The way the joint modernization of the plant for producing ammonia and equipment for production of urea

 

The way the joint modernization of the plant for producing ammonia and urea involves the creation method comprising sequentially arranged sections for production of synthesis gas, the conversion of carbon monoxide, decarbonization, mechanisatie, a compression section, section synthesis of ammonia and urea, which has a section synthesis of carbamate and section decomposition of the carbamate, which are designed to receive a certain number of diluted carbamate and gas, consisting of hydrogen and nitrogen, which serves in existing sections of the synthesis of ammonia and urea. The method of implementation of the joint production of ammonia and urea and installation for implementing the method is based on the aggregation in a single technological cycle for the synthesis of ammonia, urea, which are connected with the section of the synthesis and decomposition of the carbamate. This upgrade allows you to significantly increase performance and reduce energy consumption in existing facilities intended for obtaining urea and ammonia, usually without any replacement or invalid increasing the load on the existing section of decarbonization, mechanisatie and compression. 3 S. and 17 C.p. f-crystals, 3 ill.

The invention in particular relates to a joint modernization of the plant for producing ammonia containing consistently located the section receiving the raw synthesis gas from which ammonia and which consists of carbon monoxide, hydrogen, and nitrogen, section conversion of carbon monoxide, the decarbonization section, section mechanisatie, a compression section, in which there is compression of the synthesis gas, and the section of the ammonia synthesis, and equipment for production of urea, containing consistently located the compression section, in which the compression of carbon dioxide, the section of the synthesis of urea and the section selection urea.

In the further description and the claims under the "upgrade" means a revision to an existing installation to improve her performance and received her results, in particular performance and/or conversion output, and reduce power consumption.

Under "joint modernization" in the invention refers to modernization, which affects at the same time as the existing installation to produce ammonia and the existing installation to obtain urea and aims to increase their productivity the RA synthesis), and with a slight revision of sections decarbonization, mechanisatie and compression sections.

The present invention also relates to a method joint production of ammonia and urea, as well as to an apparatus for implementing this method.

The present invention may find particular application in cases where an installation for producing ammonia and device for producing urea technologically combined with each other in a common setting, i.e. when all the resulting ammonia or at least the greatest part of it is converted into urea in the interaction with carbon dioxide obtained as a side product from the synthesis-gas.

As is known, upon receipt of the ammonia and urea increasingly felt the need to create systems with maximum performance and efficiency with minimal capital investment and production costs, and with minimal energy consumption.

The prior art presently known various methods of upgrading existing facilities to produce ammonia and urea, mainly based on the modification of the synthesis reactor, replacement vehicles, rabotaushii installing new devices in parallel to the existing.

For example, in application EP 0202454 method of modernization of the reactor for the synthesis of ammonia by replacement of the catalytic layers of the axial flow type catalyst layers radial-axial type, which increases the conversion output of the reactor, and hence the performance of the entire plant for producing ammonia.

In other ER-AND 0796244 method of modernization of the equipment for production of urea, which provides for the increase of the content of partially decomposed carbamate in aqueous solution circulating through the synthesis reactor. This upgrade helps to visibly reduce the amount of water pumped through the synthesis reactor, and to increase thereby the conversion output, and hence the performance of the installation.

One of the main problems that must be addressed while increasing performance combined in one process of the existing plants to produce ammonia and urea, is to simultaneously increase the performance of the sections located in the technological cycle before corresponding synthesis reactors.

In particular, section decarbonization, mechanisatie and compression section of the synthesis gas, as well as the compress is the Ktsia synthesis of urea, are the most difficult from the point of view of a possible increase their productivity so as to increase the flow rate of the reagents inevitably leads to overloading.

This problem becomes even more serious in the case when the existing installation already had been some modernization of the known methods, and above the equipment is already stretched to the limit of their capabilities.

In these cases, to improve the performance of various sections located before the corresponding synthesis reactors, the above-described methods of upgrading are only replacing existing devices devices more power or the installation of new devices, operating in parallel with them.

Such decisions are related, obviously, and with the increase in capital expenditures and increase in power consumption, and their practical implementation, in addition, can be extremely difficult.

Despite the ever-growing industry interest in the upgrading of existing facilities rather than creating new and improving their productivity while reducing energy costs and investments, it can be assumed that due to the above problems m sopostavimyh with the cost of creating new units. In addition, when upgrading facilities known ways of improving performance is usually accompanied by a decrease of the conversion output and thus increasing power consumption.

Summary of the invention the Task underlying the present invention is to develop a method of joint modernization of the plant for producing ammonia and equipment for production of urea, which was easily technically feasible and would improve the performance of plants at low energy consumption and low investment.

In accordance with the present invention this problem is solved using the method of the above-mentioned type which is characterized by the fact that for section synthesis of carbamate and the section of the decomposition of the carbamate, - provide for a system of pipelines with associated devices and equipment (hereinafter simply equipment or piping for feeding compressed to the necessary pressure synthesis gas containing carbon dioxide, hydrogen and nitrogen, in section synthesis of carbamate, for the pipeline to supply parts of ammonia, hydrogen and nitrogen obtained in the section of the ammonia synthesis section synthesis of key selection urea in section decomposition of carbamate, - provide a pipeline for supplying ammonia and carbon dioxide in vapour phase obtained in the decomposition section, the section of the synthesis of urea, - provide a pipeline for supplying the diluted carbamate in aqueous solution obtained in section decomposition of carbamate in section synthesis of carbamate,
- provide a pipeline for the supply of hydrogen and nitrogen obtained in section synthesis of carbamate in section synthesis of ammonia,
- provide a pipeline for supplying an aqueous solution of carbamate obtained in section synthesis of carbamate in section decomposition of carbamate and/or in the section of the synthesis of urea.

The advantage of the present invention is that it can significantly increase the plant capacity to produce ammonia and accordingly urea simple and effective way by the partial unification of the two plants with the elimination of the problems inherent in existing systems and associated equipment, located in front of the appropriate sections of the synthesis and virtually no impact on increasing the productivity of the installation.

In other words, the use of plants to produce ammonia and urea additional sections of synthesis and degradation of the ka reagents in sections decarbonization and mehanizaciyi and a compression section, who can work in the optimal mode.

In fact, the number of reagents that you want to improve the performance of plants to produce ammonia and urea, can be successfully obtained through the installation of additional sections of synthesis and decomposition of carbamate that operate independently from the existing sections decarbonization, mechanisatie and compression sections.

In particular, as is described in more detail below with reference to the drawings, the sections of the synthesis of carbamate allows you to receive a stream of gas containing hydrogen and nitrogen, which can be used as an additional reagents for the synthesis of ammonia, and the presence of a partition decomposition of carbamate allows you to receive a stream of gas containing ammonia and carbon dioxide, which can be used as an additional reagents for the synthesis of urea.

Another advantage achieved with the modernization of the method according to the present invention is that, using the additional section of the decomposition of the carbamate to the partial decomposition of at least one part of an aqueous solution of carbamate obtained in section selection urea, in section synthesis of carbamate can apply the solution soienoe carbon dioxide, that allows to reduce the molar ratio of N2O/CO2in this reactor, and consequently to increase the output of urea.

This feature of the proposed method is particularly effective not only because achieved in this case the productivity of the plant for producing urea, but because of the significant reduction in power consumption while increasing conversion output.

Moreover, the proposed method allows not only to maintain a low molar ratio of N2O/CO2in the reactor for the synthesis of urea, but also to effectively use at least part of the water contained in the aqueous solution of carbamate coming from the section selection urea, pumping it easy and economical way in section synthesis of carbamate to increase the absorption of carbon dioxide and obtain and maintain carbamate in aqueous solution without undesired crystallization.

In the present invention it is also proposed a method for simultaneous obtaining of ammonia and urea at the facility, has a section for production of synthesis gas which includes carbon monoxide, hydrogen and nitrogen, section conversion of carbon monoxide, the decarbonization section, section mechanisatie, compression the Intesa urea and section selection urea. This method differs in that in the process of getting the first part of the ammonia and urea stream of synthesis gas which includes carbon dioxide, hydrogen and nitrogen, is passed through the decarbonization section, mechanisatie and compression of the synthesis gas with getting compressed to the necessary pressure gas containing hydrogen and nitrogen, compressed to the necessary pressure gas containing hydrogen and nitrogen, is fed into the section of the ammonia synthesis, a portion of the ammonia obtained in the section of the ammonia synthesis, served with carbon dioxide coming from the decarbonization section, in the section of the synthesis of urea, and in the process of getting the second part of the ammonia and urea at least part of the aqueous solution of carbamate coming from the section selection urea, subjected to partial decomposition in the decomposition of the carbamate with getting the vapors of ammonia and carbon dioxide, and diluted carbamate in aqueous solution, the vapors of ammonia and carbon dioxide is fed to the section of the synthesis of urea, diluted carbamate in aqueous solution obtained in section decomposition of carbamate, serves in section synthesis of carbamate, compressed to the necessary pressure synthesis gas which includes carbon dioxide, hydrogen and nitrogen, is fed into the section of the synthesis under the synthesis of carbamate, ammonia is subjected to interaction with carbon dioxide in the synthesis of the carbamate with obtaining an aqueous solution of carbamate and stream containing hydrogen and nitrogen gas, an aqueous solution of carbamate served in the partition decomposition of carbamate and/or in the section of the synthesis of urea, the stream containing hydrogen and nitrogen gas is fed into the section of the ammonia synthesis.

The present invention relates also to the installation, designed to implement the above method, the joint production of ammonia and urea and characterized by the presence of
section to obtain a synthesis gas containing carbon monoxide, hydrogen, and nitrogen, section conversion of carbon monoxide, the decarbonization section, section mechanisatie, a compression section compressing the synthesis gas section of the ammonia synthesis, a compression section for compressing carbon dioxide section of the synthesis of urea, the section selection urea, section synthesis of carbamate and sections decomposition of carbamate,
equipment for compressed to the necessary pressure synthesis gas section synthesis of carbamate,
equipment for feeding parts of ammonia, hydrogen and nitrogen obtained in the section of the ammonia synthesis section synthesis of carbamate,
equipment for feeding at least part of the water is iaka and carbon dioxide in vapor phase, obtained in the decomposition section, the section of the synthesis of urea,
equipment for feeding diluted carbamate in aqueous solution from section decomposition of carbamate in section synthesis of carbamate,
equipment for feeding hydrogen and nitrogen obtained in section synthesis of carbamate in section synthesis of ammonia,
equipment for feeding an aqueous solution of carbamate obtained in section synthesis of carbamate in section decomposition of carbamate and/or in the section of the synthesis of urea.

Proposed in the present invention installations intended for the joint production of ammonia and urea, can be a newly created installation or, preferably, can be obtained by upgrading existing facilities, aimed at improving their performance and reducing energy consumption.

Other features and advantages of the present invention is described in more detail below with reference to the accompanying drawings on the example of some possible implementation of the proposed method of modernization in relation to the process of synthesis of urea.

Brief description of drawings
In Fig. 1 shows a diagram combined with each other in one process line existing simultaneously produce ammonia and urea, received by the facility upgrades in Fig.1 proposed in the present invention method.

In Fig.3 schematically shows one of the plots technological lines proposed in the present invention is installed, the scheme of which is shown in Fig. 2.

The preferred embodiment of the invention
In Fig.1 shows the basic elements are combined into one production line installations of conventional type, one of which is indicated by the number 1, is designed to produce ammonia, and the other designated position 2 for urea.

Installation 1 for ammonia and installation of 2 for urea are usually combined in one production line, in which at least a portion of the ammonia and carbon dioxide generated at the plant to produce ammonia, are used as reagents in the device for producing urea.

Installation 1 for ammonia contains the following consistently placed on technological cycle components: section 3 to obtain a synthesis gas containing carbon monoxide, hydrogen and nitrogen, section 4 of the conversion of carbon monoxide, section 5 decarbonization, section 6 of mechanisatie, the compression section 7, the compression of these things consistently for technological cycle components: a compression section 9 of the compression of carbon dioxide, section 10 of the synthesis of urea and section 11 of the selection urea.

At the entrance to the section 3 is a special equipment 12 and 13, is designed to feed into it, respectively, of the gas stream containing hydrocarbons and steam, and gas flow containing nitrogen, such as air or air enriched with oxygen.

This equipment includes, in particular, pipes, connecting pipes, pumps, compressors, ejectors and other well-known devices that are typically used in installations of this type and therefore do not require detailed description.

In General, unless otherwise specified in the description and the claims, the term "receiving" refers to piping, fittings, pumps, compressors, ejectors and other known devices which are used for pumping fluid or gas flow from one installation to another.

The term "hydrocarbons" in the description refers to the raw material serving as a source of hydrogen and carbon, such as methane or a mixture of liquid and/or gaseous hydrocarbons, in particular natural gas or naphtha. Under air, oxygen-enriched" in the description refers to the air, in which the molar content of oxygen exceeds arvae decomposition vapors of the hydrocarbons into hydrogen, carbon monoxide and carbon dioxide, and the degree of secondary reforming process in which the decomposition of vapors of hydrocarbons continues with the addition of nitrogen gas.

The resulting synthesis gas from sections 3 through respective pipes 14 comes in section 4 conversion of carbon monoxide.

In accordance with the present invention, the synthesis gas containing hydrogen, nitrogen and carbon monoxide, can be obtained in section 3 by any other known method, alternative steam reforming of hydrocarbons, such as simple partial catalytic oxidation with addition of oxygen-enriched air.

Section 4 may contain a high-temperature conversion stage and the low-temperature conversion stage, in which the conversion of carbon monoxide present in the synthesis gas, carbon dioxide.

Synthesis gas from sections 4 through the pipeline 15 is fed into the section 5 decarbonization, which stands out carbon dioxide, which through a set of equipment 16 is supplied to the compression section 9.

Synthesis gas comprising hydrogen and nitrogen, before submission of section 5 of the decarbonization section 8 synthesis of ammonia is pumped through the pipeline 17 through section argueta compression.

In section 7 mechanisatie possible traces remaining in the gas of carbon monoxide and/or carbon dioxide are easily converted into methane. In the compression section of the thus purified gas is compressed to a pressure of synthesis, which typically ranges from 100 to 200 bar.

Operating parameters pressure and temperature in sections 3-8 correspond to the parameters a typical installation for the synthesis of ammonia and is well known to specialists.

Equipment for the synthesis of ammonia under high pressure, is presented in the diagram in section 8, typically contains a reactor for the synthesis of ammonia and the corresponding device and apparatus for separating and recycling unreacted hydrogen and nitrogen in the synthesis reactor. In addition, in this section there are also compressors that are installed in the cooling circuit.

Stream, consisting mainly of ammonia, of section 8 by pipe 18 to send a whole section 10 of the synthesis of urea or if necessary, a portion of ammonia, even significant, can be withdrawn from the unit 1 via line 19 and to use it for a variety of purposes. In the absence of the need to obtain urea entire ammonia from section 8 is taken from the unit 1 via line 19.

The flow of gaseous carbon dioxide is 0, where it reacts with ammonia, forming a reaction mixture comprising urea, carbamate and free ammonia in aqueous solution.

The circuit flowing at high temperature and high pressure synthesis of urea, presented in the diagram in section 11, typically contains one or more reactors for the synthesis of urea and in accordance with the features of the process can have one or more units for evaporation and condensation of light fractions of hydrocarbons.

Thus obtained reaction mixture through the pipeline 21 is fed into the section 11 selection urea, which is obtained in section 10 of the urea is excreted from an aqueous solution of carbamate and liquid ammonia and excreted from the unit 2 to line 22, not shown in the diagram section for further concentration.

Section selection urea usually contains one or two apparatus for the decomposition of carbamate, working respectively with an average absolute (about 18 bar) or middle and low absolute pressure (4 bar), and the corresponding carbamate condensers.

Carbamate and free ammonia in aqueous solution obtained in section 11 selection urea, eventually pumped through pipelines is seeking a very large amount of water, which reduces the conversion output this section.

In Fig. 2 shows a schematic setup for the joint production of ammonia and urea, the resulting modernization of the known installation according to Fig.1 proposed in the present invention method.

In the form shown in Fig. 2 installation elements, structurally and functionally equivalent to the corresponding elements of the units 1 and 2 in Fig.1, are denoted by the same positions and will not be re-considered.

Proposed in the invention upgrade improves the performance units 1 and 2 without overloading sections located in a production cycle to sections 8 and 10 of the synthesis, and, in particular, sections 5-7 and 11, and also compressor cooling circuit in section 8.

To this end, in this embodiment of the invention in the above-described installation added the following sections and piping with appropriate devices, not necessarily in the order in which they are listed below:
section 24 synthesis of carbamate,
section 25 of the decomposition of the carbamate,
pipe 26 for supplying compressed to the necessary pressure synthesis gas section 24 synthesis of carbamate,
pipe 27 for supplying part of the flow comprising ammonia, hydrogen and nitrogen, polycaste flow of an aqueous solution of carbamate from section 11 of the selection urea 11 in section 25 of the decomposition of the carbamate,
pipe 29 to the feed stream containing ammonia and carbon dioxide in vapor phase from section 25 of the decomposition of the carbamate in section 10 of the synthesis of urea,
the pipeline 30 to the feed stream containing the diluted carbamate in aqueous solution, the partition decomposition of carbamate in section 24 synthesis of carbamate,
pipe 31 for supplying gas stream containing hydrogen and nitrogen, from section synthesis of carbamate in section 8 of ammonia synthesis, and
pipe 32 to the feed stream containing the aqueous solution of the carbamate from section 24 synthesis of carbamate in section 25 of the decomposition of the carbamate.

This scheme is partial integration of existing systems can increase the capacity of plants to produce ammonia and urea without overloading existing partitions decarbonization, mechanisatie and compression sections (including the compressor of the cooling circuit section synthesis of ammonia), which typically operate at the limit of their capabilities and limit the extent of possible productivity throughout the process.

In other words, due to the proposed invention method on existing installations, you may receive an additional amount of ammonia and urea use and the normal of the method described above in the installation according to Fig.1, in the preferred embodiment, is provided by the following operations:
- supply at least part of the flow of an aqueous solution of carbamate from section 11 of the selection urea (pipeline 28) consisting of partial decomposition of carbamate processing section 25 decomposition of the carbamate with receiving a stream of ammonia and carbon dioxide in vapour phase (line 29) and the flow of the diluted carbamate in aqueous solution (line 30),
the flow of ammonia and carbon dioxide in vapour phase (pipeline 29) in section 10 of the synthesis of urea,
- flow (pipeline 30) flow of diluted carbamate in aqueous solution obtained after partial decomposition of carbamate in section 24 synthesis of carbamate,
- compressed to the necessary pressure synthesis gas (by pipeline 26) in section 24 synthesis of carbamate,
- flow part of the flow of ammonia, hydrogen and nitrogen obtained in section 8 synthesis of ammonia (by pipeline 27) in section 24 synthesis of carbamate,
- carrying out a reaction between ammonia with carbon dioxide in the section 24 of the synthesis of the carbamate with receiving a flow of an aqueous solution of carbamate (line 32) and the gas stream containing hydrogen and nitrogen (line 31),
- supply vododara and nitrogen gas (by pipeline 31) in section synthesis of ammonia.

In modernized in this way the installation in sections 8 and 10 through the piping 31 and 29 receives an additional amount of reagents required for the synthesis, respectively, ammonia and urea.

Obviously, this upgrade eliminates the need to increase the load on the existing section of decarbonization and mechanisatie or compression section that will work optimally with low energy consumption. Moreover, proposed in the present invention upgrade does not require the installation of additional units of this type, which consume a lot of energy and require a large investment.

On modernized in this way the installation, which has been added is shown in Fig.2 sections and pipes with the appropriate devices and equipment, was received additional amounts of reagents, allowing for comparison with setting up its modernization to increase the production of ammonia and urea by 10-50%, preferably 30-45%, and obtain the most satisfactory results in terms of investment and energy consumption.

Moreover, if existing installations 1 and 2 were somehow upgraded (WPI is the first section, the proposed method allows you to transfer part of the load on additional sections, thus relieving the existing partitions that will work optimally. This method allows to further reduce the amount of consumed throughout the installation of energy.

To achieve maximum conversion of the output section 10 of the synthesis of urea (reduction of the molar ratio2O/CO2and thereby to minimize the energy consumption in this section, preferably by pipeline 32 to pump in section 25 of the decomposition of the carbamate entire flow of carbamate in aqueous solution obtained in section 24.

In the same vein, preferably the entire flow of carbamate in aqueous solution from section 11 of the selection urea to apply section 25 of the decomposition of the carbamate.

In the alternative in section 10 of the synthesis of urea 10 pipeline 33 (shown in Fig. 2 by the dashed line) to apply the whole or at least part of the flow of carbamate and line 23 (also shown in Fig.2 by the dashed line) to apply part of the flow of carbamate in aqueous solution.

It is advisable stream of synthesis gas feeding pipeline 26 in section synthesis of carbamate in a compressed to an appropriate pressure, so work 8 synthesis of ammonia.

With this purpose in accordance with the preferred option proposed in the invention method of modernization provides for the use of additional compression section 34 and the pipe 26, through which the synthesis gas is supplied to the additional compression section 34, and then in section synthesis of carbamate.

Compression section 34 may have one or more compressors of conventional type, which provide the necessary compression and additional reagents required for the synthesis of ammonia, and the extra amount of carbon dioxide used for the synthesis of urea.

In accordance with the shown in Fig.2 a variant of the method proposed modernization of the pipeline 26, intended for the supply of the synthesis gas section 24 synthesis of carbamate has the equipment (for example, not shown in the drawing, control valves for selecting part of the synthesis gas from section 4 conversion of carbon monoxide and pumping it through a pipeline 15 in section 5 decarbonization.

In other words, in this case, the stream containing carbon dioxide, hydrogen and nitrogen gas, which must fall within section 24 synthesis of carbamate, is taken from the installation to section 5 decarbonization.

The stream of gas, which doeth the amount of energy required for its compression to the desired pressure. It should be noted that this feature applies equally to the flow of the reagents supplied in section 8 synthesis of ammonia and the flow of carbon dioxide, which is given in section 10 of the synthesis of urea.

Particularly good results can be obtained in the case when part of the synthesis gas coming from section 4 conversion of carbon monoxide in section 24 synthesis of carbamate, is from 10 to 50%, preferably from 30 to 45% of the total amount of synthesis gas at the outlet of section 4 of the conversion of carbon monoxide.

The same good results can be obtained even when the amount of gas flowing through the pipeline 27 of section 8 of the ammonia synthesis 8 in section synthesis of carbamate, is in the range from 10 to 50%, preferably from 30 to 45% of the total amount of gas containing ammonia, hydrogen and nitrogen obtained in section 8 synthesis of ammonia.

With the increasing productivity of plants to produce ammonia and urea and simultaneous selection of additional amounts of reactants from the gas flow directed to the existing partition, decarbonization, as shown for example in Fig.2, it may be appropriate instead of the excessive load increase GU section for production of synthesis gas, containing carbon monoxide, hydrogen and nitrogen.

In this variant proposed in this invention upgrade includes another stage, which consists in the creation of additional sections 35 to produce synthesis gas from the pipe 36 for supplying received in the additional section 35 synthesis gas section of the conversion of carbon monoxide.

The example shown in Fig. 2, based on the assumption that section 4 of the conversion of carbon monoxide can work with a significant increase in load. In principle, however, you can instead set the additional section of the conversion of carbon monoxide (not shown), eliminating the need to supply an additional amount of synthesis gas in section 4.

Section 35, designed to produce synthesis gas may contain one or several stages of reforming or preferably a single stage catalytic partial oxidation.

Additional amounts of carbon monoxide, hydrogen and nitrogen can be obtained by filing a section 35 piping 37 and 38, respectively, hydrocarbons and nitrogen-containing gas, such as air or preferably oxygen-enriched air.

It should be noted that the present invention is in section 24 synthesis of carbamate gas, containing carbon dioxide, hydrogen and nitrogen.

The scheme depicted in Fig.3, in more detail reflects additions and changes to the process line in accordance with the proposed invention by way of modernization.

It is shown in Fig.3 the elements of the unit for the joint production of ammonia and urea, which are structurally and functionally equivalent elements shown in Fig. 2, are denoted by the same positions and therefore are not further described.

For simplification in Fig.3 schematically shows only the part shown in Fig. 2 installation for the joint production of ammonia and urea, as the other sections of this installation does not play a significant role from the point of view of being present invention.

In addition, reference is shown in Fig.3 pipelines connecting various parts of the device, are made only when there is a special need for this. By themselves, these pipelines have the usual, well-known to specialists in the design.

In Fig. 3 position 39 marked the pipeline through which the flow of water from the section of the urea concentration (not shown) installed to obtain urea is fed into the section 24 synthesis of carbamate.

This recharge (with the and carbamate, exceeds the amount of water contained in the flow of carbamate, diluted in aqueous solution, flowing from section 25 of the decomposition of the carbamate (pipeline 30).

With this method of feeding is unnecessary to use water from an external source, since the entire water requirement provides water received in one of the sections located outside the reactor for the synthesis of urea, resulting in noticeable savings in current spending.

The installation is made in accordance with a preferred variant of the invention has a connecting section 8 synthesis of ammonia and section 24 synthesis of carbamate pipe 27, which in section synthesis of carbamate is ammonia in the vapor phase, immediately interact with the existing section 24 carbon dioxide, thereby enabling the synthesis of carbamate.

Before filing section 8 synthesis of ammonia by pipeline 31 containing hydrogen and nitrogen gas it is advisable to properly clean. For this purpose shown in Fig.3, the apparatus 40 and 41 of conventional type, in which there is mehanizacija and drying of the gas.

In particular, in the drying apparatus 41, the flow of hydrogen - and nitrogen-containing gas is dehydrated what about the liquid ammonia is fed into the drying device 41 together with a stream of hydrogen - and nitrogen-containing gas from the pipeline 31, in which he gets from the pipeline 42.

In the drying apparatus, the water contained in the stream of hydrogen and nitrogen, absorbed ammonia, forming an aqueous solution of ammonia, which is then pumped through the pipes 43 and 32 in section 25 of the decomposition of the carbamate, while dehydrated stream of hydrogen and nitrogen through the conduit 31 is fed into the section 8 synthesis of ammonia.

In the installation shown in Fig.3, between the section 24 synthesis of carbamate and section 25 of the decomposition of the carbamate is selected separator 44, designed to remove the pipe 45 from an aqueous solution of carbamate remaining in it and polluting it traces of hydrogen and nitrogen.

Section 25 of the decomposition of the carbamate may be one, as shown in Fig.3, is designed to decompose the carbamate apparatus, such as desorber, or two or more working consistently at different temperature and pressure of desorbers.

Preferable example according to Fig.3 is a variant with a single apparatus for the decomposition of carbamate operating at the same temperature and the same pressure, and that section 10 of the synthesis of urea.

In turn, section 24 synthesis of carbamate can be performed in a single reaction chamber, to which suitable pipes 26, 27 and 30, or more of asana in Fig.3.

In the latter case section 24 is performed in a single apparatus with three reaction chambers 46, 47 and 48 separated by two absorbers 49 and 50, for example, film type.

The first reaction chamber 46 is located in the lower part of the section 24 and is connected with the pipe 26, through which it enters the stream containing hydrogen, nitrogen and carbon dioxide gas, and the pipe 32, whereby an aqueous solution of carbamate obtained in section 24, is given in section 25 of the decomposition of the carbamate.

The second reaction chamber 47 is located in the Central part of the section 24 and is connected with the pipe 27, which in her section 8 synthesis of ammonia flows of ammonia, hydrogen and nitrogen.

The third reaction chamber 48 located in the upper part of the section 24 and is connected by pipes 39 and 30, by which it is served, respectively, water and diluted carbamate in aqueous solution, and also with the conduit 31, through which the hydrogen - and nitrogen-containing gas is supplied from section 24 synthesis of carbamate 24 section 8 synthesis of ammonia.

The first absorber 49 is located between the first 46 and second 47 cameras and, for example, consists of many tubes connected by their ends to the first and second reaction chambers.

Second aswome ends with the second and third reaction chambers.

This design section 24 synthesis of carbamate for all its simplicity, small size and low cost of manufacture and operation allows to create conditions for proceeding with high speed and efficiency of the reaction of interaction between ammonia and carbon dioxide.

The flow of the diluted carbamate in aqueous solution from section 25 of the decomposition of the carbamate preferably be submitted in the third reaction chamber 48 through the conduit 30, which is located next to the second absorber 50.

However, satisfactory results can be achieved in the case when the flow of diluted carbamate in aqueous solution is fed to the third reaction chamber 48 located in the upper part of the section 24, or the second reaction chamber 47 that is adjacent to the second absorber 50, as shown in dotted lines in Fig.3.

The third chamber 48, which operates mainly in the adiabatic regime, has a large number of perforated horizontal plates of conventional type, which allow to increase the output of the absorbed product.

In having such a construction of section 24 synthesis of carbamate in Fig.3 stream containing hydrogen, nitrogen and carbon dioxide gas is supplied by pipeline 26V which it flows in the direction opposite to the direction of flow of ammonia and an aqueous solution of carbamate derived from the second chamber 47.

In this area the main part of the carbon dioxide reacts with free ammonia, preferably in the vapor phase and in the liquid phase, forming a carbamate, which is collected in the chamber 46.

The gas stream emerging from the first absorber 49, in the chamber 47 is mixed with a stream of ammonia, hydrogen and nitrogen, flowing from section 8 synthesis of ammonia by pipeline 27 and into the filled tubes the area of the second absorber 50, in which the main part of the carbon dioxide and ammonia in the vapor phase is absorbed in dilute ammonia solution, resulting from the third chamber 48.

In the third chamber 48 into which the pipeline respectively 39 and 30 water comes from the section of the urea concentration and the flow of an aqueous solution of carbamate from section 25 of the decomposition of the carbamate, is the final distillation of the residual ammonia and carbon dioxide.

The present invention allows, in particular, to ensure that the output from the third chamber 49 (line 31) in a stream of hydrogen and nitrogen molar concentration of residual ammonia was about 1%, and the molar content of residual duoc the indirect heat exchange of the cooling fluid (e.g., water), which is preferably pumped through the outer casing absorbers 49 and 50.

This method of cooling allows to maintain the temperature in the section 24 synthesis of carbamate, in which the tubes of the absorbers is not happening crystallization carbamate.

For example, the absolute pressure in the section of the synthesis of the carbamate may be from 140 to 200 bar, preferably 180 bar, and the temperature can range from 110 to 150oC, preferably 130oC.

Installation for the joint production of ammonia and urea, modernized proposed invention may be made in the form of re-manufactured and assembled from new equipment installation.

Such installation must have all sections and pipelines (with the necessary devices and equipment), shown in Fig.2. Distinctive features such installation upon receipt of the ammonia and urea specified in paragraphs 15-20 of the claims.

All the advantages characteristic of modernized proposed in the invention by way of the existing plants to produce ammonia and urea, will be created again and made in accordance with the present invention set the

The installation is made in accordance with the present invention, regardless of whether it is a modernized appropriate method to an existing installation, re-created, you can get the ammonia and urea proposed in the invention method, the distinctive features of which are listed in PP 7-14 claims.

Example.

It is assumed that there is a need for simultaneous modernization of the plant for producing ammonia and equipment for production of urea, the dimensions of the main sections which may not be increased or they cannot be improved by conventional methods. The essential point is that this upgrade is to improve the performance of these facilities.

However, the performance of the units should be increased in the following amounts: for NH3- from 1300 to 2000 metric tons (MT) per day; the device for producing urea from 2300 to 3500 MT/day.

If we are talking only about how to improve performance, the present invention allows to achieve the required increase in performance (700 MT/day NH3and 1200 MT/day urea simple volume of different types of plants for the synthesis of urea and the same unit for the production of ammonia, in particular:
in the first case was used for urea based on the desorption process using a CO2,
in the second case was used for urea based on the process of imagesarray (ammonia).

In the first case section synthesis urea synthesis reactor) is characterized by the following working conditions:
the pressure of 140-150 bar,
- temperature 183-188oWith,
- the molar ratio of NH3/CO2about 3,
- the molar ratio of N2O/CO2about 0.5,
- conversion exit=60%.

In this embodiment, the urea solution, taken out of the synthesis reactor is flushed in the usual manner in desorber using CO2. The obtained vapors are partially condensed in the carbamate condenser and fed to the synthesis reactor together with pumped from the section selection of the urea aqueous solution of carbamate.

The above-described method for simultaneous modernization of the plant for producing ammonia and equipment for production of urea in accordance with the present invention to increase the performance of the plant for producing urea to 3500 MT/day. This section of the synthesis of urea poderi/CO2about 3,
- the molar ratio of N2O/CO2about 0.15,
- conversion exit=65%.

It should be noted that in addition to the noticeable increase in performance due to reduction in the molar ratio of N2O/CO2from 0.5% to 0.15% it was possible to increase the conversion yield from 60% to 65%, thus providing a corresponding savings in energy consumption.

In the second case section synthesis urea synthesis reactor) is characterized by the following working conditions:
the pressure of 140-150 bar,
- temperature of 185-190oWith,
- the molar ratio of NH3/CO2about 3.2,
- the molar ratio of N2O/CO2about 0.5,
- conversion exit=62%.

Coming from the synthesis reactor a solution of urea is cleared in desorber the usual way mode imagesarray. The obtained vapors are condensed in the first condenser, and the condensate is pumped back to the reactor. The urea solution coming from desorber consistently is distilled at a pressure of 18 bar secondary pressure and at a pressure of 4 bar in the low pressure stage and passes into the section of the vacuum concentration to obtain eventually cleared condensed in the second condenser in the presence of a circulating aqueous solution of carbamate and take place in the distillation column, which is obtained as the head product of pure NH3after the condensation is pumped back to the reactor, and taken from the bottom of the column an aqueous solution of carbamate merges into the first capacitor and it is pumped back to the reactor.

Joint modernization of a plant for producing ammonia and equipment for production of urea, implemented in accordance with the present invention, allows to increase the performance of the plant for producing urea to 3500 MT/day. This section of the synthesis of urea was supported by the following conditions:
the pressure of 140-150 bar,
- temperature of 185-190oWith,
- the molar ratio of NH3/CO2about 3.2,
- the molar ratio of N2O/CO2about 0.2,
- conversion exit=65%.

And in this case, in addition to the performance improvement has been achieved in increasing the conversion yield and reducing energy consumption.


Claims

1. The way the joint modernization of the plant for producing ammonia containing consistently located the section receiving the raw synthesis gas from which ammonia and which consists of anizatio, the compression section, in which there is compression of the synthesis gas, and the section of the ammonia synthesis, and equipment for production of urea, containing a compression section, in which the compression of carbon dioxide, the section of the synthesis of urea and the section selection urea, characterized in that the include section of the synthesis of the carbamate and the section of the decomposition of the carbamate, provide for a system of pipelines with associated devices and equipment for feed stream compressed to the necessary pressure synthesis gas containing carbon dioxide, hydrogen and nitrogen, in section synthesis of carbamate, provide a pipeline for supplying part of ammonia, hydrogen and nitrogen, received in the section of the ammonia synthesis section synthesis of carbamate, provide a pipeline for supplying at least part of the aqueous solution of the carbamate from the section selection urea in section decomposition of carbamate, provide a pipeline for supplying vapors of ammonia and carbon dioxide obtained in the decomposition of the carbamate in the section of the synthesis of urea, provide a pipeline for supplying the diluted carbamate in aqueous solution obtained in section decomposition of carbamate in section synthesis of carbamate provide Truboprovod pipeline for supplying an aqueous solution of carbamate, obtained in section synthesis of carbamate in section decomposition of carbamate and/or in the section of the synthesis of urea.

2. The method according to p. 1, characterized in that also provide additional compression section and provide a pipeline for feeding the synthesis gas containing carbon monoxide, hydrogen and nitrogen, in this additional compression section, and from there into the partition of the synthesis of the carbamate.

3. The method according to p. 1, characterized in that the piping for feeding the synthesis gas containing carbon monoxide, hydrogen and nitrogen, in section synthesis of carbamate has a device for selecting a portion of the synthesis gas supplied from the section conversion of carbon monoxide, and feed this part of the synthesis gas in the decarbonization section.

4. The method according to p. 3, characterized in that it also provides additional section to obtain a synthesis gas containing carbon monoxide, hydrogen and nitrogen, and provide a pipeline for feeding the synthesis gas containing carbon monoxide, hydrogen and nitrogen obtained in this additional section, section conversion of carbon monoxide.

5. The method according to p. 1, characterized in that section synthesis of carbamate has a first chamber which communicates with the pipe for feeding the synthesis gas, is to supply an aqueous solution of carbamate, obtained in section synthesis of carbamate in section decomposition of carbamate and/or in the section of the synthesis of urea, the second chamber, which communicates with the pipe for feeding ammonia, hydrogen and nitrogen gas obtained in the section of the ammonia synthesis section synthesis of carbamate, a third chamber which communicates with the pipe for supplying the diluted carbamate in aqueous solution in section synthesis of carbamate and, respectively, with the pipeline to supply containing hydrogen and nitrogen gas obtained in section synthesis of carbamate in the section of the ammonia synthesis, the first absorber film type, located between the first and second chambers and containing a number of tubes, which open their opposite ends are communicated respectively with the first and second chambers, the second absorber film located between the second and third chambers and containing a number of tubes, which open their opposite ends are communicated respectively with the second and third chambers.

6. The method according to p. 1, characterized in that also provide a pipeline to supply water from a section of the concentration of urea in section synthesis of carbamate.

7. Way to simultaneously produce ammonia and urea in the us is, section conversion of carbon monoxide, the decarbonization section, section mechanisatie, a compression section compressing the synthesis gas, the section of the ammonia synthesis, a compression section for compressing carbon dioxide, the section of the synthesis of urea and the section selection urea, characterized in that in the process of getting the first part of the ammonia and urea stream of synthesis gas, comprising carbon monoxide, hydrogen and nitrogen, is passed through the decarbonization section, mechanisatie and compression of the synthesis gas with getting compressed to the necessary pressure gas containing hydrogen and nitrogen, compressed to the necessary pressure gas containing hydrogen and nitrogen, serves in section synthesis of ammonia and part of the ammonia obtained in the section of the ammonia synthesis, served with carbon dioxide coming from the decarbonization section, in the section of the synthesis of urea, and in the process of getting the second part of the ammonia and urea at least part of the aqueous solution of carbamate coming from the section selection urea, subjected to partial decomposition in the decomposition of the carbamate with getting the vapors of ammonia and carbon dioxide, and diluted carbamate in aqueous solution, the vapors of ammonia and carbon dioxide is fed to the section of the synthesis of urea, razbavlennyi to correct pressure synthesis gas, comprising carbon monoxide, hydrogen and nitrogen, is fed into the section of the synthesis of the carbamate, the portion of the stream containing ammonia, hydrogen and nitrogen obtained in the synthesis of ammonia, is fed into the section of the synthesis of carbamate, ammonia is subjected to interaction with carbon dioxide in the synthesis of the carbamate with obtaining an aqueous solution of carbamate and stream containing hydrogen and nitrogen gas, an aqueous solution of carbamate served in the partition decomposition of carbamate and/or in the section of the synthesis of urea and the stream containing hydrogen and nitrogen gas is fed into the section of the ammonia synthesis.

8. The method according to p. 7, characterized in that also carry out the compression of the synthesis gas, comprising carbon dioxide, hydrogen and nitrogen in the additional compression section before submitting it to the section of the synthesis of the carbamate.

9. The method according to p. 7, characterized in that the synthesis gas, comprising carbon monoxide, hydrogen and nitrogen and which is fed to the section synthesis of carbamate, contains part of the synthesis gas, which is supplied from the section conversion of carbon monoxide in the decarbonization section.

10. The method according to p. 9, characterized in that they also carry the burning flow of hydrocarbons from the additional amount of synthesis gas, sodergard, hydrogen and nitrogen, is supplied from the section of the partial oxidation of hydrocarbons in the section conversion of carbon monoxide.

11. The method according to p. 7, characterized in that the flow taken from the section of the ammonia synthesis, contains a pair of ammonia.

12. The method according to p. 7, characterized in that the amount of gas taken from the section of the ammonia synthesis, is from 10 to 50%, preferably from 30 to 45% of the total stream containing ammonia, hydrogen and nitrogen gas obtained in the synthesis of ammonia.

13. The method according to p. 9, characterized in that the portion containing carbon monoxide, hydrogen and nitrogen synthesis gas taken from the section conversion of carbon monoxide and supplied in section synthesis of carbamate, is from 10 to 50%, preferably from 30 to 45% of the total flow of the synthesis gas taken from the section conversion of carbon monoxide.

14. The method according to p. 7, characterized in that it also provides for the supply of water taken from the section of the concentration of urea in section synthesis of carbamate.

15. Installation for simultaneous recovery of ammonia and urea containing section for production of synthesis gas from which ammonia and which consists of carbon monoxide, hydrogen, and nitrogen, section conversion of carbon monoxide, the decarbonization section, section mennow section, which is the compression of carbon dioxide, the section of the synthesis of urea, the section of the synthesis of the carbamate and the section of the decomposition of the carbamate, the pipeline for flow of compressed to the proper pressure synthesis gas containing carbon monoxide, hydrogen and nitrogen, in section synthesis of carbamate, a pipeline for supplying part of ammonia, hydrogen and nitrogen obtained in the section of the ammonia synthesis section synthesis of carbamate, a pipeline for supplying at least part of the aqueous solution of the carbamate from the section selection urea in section decomposition of carbamate, a pipeline for supplying vapors of ammonia and carbon dioxide obtained in the decomposition of the carbamate, in section synthesis of urea, a pipeline for supplying the diluted carbamate in aqueous solution obtained in section decomposition of carbamate in section synthesis of carbamate, a pipe for supplying hydrogen and nitrogen obtained in section synthesis of carbamate in the section of the ammonia synthesis, a pipeline for supplying an aqueous solution of carbamate obtained in section synthesis of carbamate in section decomposition of carbamate and/or in the section of the synthesis of urea.

16. Installation according to p. 15, characterized by the presence of additional compression section and a pipeline for supplying the synthesis gas, containing the of bamaca.

17. Installation according to p. 15, characterized in that the piping for feeding the synthesis gas containing carbon monoxide, hydrogen and nitrogen, in section synthesis of carbamate contains a device for selecting a portion of the synthesis gas supplied from the section conversion of carbon monoxide, and feed this part of the synthesis gas in the decarbonization section.

18. Installation under item 17, characterized by the presence of additional sections to obtain a synthesis gas containing carbon monoxide, hydrogen and nitrogen, and a pipeline for supplying the synthesis gas containing carbon monoxide, hydrogen and nitrogen obtained in this additional section, section conversion of carbon monoxide.

19. Installation according to p. 15, characterized in that section synthesis of carbamate contains a first chamber which communicates with the pipe for feeding the synthesis gas containing carbon dioxide, hydrogen and nitrogen, in section synthesis of carbamate and, respectively, with a pipe for feeding an aqueous solution of carbamate obtained in section synthesis of carbamate in section decomposition of carbamate and/or in the section of the synthesis of urea, the second chamber, which communicates with the pipe for feeding ammonia, hydrogen and nitrogen gas obtained in the synthesis of ammonia, in section synthesis to the thief in section synthesis of carbamate and accordingly, with the pipeline to supply containing hydrogen and nitrogen gas obtained in section synthesis of carbamate in the section of the ammonia synthesis, the first absorber film located between the first and second chambers and containing a number of tubes, which open their opposite ends are communicated respectively with the first and second chambers, and a second absorber film located between the second and third chambers and containing a number of tubes, which open their opposite ends are communicated respectively with the second and third chambers.

20. Installation according to p. 15, characterized by the presence of a pipeline to supply water from a section of the concentration of urea in section synthesis of carbamate.

 

Same patents:
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The invention relates to a method for production of ammonia from synthesis gas and Converter for its implementation

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

FIELD: organic chemistry, in particular urea producing from carbon dioxide from carbon and ammonia incorporated with production of syngas followed by conversion thereof to ammonia.

SUBSTANCE: claimed method includes step of syngas production containing carbon dioxide for ammonia synthesis; step of syngas conversion to ammonia; reaction of ammonia with carbon dioxide in syngas to produce ammonium carbamate; further conversion thereof to produce urea. Method also includes washing of starting syngas with ammonia aqueous solution, removing of ammonia excess from washed syngas by washing with water and recovering of ammonia aqueous solution. Washed with water syngas is purified by removing of rest water and ammonia and converted to ammonia. In syngas washing step with ammonia aqueous solution washed syngas stream is cooled and ammonia is isolated in liquid form. Further syngas is purified from rest water and ammonia and obtained stream is recycled into washing step.

EFFECT: improved incorporated process for production of carbon dioxide and ammonia reagent from syngas and production of urea via ammonium carbamate intermediate.

1 ex, 2 dwg, 6 tbl

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