the hollow shaft arranged as capable of supplying liquid coolant to walls of working cavities in counterflow relative to supply of granulated ammonium nitrate. The method for production of porous granulated ammonium nitrate consists in the fact that thermal treatment of granulated ammonium nitrate is carried out by means of its heating in a rotary drum to the temperature of 32.3 - 50C, soaking at this temperature in a rotary drum for 0.5 - 5 minutes and soaking in a receiving hopper at the temperature of environment for 0.5 - 10 minutes.

EFFECT: invention provides for high efficiency, safety and ecological compatibility of a technological process.

8 cl, 7 dwg

FIELD: chemistry.

SUBSTANCE: invention can be used in chemical industry. Natural gas is compressed, heated and purified from sulphur compounds in a radial-spiral reactor. Two-step catalytic conversion of methane under pressure is carried out in a radial-spiral reactor which is divided into two sections. Steam conversion is carried out in the first section at temperature 800 - 1000C using heat from the gas which is converted at the second step, as well as portions of natural gas, blow-off and flash gases additionally burnt at a burner. The temperature of flue gases after the burner is kept in the range of 900-1100C by recycling a portion of cooled flue gases with mixture thereof with air fed into the burner. The mixture of gases fed into the burner is first heated using heat from flue gases from the first section. Air-steam conversion is carried out in the second section at 900-1400C. Heat of the converted gas is used to heat the initial natural gas and generate steam. Catalytic conversion of carbon oxide is carried out in a single step in the radial-spiral reactor at temperature 200-220C, which is maintained via water evaporation cooling. The nitrogen-hydrogen mixture is cleaned from carbon dioxide and oxygen-containing compounds in the radial-spiral reactor, compressed and fed for ammonia synthesis into the radial-spiral reactor.

EFFECT: cost effectiveness and ecological cleanness.

6 cl, 1 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: inventions can be used in chemical industry. The method of producing a stoichiometric hydronitric mixture for synthesis of ammonia involves conversion of natural gas and subsequent purification of the obtained synthetic gas. When purifying synthetic gas, the operation of removing methane and argon from the synthetic gas is combined with the operation for condensation of excess nitrogen by absorbing methane and argon with the condensed excess nitrogen. The absorption process takes place in vertical pipes of an absorber-condenser in counter flow with the purified synthetic gas moving in the pipes from bottom up. The space between the pipes is cooled by throttling the condensate, and the absorber-condenser pipes are fitted with apparatus for swirling the stream of condensate. The obtained purified hydronitric mixture can be used in the ammonia synthesis method.

EFFECT: invention enables to completely extract methane and argon impurities from synthetic gas with incidental production of an argon product and liquefied methane, and also enables to considerably reduce ammonia synthesis pressure from 300 to 170 atm, which reduces power consumption in production of ammonia.

19 cl, 3 tbl, 2 dwg, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing ammonia from nitrogen and hydrogen and can be used in the chemical industry. Ammonia 3 is obtained from a gaseous mixture 4 essentially consisting of nitrogen and hydrogen, obtained from natural gas 5 using the following method. Unpurified synthetic gas 7 is obtained from natural gas 5 through partial oxidation with an oxygen-rich gas 6 in the presence of water vapour. Converted ynthetic gas 8 which contains hydrogen, carbon dioxide and carbon monoxide is obtained from synthetic gas 7 during at least one step for a catalytic reaction (shift) and conversion of a portion of carbon monoxide to carbon dioxide. On at least one decarbonisation step, carbon dioxide 20a is at least partially removed from the obtained synthetic gas and at least during one purification step, carbon monoxide 22a is at least partially removed. On at least one converted synthetic gas purification step, at least one molecular sieve is used. The oxygen-rich gas contains at least 50% oxygen and partial oxidation takes place at pressure between 40 and 150 bars.

EFFECT: method enables to increase efficiency while reducing power consumption and operational costs owing to reduction of the amount of initial hydrocarbon material.

5 cl, 1 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: synthesis gas consisting of makeup gas or a mixture of makeup gas and recycle gas is passed through at least two synthesis steps connected in series into a synthesis system. After coming out of the synthesis steps, gases which contain the product, except gases containing the product from the last synthesis step, are divided into at least two separate streams, one of which is cooled to condensation temperature of the contained product, and the condensate containing the product is separated from the gas which is then combined with the hot portion of gases containing the product to bring their temperature to a level it should have when entering the next synthesis step. Also before repeated addition to the hot portion of gases containing the product, the separate stream from which the product was separated via condensation and then removed can be heated to a temperature, which after such heating should be below temperature of the hot portion of the gases containing the product, and the heat used for heating the separate stream from which the product was separated via condensation, can at least be partially extracted from the said stream when cooling it.

EFFECT: method allows for carrying out heterogeneous catalytic exothermal gas-phase reactions with increased output and reduced energy consumption.

14 cl, 8 dwg, 3 tbl

FIELD: heat power and chemical industries, applicable in production of ammonia.

SUBSTANCE: in the method for steam generation at production of ammonia from hydrocarbon gases, saturation of the hydrocarbon gas after desulfurization and/or process air fed to the secondary reforming is effected due to the use of the flue gas of a tube furnace at a temperature of 160 to 580C, preferably within 220 to 480C, by means of water recirculation.

EFFECT: reduced consumption of energy due to reduction of the total amount of generated steam, reduced consumption of feed water, and recovered gases dissolved in the process condensate.

4 cl, 1 dwg

FIELD: heat power and chemical industries, applicable in production of ammonia.

SUBSTANCE: in the method for steam generation at production of ammonia from hydrocarbon gases the mean-pressure steam used for the process of steam reforming and/or for the compressor drives is subjected to humidification by injection of the process condensate or feed water, and the obtained humidified steam is overheated by the heat of the flue gas in a unit of the heat-using equipment of the reforming tube furnace.

EFFECT: reduced consumption of energy due to reduction of the amount of generated steam and reduced of the amount of generated steam and reduced consumption of feed water; provided additional cleaning of the process condensate and recovering of gases dissolved in it in the process of steam humidification in the mass transfer device.

2 cl, 1 dwg

FIELD: inorganic synthesis catalysts.

SUBSTANCE: invention provides ammonia synthesis catalyst containing ruthenium as active ingredient supported by boron nitride and/or silicon nitride. Catalyst can be promoted by one ore more metals selected from alkali, alkali-earth metal, or rare-earth metals. Ammonia synthesis process in presence of claimed catalyst is also described.

EFFECT: increased temperature resistance of catalyst under industrial ammonia synthesis conditions.

4 cl, 6 ex

FIELD: chemical industry; production of ammonia.

SUBSTANCE: the invention is pertaining to the process of synthesis of ammonia, in particular to improvement of the process of cleanout synthesis of the gas added into the catalytic reactor for substitution of the reacted synthesis gas. The method of synthesis of ammonia provides for compression of the synthesis gas containing hydrogen and nitrogen in a many-stage centrifugal compressor. On the first stage of this compressor the synthesis gas is compressed up to the pressure making from approximately 800 up to 900 pounds per a square inch - (56-63)·105 Pa, withdraw from this stage and cool, and also dehydrate by a contact to a liquid ammonia in a dehydrator. Then the cooled and dehydrated synthesis gas is fed back in the compressor and bring it on the second stage. The installation for realization of this process contains a centrifugal compressor supplied with the synthesis gas outlet, that connects the synthesis gas discharge outlet from the first stage of the compressor with the synthesis gas inlet in the dehydrator, and also an intermediate inlet of the synthesis gas connecting by a hydraulic link the inlet of the second stage of the compressor with the synthesis gas discharge (outlet) from the dehydrator. Due to the intermediate cooling and a dehydration the compressor rate is lowered, and due to favorable effect of the dehydrator on the last two stages of the compressor a significant saving of the consumed power is also achieved. The additional saving of the consumed power is possible due to decreased need of chill in the closed contour of the synthesis process.

EFFECT: the invention ensures a significant saving of the consumed power for the synthesis process in the installation.

13 cl, 1 dwg

FIELD: industrial inorganic synthesis.

SUBSTANCE: process comprises passing nitrogen and hydrogen-containing synthesis gas stream through three stacked catalyst beds, wherein catalyst is based on iron with magnetite as principal constituent, which is reduced during the process until catalytically active form of alpha-iron is produced. Above-mentioned synthesis gas stream is obtained by combining stream directly supplied onto first catalyst bed with another stream, which is preheated via indirect heat exchange with products exiting first and second catalyst beds, whereupon product is recovered. Method is characterized by that gas under treatment is passed through middle catalyst bed at volume flow rate between 0.65 and 2.00 value of volume flow rate, at which gas under treatment is passed through upper catalyst bed, volume ratio of middle catalyst bed to upper catalyst bed lying preferably between 0.5 and 1.5.

EFFECT: increased yield of product.

2 cl, 1 dwg, 1 tbl

FIELD: inorganic synthesis catalysts.

SUBSTANCE: ammonia synthesis catalyst includes, as catalytically active metal, ruthenium deposited on magnesium oxide having specific surface area at least 40 m2/g, while concentration of ruthenium ranges between 3 and 20 wt % and content of promoter between 0.2 and 0.5 mole per 1 mole ruthenium, said promoter being selected from alkali metals, alkali-earth metals, lanthanides, and mixtures thereof. Regeneration of catalytic components from catalyst comprises following steps: (i) washing-out of promoters from catalyst thereby forming promoter-depleted catalyst and obtaining solution enriched with dissolved promoter hydroxides; (ii) dissolution of magnesium oxide from promoter-depleted catalyst in acidic solvent wherein ruthenium is insoluble and thereby obtaining residual ruthenium metal in solution enriched with dissolved magnesium compound; and (iii) regeneration of residual ruthenium metal from solution enriched with dissolved magnesium compound via liquid-solids separation to form indicated solution enriched with dissolved magnesium compound and ruthenium metal.

EFFECT: increased catalyst activity.

6 cl, 6 ex

FIELD: petrochemical industry; methods of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gases.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gases. The method of the catalytic synthesis of ammonia from the mixture of nitrogen and hydrogen provides, that the natural gas together with the oxygen-enriched gas containing at least 70 % of oxygen is subjected to the autothermal reforming at temperature from 900 up to 1200°C and the pressure from 40 up to 100 bar at the presence of the catalyzer of cracking, producing the unstripped synthesis gas containing in terms of the dry state 55-75 vol.% of H2, 15-30 vol.% of C and 5-30 vol.% CO2. At that the volumetric ratio of H2: CO makes from 1.6 : 1 up to 4 : 1. The unstripped synthesis gas is removed from the furnace of the autothermal reforming, cooled and subjected to the catalytic conversion producing the converted synthesis gas containing in terms of the dry state at least 55 vol.% of H2 and no more than 8 vol.% of CO. The converted synthesis gas is subjected to the multistage treatment for extraction ofCO2, CO and CH4. At that they realize the contact of the synthesis gas with the liquid nitrogen and using at least one stage of the absorption treatment produce the mixture of nitrogen and hydrogen, which is routed to the catalytic synthesizing of ammonia. At that at least a part of the synthesized ammonia may be transformed into carbamide by interaction with carbon dioxide. The realization of the method allows to solve the problem of the ammonia synthesis efficiency.

EFFECT: the invention ensures solution of the problem of the ammonia synthesis efficiency.

8 cl, 1 ex, 2 tbl, 2 dwg

FIELD: chemical industry; installations and the methods of production of the synthesis-gas from the natural gas.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the installation and the method for simultaneous production from the natural gas of the methanol synthesis-gas, the ammoniac synthesis-gas, carbon monoxide and carbon dioxide. The installation consists of the in-series connected to each other assembly units and includes: the first reactor (A), in which at feeding of oxygen realize the transformation of the natural gas into the synthesis gas consisting of carbon monoxide, carbon dioxide, hydrogen and the steam; the second reactor (B), in which exercise the regular transformation of carbon monoxide into carbon dioxide; if necessary the compressor (C) using which the formed gases may be contracted; absorbing apparatus D, which serves for absorption of carbon dioxide and production of he mixture of monoxide with hydrogen used for synthesizing methanol; the refrigerating separator E, in which at feeding of the liquid nitrogen receive the ammoniac synthesis gas and simultaneously produces carbon monoxide, argon and methane. The invention allows to increase profitability of the installation due to production at one installation of several products.

EFFECT: the invention ensures the increased profitability of the installation due to production at one installation of several products.

15 cl, 1 dwg, 1 tbl

FIELD: inorganic synthesis catalysts.

SUBSTANCE: ammonia synthesis catalyst is based on ruthenium on carrier of inoxidizable pure polycrystalline graphite having specific BET surface above 10 m2/g, said graphite being characterized by diffraction pattern comprising only diffraction lines typical of crystalline graphite in absence of corresponding bands of amorphous carbon and which graphite being activated with at least one element selected from barium, cesium, and potassium and formed as pellets with minimal dimensions 2x2 mm (diameter x height). Catalyst is prepared by impregnating above-defined catalyst with aqueous potassium ruthenate solution, removing water, drying, reduction to ruthenium metal in hydrogen flow, cooling in nitrogen flow, water flushing-mediated removal of potassium, impregnation with aqueous solution of BaNO3 and/or CsOH, and/or KOH followed by removal of water and pelletizing of catalyst.

EFFECT: increased activity of catalyst even when charging ruthenium in amount considerably below known amounts and increased resistance of catalyst to methane formation.

12 cl, 1 tbl

FIELD: chemical industry; methods and devices for production of ammonia from the synthesis gas.

SUBSTANCE: the invention is pertaining to the method and installation for production of ammonia from the synthesis gas. The method of production of ammonia provides for the catalytic reaction of the synthesis gas contracted in the appropriate compressor having several stages, each of which has the inlet and the outlet for the synthesis gas. The synthesis gas is purified by the liquid ammonia from contained in it water and carbon dioxide. At that at purification of the synthesis gas use the gas-liquid mixer, which is connected on the one hand to the outlet of the first stage of the compressor, or to the outlet of the intermediate stage of the compressor, and on the other hand - with the inlet of the second stage located behind the first stage, or with the inlet of the intermediate stage of the compressor, and has the section of the certain length with diminishing cross-section. Into the mixer in the axial direction feed in the forward flow the stream of the synthesis gas taken from the first stage of the compressor, or from the intermediate stage and the stream of the liquid ammonia, essentially the dehydrated synthesis gas is separated from the mixture flow coming out of the mixer and guide it into the second stage of the compressor, which is located behind the first stage or behind the intermediate stage. The technical result of the invention consists in the rise of the conversion outlet and in the decrease of the power inputs.

EFFECT: the invention ensures the increased conversion outlet and the decreased power inputs.

10 cl, 2 dwg

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