Method of combined methanol and ammonia production from initial hydrocarbon raw material

FIELD: chemistry.

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

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

7 cl, 1 dwg, 1 tbl

 

The present invention relates to a joint production of methanol and ammonia, and more particularly to a method for simultaneous production of methanol and ammonia from a source of hydrocarbon raw materials.

Modern methods for co-production of methanol and ammonia include generally parallel processes that use shared reforming section to produce synthesis gas. The synthesis gas is separated into separate parallel streams, one of which is used for methanol synthesis and the other for the synthesis of ammonia. The joint production of methanol and ammonia can also be carried out sequentially or one after the other, when the synthesis gas obtained in the reforming section, first converted to methanol, and unreacted gas containing oxides of carbon and hydrogen, is then used for the synthesis of ammonia. The necessary shift reaction with steam and/or steps for removing carbon dioxide from a stream of synthesis gas, which thus entails emissions of CO2in the atmosphere, and the cost of expensive and complicated equipment units for the implementation of the shift reaction and removal of carbon dioxide.

In US-A-2007/0299144 in one embodiment, the disclosed method in which methanol and ammonia are produced in parallel and independently of the total flow of the synthesis gas and without the production of urea. Because the ku urea is not performed, there is no need to take carbon dioxide for the synthesis of urea. The carbon monoxide in the stream of synthesis gas used for the synthesis of ammonia, is converted into carbon dioxide, and the reforming is carried out in a basic oxygen furnace reactor, the oxygen will be produced from the Air Separation Unit.

In U.S. patent US 6106793 describes the way in which methanol and ammonia are produced in parallel and independently. The gas obtained in the secondary section of the reformer is cooled by indirect heat exchange with a gas containing methane, and steam from the second primary reforming section, to obtain the synthesis gas ammonia production. The heated gas reacts to produce synthesis gas for methanol production, containing CO, CO2and H2.

In European patent application EP-A-0553631 disclosed a process for the production of methanol, accompanied by the production of ammonia. Before conducting the synthesis of ammonia, unreacted synthesis gas for methanol production comes to the stage of removal of CO2and add nitrogen. Air Separation Unit provides nitrogen for N2-add and oxygen oxygen oxygen secondary reformer, located at the front section of methanol synthesis.

In JP-A-2000063115 describes the process of co-production of methanol and ammonia. In the reforming section of the secondary reformer is purged with air, and dioxi the carbon is removed from the synthesis gas, to adjust the composition of the synthesis gas. There is no need for the shift reactor to convert CO in the CO2.The synthesis gas used for the production of methanol in the process, in which a recirculation flow of the product. Process gas leaving sections of methanol, subjected to ketanazii and then used for the production of ammonia.

The present invention is to provide a process of co-production of methanol and ammonia, which is simpler than a modern way, and which at the same time makes possible a minimum separation of carbon dioxide into the atmosphere.

Another objective of the present invention is to provide a process of co-production of methanol and ammonia, which is simpler and cheaper than modern methods both in terms of capital and operating costs.

These and other problems are solved by using the present invention.

According to this, we provide a process of co-production of methanol and ammonia from a source of hydrocarbons containing a consecutive stages:

(a) obtaining synthesis gas methanol containing hydrogen, nitrogen and carbon dioxide by steam reforming of the original hydrocarbons in the initial stage of reforming and then at the WTO the primary stage of reforming air blast;

(b) catalytic conversion of carbon oxides and hydrogen synthesis gas for methanol production at forward methanol synthesis and abstraction facing product containing methanol, and the exhaust gas stream containing nitrogen, hydrogen and unconverted carbon oxides;

(c) obtaining synthesis gas ammonia production without the use of shift reaction with steam and without removal of carbon dioxide by removing unconverted carbon oxide gas stream of step (b) at the stage catalytic ketanazii and abstraction synthesis gas of ammonia gas having a molar ratio of H2:N2equal to 3:1;

(d) catalytic conversion of nitrogen and hydrogen synthesis gas production of ammonia synthesis ammonia and abstraction facing product containing ammonia and the exhaust gas stream containing hydrogen, nitrogen and methane.

Used herein, the term "carbon oxide" means the components of carbon monoxide and carbon dioxide.

Used here on the stage (C) the term "removal of unconverted carbon oxides on stage catalytic ketanazii means the conversion of the unconverted carbon oxides to methane. This obviously differs from the removal of carbon dioxide through the use of absorbers with the release of sour gas, is AutoRAE the present invention eliminates.

Accordingly, when used herein, the term "removal of carbon dioxide" means a very expensive stage of removal of CO2in the form of cleaning sour gas, such as a conventional cleaning MDEA and carbonates.

Used herein, the term "primary stage of reforming" means reforming carried out in a conventional steam methane reformer (SMR), i.e. in the tubular reformer, in which the heat required for the endothermic reforming, is provided by burners, such as burners located along the walls of the tubular reformer.

Used herein, the term "secondary stage reforming with air-blown" means reforming carried out in the autothermal reformer or reactor using air for the catalytic partial oxidation.

Used herein, the term "forward-phase methanol synthesis" means that methanol is at least one catalytic reactor operating in the single passage mode, i.e. without substantial recirculation (not more than 5%, i.e. less than 5%, often 0%) volume flow of any gas generated during the synthesis of methanol, at least one of the methanol reactor for methanol synthesis, in particular a gas stream containing hydrogen and unreacted oxides of carbon.

Preferably, the source is e hydrocarbon feedstock is natural gas, for example, in the form of liquefied natural gas (LNG) or substitute natural gas (SNG).

In accordance with the invention, we directly carry out the reaction, causing the reforming, methanol synthesis and the synthesis of ammonia, so that the methanol and ammonia can be produced together without removal of carbon dioxide withdrawn from the synthesis gas. The production of hydrogen by steam reforming due to the endothermic reaction of CH4+H2O=CO+3H2, while the methanol synthesis in the absence of carbon dioxide due to reaction of CO+2H2=CH3HE. In the presence of carbon dioxide methanol is formed differently according to the reaction CO2+3H2=CH3HE+H2O. ideally, the raw synthesis gas for methanol production is a gas containing the highest possible molar ratio CO/CO2. The ammonia synthesis occurs according to the reaction N2+3H2=2NH3. Because if full-reforming process creates only 3 mol of hydrogen, while the methanol synthesis already takes 2 mol of hydrogen, and ammonia synthesis requires 3 mol of hydrogen, we were limited in order that the amount of ammonia that must be made is one third part, in order to fully utilize the hydrogen that comes on is icii according to the equation 1/3 (N 2+3H2=2NH3). Therefore, in some way, according to the invention we deliberately maintained a minimum of flexibility in the separation of the products of methanol and ammonia.

This simple and clear measure allows to produce about 75-80 wt.% methanol and 20-25 wt.% ammonia at any time in a way that is simpler and less costly than conventional methods. This method eliminates the need to use expensive stages of the shift reaction with steam to convert carbon monoxide into hydrogen and carbon dioxide. It also eliminates the need to use expensive stages of removal of CO2i.e. cleaning sour gas, such as conventional cleaning MDEA, and cleaning processes carbonates. Operating costs also remain at a low level, because there is no need to replace the catalyst for the shift reaction and there is no need to replenish the solvent tools in the processes of removal of CO2. This is in contrast with other United ways for the production of methanol and ammonia, such as in JP 2000063115 where very expensive to remove carbon dioxide using conventional purification from CO2or absorber is necessary to adjust the ratio of CO2/CO in the synthesis gas and still is a way to achieve flexibility in the process. In addition, since the secondary reforming is conducted in the secondary reformer with air blowing (the autothermal reformer with air-blown), in order to provide the required nitrogen there is no need for expensive and bulky plants air separation (ASU). This also makes the method less expensive than modern methods, which often require installation ASU to provide oxygen autothermal reformers and usually applies concomitant production of nitrogen for subsequent dilution with nitrogen.

The method of the present invention is friendly to the environment, because there are no emissions of CO2withdrawn from the synthesis gas for producing methanol and ammonia. Almost all of the carbon monoxide and carbon dioxide)formed in the process used for the synthesis of methanol. The method is suitable for enterprises of any capacity, including large enterprises producing more than 2000 tons per day of ammonia and methanol, for example, 3000, 5000 tons/day or even more.

Phase methanol synthesis, preferably, is carried out by conventional methods, by passing the synthesis gas at high pressures and temperatures, such as 60 to 150 bar, preferably 120 bar and 150-300C, at least one of the methanol reactor, sod is Rashi, at least one fixed bed of catalyst for methanol synthesis. Especially preferred methanol reactor is a reactor with a fixed bed of catalyst, cooled by a suitable cooling agent, such as boiling water, such as boiling water reactor (BWR). In a specific embodiment, the phase methanol synthesis at the stage (b) is accomplished by passing the synthesis gas through a single boiling water reactor and then through adiabatic reactor with a fixed catalyst bed. Or by passing the synthesis gas through a cascade of boiling water reactor and then through adiabatic reactor with a fixed catalyst bed. Preferably, the boiling water reactor is a single reactor condensation type for methanol, which contains within the usual casing fixed bed of granular catalyst for methanol synthesis and the cooling device adapted for indirect cooling of the synthesis gas for methanol production with a cooling agent. The reactor preferably operates at pressures above 90 bar and below 150 bar, more preferably above 110 bar and below 130 bar, as described in our Danish patent applications RA 200800261 and PA 200800260, registered on February 25, 2008, the Application of a methanol reactor in these applications gives who is very useful to work at pressures significantly higher than conventional boiling water reactors, which typically have a pressure of about 80 bar. In addition, it enables you to apply one reactor instead of two conventional boiling water reactor, thereby significantly reducing production rates. Moreover, since the working pressure for methanol synthesis can be maintained as high as about 120 bar or even higher, there is a significant savings in terms of equipment and total investment, as the synthesis of methanol is preferred at high pressures.

Accordingly, the invention provides the possibility of the section of the synthesis of methanol and ammonia at a similar operating pressures, for example 130 bar, which means the simplification process with significant savings in the size of the equipment, as mentioned above. There is also the opportunity to work at two different operating pressures, for example 80 bar at the stage of synthesis of methanol and 130 bar at the stage of synthesis of ammonia, which means saving energy for methanol synthesis.

At stage (b) an output stream containing methanol, preferably, is a liquid stream. This output stream is obtained by cooling and condensation of the synthesis gas from the methanol reactor. Therefore, the method of the invention may also contain cooling the synthesis gas discharged from each of the methanol of reaction is ora for condensation of methanol, and the transmission of gas through the separator, the abstraction of the bottom fraction from the separator containing the crude methanol, lead the top fraction containing synthesis gas, which is passed to the next methanol reactor, and the formation of a single outgoing liquid stream containing methanol, by combining the lower fractions of separators each reactor containing crude methanol.

It is clear that the term "methanol reactor"as used here, includes adiabatic reactor with a fixed bed of catalyst and cooled reactors such as boiling water reactors, and reactors methanol condensation type, which contain within the usual casing fixed bed of granular catalyst for methanol synthesis and the cooling device with a cooling agent, intended for the indirect cooling of the synthesis gas for methanol production.

Because the stage of synthesis of methanol is forward, there is no need to return a part of the top fraction from the separator adiabatic reactor with fixed bed back in the first methanol reactor methanol synthesis. This is the difference with other United ways of production of methanol and ammonia, such as the method described in JP 2000063115, where the methanol synthesis involves considerable recirculation of the technology the ski gas.

At the stage (s) stage catalytic ketanazii for the conversion of carbon oxides to methane is at least one reactor ketanazii, which, preferably, is an adiabatic reactor containing a fixed bed of catalyst ketanazii.

At stage (d) synthesis gas ammonia production from the stage of ketanazii containing the desired ratio of hydrogen and nitrogen (molar ratio of H2:N2equal to 3:1), if required, is passed through the compressor to obtain the desired pressure for the synthesis of ammonia, such as from 120 to 200 bar, preferably about 130 bar. The ammonia is then made in the usual way through a cycle of synthesis ammonia containing at least one ammonium Converter containing at least one fixed bed of catalyst for ammonia synthesis interlayer cooling. The exit stream containing ammonia, also contains hydrogen, nitrogen and inert gases, such as methane and argon. Ammonia can be removed from the thread that contains it, in the form of liquid ammonia by condensation and subsequent separation. Preferably, the outgoing gas stream containing hydrogen, nitrogen and methane, is output from the stage of synthesis of ammonia as well as a stream rich in hydrogen (>90% vol. H2). These threads may, for example, proceed from the unit, regenerative purge ha is. Preferably, this stream of hydrogen is added to the stage methanol synthesis (stage (b)), for example, by connection with the synthesis gas for methanol production. The cycle repeated use of this hydrogen-enriched stream gives a possibility to increase the efficiency of the process, since the useful hydrogen is used for the synthesis of methanol and then for the synthesis of ammonia, but not used as fuel.

In order to increase the energy efficiency of the process, the waste gas stream containing hydrogen, nitrogen and methane from step (d) is returned to the step (a), that is, it is returned as the exhaust gas fuel reforming section of the enterprise, in particular, for the initial stage of reforming.

On the accompanying drawing shows a simplified block diagram of the method according to a particular variant of carrying out the invention includes the reformer, the phase methanol synthesis, stage ketanazii and the stage of synthesis of ammonia.

Natural gas 1 is fed to the first stage 20 of the reforming (steam methane reformer) when you add a pair of 2. Partially reformirovannoy gas reformiruetsya then additional secondary stage 21 of the reformer (the autothermal reformer with air-blown) adding air 3. Synthesis gas 4 production of methanol containing hydrogen, oxides of carbon and nitrogen, is cooled in the HRSG(arts) education is m steam and then is compressed to a pressure for synthesis of methanol (not shown). At the stage 22 synthesis of methanol synthesis gas 4 production of methanol is converted in single pass operation (single pass, without any recirculation), forming a liquid stream 5 containing methanol, and the gas stream 6 containing nitrogen, hydrogen and unconverted carbon oxides. Approximately 80 wt.% the total capacity of the plant is the production of methanol in the stream 5. Oxides of carbon in the output gas stream 6 hydrogensource to methane at the stage 23 ketanazii, thus forming a synthesis gas 7 ammonia, having a molar ratio of H2:N2equal to 3:1. Synthesis gas 7 ammonia then passes through a stage 24 synthesis of ammonia stream 8 containing ammonia, and recirculation stream 9 containing hydrogen, methane and nitrogen, which is returned as the exhaust fuel gas to the first stage 20 of the reformer. Rich hydrogen stream 10 (>90% vol. H2also given from the stage 24 synthesis of ammonia. This thread is added to the stage 22 synthesis of methanol, combined with stream 4 for the synthesis of methanol. Approximately 20 wt.% the total capacity of the plant is used to produce ammonia in the stream 8. The plant does not require the use of air separation (ASU), as well as shift reaction with steam and stages of removal of CO2.

The following table shows the temperature, giving the mode and rate of flow of the various streams for the method, is depicted in Fig.1. By this method we can produce about 3,000 tons per day of methanol and 750 tons per day of ammonia, despite the use of complex feedstocks. Used the feedstock is a heavy natural gas (85% vol. methane):

TABLE
PositionThe pace.PressureFlow rate/KMOL/h
CBarH2OH2N2CH4COCO2Ar
494730.158901202314144193147104316
635120.32.745741457 463173820
735119.34371145751820
9351216747745016
103532146366614

1. The way co-production of methanol and ammonia from a source of hydrocarbons containing a consecutive stages:
a) obtaining synthesis gas methanol containing hydrogen, oxides of carbon and nitrogen by steam reforming of the original hydrocarbons in the initial stage of reforming and then on the secondary stage of reforming in the air blast;
(b) catalytic conversion of carbon oxides and hydrogen synthesis gas for methanol production at forward methanol synthesis and abstraction facing product containing methanol, and the exhaust gas stream containing nitrogen, hydrogen and unconverted carbon oxides;
(c) removing unconverted carbon oxide gas stream of step (b) by hydrogenation to methane at the stage catalytic ketanazii with the formation of synthesis gas of ammonia gas having a molar ratio of H2:N2equal to 3:1;
(d) catalytic conversion of nitrogen and hydrogen synthesis gas production of ammonia synthesis ammonia and abstraction facing product containing ammonia and the exhaust gas stream containing hydrogen, nitrogen and methane.

2. The method according to p. 1, in which the source of the hydrocarbon raw material is a natural gas or substitute natural gas (SNG).

3. The method according to p. 1, in which stage of the synthesis of methanol in step (b) is accomplished by passing the synthesis gas through a single boiling water reactor and then through adiabatic reactor with a fixed catalyst bed or by passing the synthesis gas through a cascade of boiling water reactor and then through adiabatic reactor with a fixed catalyst bed.

4. The method according to p. 3, in which the boiling veganoutreach.org represents the separate reactor condensation type for methanol, which contains within the usual casing fixed bed of granular catalyst for methanol synthesis and the cooling device adapted for indirect cooling of the synthesis gas for methanol production with a cooling agent.

5. The method according to p. 3, comprising cooling the synthesis gas discharged from each of the methanol reactor, for condensation of methanol and the transmission of gas through the separator, the abstraction of the bottom fraction from the separator containing the crude methanol, lead the top fraction containing synthesis gas, which is passed to the next methanol reactor, and the formation of a single outgoing liquid stream containing methanol, by combining the lower fractions of the separators of each reactor containing crude methanol.

6. The method according to any one of paragraphs.1-5, containing also the abstraction of hydrogen-enriched stream from the stage of synthesis of ammonia and add this stream to step (b).

7. The method according to any one of paragraphs.1-5, in which the exhaust gas stream in step (d)containing hydrogen, nitrogen and methane, is returned to the step (a).



 

Same patents:

FIELD: oil and gas industry.

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

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

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

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

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

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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.

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FIELD: chemistry.

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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 can be used in chemical industry and in power engineering. Synthesis-gas 50, containing at least CO and H2 and having first temperature at least 900C, is obtained at stage 12 by reaction of hydrocarbon raw material with oxygen. At the stage of air separation 16 in ionite membrane unit 16.1 flow of permeate 42, consisting mainly of oxygen, and flow of oxygen depleted air 44, which has second temperature, lower than first and equal to at least 600C, are obtained. Flow 44 is indirectly heated 24 to at least 900C by synthesis-gas 50 and partially expanded in turbine 28 to produce electric energy with obtaining partially expanded discharge flow of oxygen-depleted air 54. Cooled synthesis-gas 58 is supplied for additional cooling into waste heat boiler 26, and then to the stage of synthesis of hydrocarbons 30. In compressor 22 pressure of permeate flow 42 is increased and it is supplied to stage 12 of synthesis-gas obtaining. Flow of compressed air 38 is heated 20 to temperature not lower than 700C by transmission of heat from the stage of nuclear reaction.

EFFECT: invention provides utilisation of nuclear reaction heat and obtaining flows with high energy content with absence of harmful emissions.

11 cl, 4 dwg

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