BG112796A - Syngas production for producing hydrogen through steam reforming of hydrocarbons applying a full combustion process of fuel gas stream in autothermal reforming - Google Patents

Abstract

The invention relates to the processes of steam reforming of hydrocarbons and of partial and complete oxidation of hydrocarbons. The syngas is a major source for the production of many hydrogen-based products. The syngas is a gas mixture obtained from hydrocarbons, which contains hydrogen and carbon monoxide, as well as carbon dioxide and residues of unreformed hydrocarbons. One of the technologies for obtaining syngas is Autothermal Reforming ATR of light hydrocarbons. An ATR variant is used as a secondary reforming in the two-step steam reforming. The processes of the conventional ATR take place in an ATR reactor consisting of two zones. One of them is for the partial combustion and mixing process, which provides heat for the endothermic steam reforming process in the next, second catalyst zone. The invention replaces the process of partial combustion of the feed process gas in the conventional ATR with a process of complete combustion of a fuel gas stream. In order to ensure the full combustion ATR process shown in Figure 4, a stream of fuel gas (11) is fed into the combustion and mixing zone of the ATR reactor (16), separated from the sulfur compounds purified gas in the sulfur treatment unit (4) mixed with a stream of steam (12). A stream of oxidant (8) mixed with a stream of water vapour (13) is also fed into the combustion zone. The products of complete combustion give off their heat by mixing with a flow (5) supplying process gas and steam. The gas mixture enters the catalyst zone (16 B) of the ATR full combustion reactor (16), where a process of steam reforming of the hydrocarbons supplied by a stream (5) feeding process gas and steam takes place. The process of complete combustion of hydrocarbons emits more heat than the process of partial combustion and accordingly provides heat for steam reforming of more hydrocarbon feedstock. Higher hydrogen production per unit of raw material and higher energy efficiency are ensured. When the process of complete combustion of a fuel gas stream is used in secondary reforming, the relative hydrogen production also increases, because there are no losses from combustion of products coming from the primary reforming. It also reduces the consumption of fuel gas for the burners of the primary reforming, because the heat exchange is direct by mixing and there are no heat losses from the flue gases whatsoever.

Description

'· ··· ··· ♦ · ·· · Preparation of Syngas for hydrogen production, by steam ^ f & (L ^ || D of the process of full combustion of a stream of fuel gases in Autothermal Reforming

Description

Name

Obtaining Syngas for hydrogen production by pomegranate reforming of hydrocarbons by applying a process of complete combustion of a stream of fuel gases in Autothermal Reforming

Field of technology

The invention relates to the production of syngas by steam reforming of hydrocarbons.

BACKGROUND OF THE INVENTION

Existing level of hydrogen production technologies.

There are different technologies for hydrogen production. The most economically efficient and, accordingly, the most widespread are the technologies that produce syngas from hydrocarbons. These are:

• Partial oxidation • Steam reforming • Autothermal reforming of ATP

Syngas is a gas mixture containing mainly hydrogen and carbon monoxide, as well as carbon dioxide and unconverted starting hydrocarbons.

In the next stage of hydrogen production - "Carbon monoxide conversion", carbon monoxide registers with water vapor to carbon dioxide, which produces more hydrogen.

Depending on the final product of production - hydrogen; ammonia; methanol; synthetic fuel; another chemical product, different ratios of hydrogen and carbon monoxide are required in the resulting syngas.

For the production of hydrogen and ammonia, the yield of hydrogen per unit of raw material must be the highest.

Review of syngas production technologies.

Partial Oxidation POX

This is a technology in which hydrocarbons are subjected to partial oxidation with oxygen.

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Obtaining Syngas for hydrogen production by means of full combustion of a stream of fuel gases in Autothermal Reforming

Oxygen can be supplied by supplying air, oxygen-enriched air, or pure oxygen.

Because all the necessary amount of raw material is supplied for combustion, oxygen is in short supply, complete oxidation (combustion) of the hydrocarbons to carbon dioxide and water does not take place. The oxidation is partial POX to carbon monoxide and hydrogen, or to carbon monoxide and water, by the following reactions (hereinafter the exemplary reactions are with methane as feedstock).

1. CH4 + 1.502 <=> CO + 2H ₂ O

2. CIS + 0.5O ₂ <=> CO + 2H ₂

ΔΗ ₂ 98 k = -519 kJ / mol

ΔΗ ₂ 98 k = -36 kJ / mol

The reactions are exothermic - they give off heat and the process does not need to supply heat from an external source.

In the next step - "Conversion of carbon monoxide", the reaction of carbon monoxide with water vapor on a catalyst produces additional hydrogen.

The ROX (partial oxidation) technology has the lowest relative hydrogen yield of these three, but is practically the only one efficient enough to produce syngas from coal, coke and heavy oil refining residues. Because it does not use a catalyst, the ROX technology is less sensitive to sulfur in the feedstocks, as well as to the formation of soot and carbon.

Steam reforming of hydrocarbons.

In steam reforming, oxidation of natural gas or light hydrocarbons with steam is performed. The process takes place in tubes filled with catalyst mainly by endothermic reaction (3).

3. CH4 + H ₂ 0 <=> CO + _{CH 2}

ΔΗ ₂ 98 k ^- +206 kJ / mol

The process has the highest relative hydrogen yield and is endothermic in need of heat, which is supplied by burners outside the pipes.

The catalyst reduces its activity in the presence of sulfur in the feed gas (natural gas or light hydrocarbons), as well as in the deposition of soot and / or carbon.

To avoid poisoning the catalysts with sulfur, the feed process gas is subjected to desulphurization at 350 - 400 ° C.

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Obtaining Syngas for the production of hydrogen by means of hydrocarbons with a process of complete combustion of a stream of fuel gases in Autothermal Reforming

To avoid the formation of soot and / or carbon, the process is carried out with an excess of water vapor, the typical molar ratio of vapor to carbon is maintained around 3.

When hydrocarbons with more carbon atoms are subjected to steam reforming, the feed process gas may be subjected to pre-reforming at temperatures of 400-550 ° C, where hydrocarbons heavier than methane are converted to methane, hydrogen, carbon monoxide and carbon dioxide.

As an apparatus, steam reforming is a complex technical facility with high investment costs. Carrying out the process in a large number of pipes, large differences in temperature and pressure inside and outside the pipes, the proximity of the flame from the burners to the walls of the pipes, impose high requirements on pipe materials, as well as limitations in process temperature and pressure. Typical values are: outlet temperature around 800 - 850 ° C, pressure up to 30 - 35 bar.

To reduce the size and capital costs of steam reforming, to reduce the fuel consumption in the furnace burners, as well as to dose the required amount of nitrogen in the production of ammonia, a two-stage reforming is used. First degree - primary, pipe, steam reforming, and second degree - secondary, steam oxygen (air) reforming.

The secondary reform consists of two zones. One in which the oxidant and the syngas from the primary reforming containing hydrogen, carbon monoxide, carbon dioxide and residual unreformed methane enter. In this area, some of the flammable components of the syngas (hydrogen, carbon monoxide, methane) are burned with oxygen by the oxidant.

Depending on the desired goals - degree of reduction of the primary reform; hydrogen extraction; dosing a stoichiometric amount of nitrogen for ammonia synthesis; a certain ratio of hydrogen to carbon monoxide, the oxidant may be oxygen-enriched air, or oxygen.

In addition to combustion, this zone must ensure good mixing and homogenization of the gas mixture in order to avoid the formation of soot and carbon and their deposition on the catalyst.

The syngas mixture and the combustion products then enter a catalyst bed zone where the endothermic steam reforming process (reaction 3) takes place and the temperature of the gas mixture drops rapidly. Typical temperatures at the exit of the secondary reforming are about 900 1000 ° C.

Secondary reforming reduces capital and operating costs (fuel for primary reforming burners), but reduces the relative ammonia yield per unit of hydrocarbon feedstock,

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Obtaining Syngas for the production of hydrogen by means of hydrocarbons in the process of complete combustion of a stream of fuel gases in Autothermal Reforming due to the combustion of part of the products or from the residual methane coming from the primary reforming.

Autothermal ATP reforming

In autothermal reforming, the processes take place in a two-zone reactor. One for partial combustion (POX) of the starting hydrocarbons in reactions 1 and 2, and another zone with a catalyst where a steam reforming process under reaction 3 takes place.

The feedstock first passes through a desulphurisation unit at 350 - 400 ° C, if the feedstock contains hydrocarbons heavier than methane, it may also be subjected to a pre-reforming process at temperatures of 400 - 550 ° C.

As the amount of hydrocarbons is greater than the stoichiometric one for complete combustion, the combustion in the combustion and mixing zone is incomplete POX (Partial Oxidation). To provide enough heat for the next catalytic, endothermic steam reforming process, oxygen-enriched air or a larger amount of air is usually used as the oxidizer (the latter requires subsequent removal of excess nitrogen).

ATP technology allows the construction and installation of cost-effective reactors with high capacity for syngas. By installing more than one ATP reactors connected to one or more combustion chambers, syngas installations with practically unlimited capacity can be built.

Despite the lower capital costs, autothermal reforming is not as widely used as two-stage steam reforming, due to the relatively lower energy efficiency and lower hydrogen yield per unit of feedstock.

In essence, the secondary reforming discussed above is autothermal reforming, but it burns components contained in the syngas coming from the primary reforming.

Different variants of steam and autothermal reforming are used, as well as combinations of them, for example heat exchange reforming (syngas leaving the secondary, autothermal reforming heats the pipes of the primary reforming located in a heat exchanger).

Raw materials also vary - methane, light hydrocarbons, waste and associated gases from refineries, oxygen-containing compounds such as alcohols and ethers, for example for Fuel Cell technology.

There are also different variants of oxidants - air enriched with oxygen, pure oxygen.

At present, the most widely used method for producing syngas is the two-stage steam reforming of methane.

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Obtaining Syngas for hydrogen production, by steam hydrocarbons with hydrocarbons is in the process of complete combustion of a stream of fuel gases in Autothermal Reforming

Technical essence of the invention

The invention replaces the process of partial ROX oxidation (combustion) in the autothermal reforming and the process of combustion of crude syngas products in the secondary reforming, with a process of complete oxidation (combustion) of a fuel gas stream.

Oxidizer and fuel flow are fed into the combustion zone in an amount allowing maximum approach to the reaction (4.) of complete combustion (oxidation). The following reaction takes place

4. CH Ar + 2O ₂ <=> CO ₂ + 2H ₂ O ΔΗ ₂ 98 = -891 kJ / mol

Depending on the desired end effect - high hydrogen yield, energy efficiency, production of a particular product, an oxidizer with different oxygen content can be used - atmospheric air; oxygen-enriched air; nitrogen-enriched air; pure oxygen.

Complete combustion (reaction 4) gives off more heat per unit of fuel as well as per unit of oxygen, compared to reactions (1,2) of partial combustion of POX, as well as from combustion in the secondary reforming of hydrogen to water and carbon monoxide to carbon dioxide. With the complete combustion of the fuel gas stream, heat is provided for the reforming of more feed process gas and the extraction of more hydrogen per unit feedstock by the steam reforming reaction (reaction 3), and a corresponding reduction in feed process gas consumption per unit final product.

The combustion is inside the reactor and after mixing with the feed process gas, the combustion products fall on the catalyst. Therefore, the flow of fuel gas entering the combustion in the autothermal reforming must also be free of sulfur-containing components.

When the full-combustion autothermal reforming process is used as a secondary reforming, a fuel stream consisting of hydrocarbons not reformed in the primary reforming is also used. Thus, the entire feed process gas stream participates in both stages of steam reforming and the total hydrogen yield is the maximum per unit feed process gas, the same as for the primary tubular steam reforming. This is because they do not burn and there is no loss of some of the products of the primary reform - as in the conventional secondary reform of the syngas coming from the primary reform. As a result, the consumption of feed process gas per unit of product is reduced.

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Obtaining Syngas for production of hydrogen, by steam * dv4> orch.ig of hydrocarbons with yariaagvle of the process of complete combustion of a stream of fuel gases in Autothermal Reforming

On the other hand, the fuel gas after complete combustion is mixed in the same apparatus with the process feed gas, giving off its heat completely and directly without heat loss through the walls of the pipes in the primary reforming and from the heat from the flue gases.

This reduces the fuel gas flow rate for reforming the same amount of feed process gas compared to conventional two-stage reforming.

The invention reduces the cost per unit of production of both the feed process gas stream and the combustion gas in the two-stage steam reforming.

As gas consumption decreases, carbon dioxide emissions into the atmosphere are reduced to the same extent.

Carbon dioxide emissions from flue gases, which are at atmospheric pressure and are technically difficult, and energetically and economically unprofitable to capture, are reduced relatively more.

The carbon dioxide in the syngas is also absolutely reduced and is less per unit of product compared to conventional autothermal and two-stage steam reform schemes. Relative to total carbon dioxide emissions (the sum of ATP process emissions and combustion in the primary reforming furnace) in the new full combustion scheme, the carbon dioxide emissions from the process (from syngas) are a percentage higher than the carbon dioxide emissions from flue gas of the primary reforming.

As the process takes place at a pressure of about 30 bar, this allows more carbon dioxide to be captured per unit of product, with known and widely used technologies for purification of syngas from carbon dioxide, and then this carbon dioxide to be used in the production of other products. (eg urea), or to be deposited.

Explanation of the figures

Four figures are presented.

Figure 1 shows a block diagram of a conventional two-stage steam reforming.

Figure 2 shows a block diagram of conventional autothermal reforming

Page 6 of 14 ···· ·· · w - Obtaining Syngas for production of hydrogen by steam | »vforl» 1 «hg of hydrogen in the process of complete combustion of a stream of fuel gases in Autothermal Reforming

Figure 3 shows a block diagram of a two-stage steam reforming with a secondary reforming with complete combustion of a fuel gas stream - object of the invention.

Figure 4 shows a block diagram of autothermal reforming with complete combustion of a fuel gas stream - object of the invention.

Designation of the elements in the figures

1. Total gas flow - raw material

2. Process feed gas stream for desulphurization

3. Fuel gas flow for primary steam reformers

4. Sulfur treatment unit

5. A mixture of feed process gas and steam

6. Primary steam reform

7. Crude syngas to secondary reform

8. Oxidizer

9. Conventional secondary reform

C. Secondary reforming catalyst zone

10. Syngas

11. Fuel gas for complete internal combustion in autothermal or secondary reforming - object of the invention

12. Steam for mixing with the feed process gas. Steam for mixing with the oxidizer

14. Conventional autothermal reforming

C. Zone with a catalyst for autothermal reforming

5. Secondary reforming with full combustion - object of the invention

C. Area with catalyst of the secondary reforming with full combustion. Autothermal reforming with full combustion - object of the invention

C. Full combustion autothermal reforming catalyst zone

Notes:

1. In all block diagrams, optionally after “4. A desulphurisation unit may be pre-reformed.

2. In the block diagrams shown in FIG. 2 and FIG. 4, not used “3. Fuel gas flow for primary steam reformers. In these figures, the flow “1. Total gas flow - raw material ", coincides with flow 2. Process feed gas stream for desulphurization.

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Obtaining Syngas for hydrogen production by steam reforming of hydrocarbons with gf ^ Lag ^ - ^ in the process of complete combustion of a stream of fuel gases in Autothermal Reforming

Examples of the invention. Detailed description.

1. Autothermal reforming with full combustion

We consider the scheme of the process Autothermal Reforming with full combustion shown in Figure 4.

The full-combustion autothermal reforming reactor is a pressure vessel that is lined with refractory materials on the inside and has a water jacket on the outside of the strength hull.

Natural gas, which contains mainly methane, is the most used raw material for the production of syngas.

The natural gas (1), heated to 350 - 400 ° C enters the block (4) for purification from sulfur compounds.

The gas purified of sulfur-containing components is mixed with a stream (12) of superheated steam.

The vapor-gas mixture is then divided into two streams - a stream (5) of feed process gas, which enters the ATP (16) for mixing with the products of complete combustion and a stream (11) of fuel gas for complete combustion, which enters the combustion zone. ATP (16). A variant of flow separation (11) is possible immediately after (4) the desulphurisation unit and before mixing with steam (12).

The oxidant (8) mixed with a certain amount of superheated steam (13) is also fed into the combustion zone of the ATP (16), and the process of complete combustion by reaction 4 takes place. A variant without supply of steam (13) in the stream is possible. oxidant (8).

The products of complete combustion are mixed with the feed process gas (5) and the gas mixture enters the catalyst zone (16 V). There is a process of steam reforming of methane by reaction 3.

Depending on the final product, the resulting syngas (10) after cooling is fed either to a unit for the conversion of carbon monoxide by steam to carbon dioxide and hydrogen, or to a production in which carbon monoxide is a raw material, for example methanol, or products according to the Fischer-Tropsch synthesis.

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Obtaining Syngas for hydrogen production by steam reforming of hydrocarbons with a process of complete combustion of a stream of fuel gases in Autothermal Reforming

2. Two-stage steam reforming with secondary reforming with full combustion. FIG. 3

The natural gas (1) is divided into two streams - a stream (3) of fuel gas for the burners of the primary reforming and a stream (2) of feed process gas, which after heating to 350 - 400 ° C enters the block (4) for desulfurization. compounds.

The gas purified of sulfur-containing components is mixed with a stream (12) of superheated steam.

The vapor-gas mixture is then divided into two streams.

A process gas supply stream (5) enters the tubes of the primary steam reforming (6), where reaction 3 of the steam reforming takes place. In order to reduce the amount of fuel gas (3), this scheme can maintain a low heat load, respectively a low reaction temperature in the pipes - below 750 ° C and the crude syngas (7) to contain more residual methane to be reformed. in the more energy-intensive secondary reform (15).

A stream (11) of fuel gas for complete internal combustion enters the combustion zone of the secondary (ATP) steam reform (15). A variant of flow separation (11) is possible immediately after (4) the desulphurisation unit and before mixing with steam (12).

The oxidant stream (8) mixed with a certain amount of superheated steam (13) is also fed into the combustion zone of the secondary reforming (15), and the process of complete combustion by reaction 4 takes place. A variant without supply of steam (13) in oxidant flow (8).

The products of complete combustion are mixed with the feed process gas (5) and the gas mixture enters the catalyst zone (15 V). There is a process of steam reforming of methane by reaction 3.

The resulting syngas (10), after cooling, is fed either to a unit for the conversion of carbon monoxide by steam to carbon dioxide and hydrogen, or to a production in which carbon monoxide is a raw material, for example methanol, or Fischer-Tropsch synthesis products. .

Use of the invention

The invention can be applied in all productions which are based on syngas.

The invention is easily feasible. A constructive design change is only required for the combustion and mixing area.

The conventional autothermal / secondary reforming reactors currently in use are designed to ensure the partial combustion of the gases entering the reactor and the mixing and homogenization of all containing

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Obtaining Syngas for the production of hydrogen by steam reforming of water pipes with the process of complete combustion of a stream of fuel gases in Autothermal Reforming substances in them, in large gas volumes and at high pressure and temperature.

The process of full combustion in ATP takes place at a temperature and pressure close to those of the process of partial combustion, and does not set fundamentally new technical requirements for the design, production, commissioning, process control and operation of reactors for autothermal and secondary reforming with full combustion.

All knowledge and experience gained with conventional processes and reactors for autothermal and secondary reforming can be applied to the new full combustion process and to the apparatus for its application.

For modern process control systems, it is not a problem to manage with a high degree of accuracy, reliability and safety, any ratio between fuel gas and oxidizer, the other necessary parameters of the flows entering the reactor, as well as the monitoring of the processes in the reactor. the reactor itself.

The invention can be applied both in newly constructed installations and for the reconstruction of existing ones.

The supply of fuel gas for complete oxidation in a stoichiometric ratio to the supplied oxidant maximizes the yield of hydrogen per unit of hydrocarbon feedstock. This is the case that brings the highest efficiency for the production of hydrogen and ammonia.

The supply of fuel gas in a different off-stoichiometric ratio for complete oxidation to oxygen in the supplied oxidizer ("partial" conduct of partial combustion), combined with methods for "adjusting the composition" of the syngas in the next stages of production, allows to obtain syngas with optimal ratio of hydrogen relative to carbon monoxide, for the production of the required end product with improved efficiency.

The composition of the syngas, and in particular the nitrogen content in it, can be varied by the use of an oxidant with a different ratio of nitrogen to oxygen in it (this ratio in air is 3.71). The oxidant can be: pure oxygen; oxygen-enriched air; ordinary air; nitrogen-enriched air.

The higher efficiency of raw material (fuel) use and technically simplified scheme favor the use of autothermal reforming with full combustion, for obtaining hydrogen for use in fuel cell technology (Fuel Cell), as well as for obtaining hydrogen for use in local small, fuel, non-fuel and production installations.

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Preparation of Syngas for hydrogen production, by steam of hydrogen in the production of a process of complete combustion of a stream of fuel gases in Autothermal Reforming

Advantages of the invention

Compared to conventional schemes for the production of syngas from hydrocarbons, the invention:

- Increases the yield of hydrogen per unit of raw material, respectively reduces the consumption of raw material per unit of product.

- Reduces capital costs

- Reduces operating costs

- Significantly reduces primary steam reforming, or for many applications eliminates the need for two-stage reforming, leaving only one stage - autothermal reforming with complete combustion of the fuel gas.

- Schemes without primary steam reforming (without reaction tubes), can work with higher process pressure over 40 bar; a lower steam to carbon ratio in the feed process gas around and below 2; with increased capacity (productivity) for syngas production.

Schemes without primary reform are no longer a bottleneck to increase plant capacity.

- Reduces atmospheric carbon dioxide emissions per unit of product.

- Allows capture and utilization of carbon dioxide to a greater extent, due to the increased share of carbon dioxide in the syngas (at high pressure), at the expense of the share of atmospheric pressure from burners in the furnace of the primary reforming.

- Increases the feasibility of steam reforming for the production of hydrogen for Fuel Cell installations and engines.

- Increases hydrogen production capacity for local, specific "boutique" applications.

- Reconstruction of existing installations with replacement of conventional reactors, or with small changes in their structures and with small investments, achieves significant energy, economic and environmental effects.

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Obtaining Syngas for hydrogen production by steam reforming of hydrocarbons by applying a process of complete combustion of a stream of fuel gases in autothermal reforming.

Applications

Sources used:

1. Azotchik's Handbook 2nd edition, revised Moscow "Chemistry" 1986

2. US5595719A Process for steam reforming of hydrocarbons

3. US6936082B2 Very large autothermal reformer

4. US7550215B2 Autothermal reformer-reforming exchanger arrangement for hydrogen production

5. EP 0 440 258 Bl Heat exchange reforming process and reactor system.

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Obtaining Syngas for hydrogen production by steam reforming of hydrocarbons with application of a process of full combustion of a stream of fuel gases in Autothermal Reforming

Claims (9)

Claims A process of full-combustion autothermal reforming to produce hydrocarbon syngas, characterized in that in the combustion zone of a full-combustion autothermal reforming reactor, by complete combustion of a stream of fuel gas with oxygen from a stream of oxidant and by mixing of the products of complete combustion with a stream of feed process gas mixed with steam, heat is provided for the endothermic catalytic process of steam reforming of hydrocarbons in the feed process gas, which process takes place in the catalyst zone of the complete combustion autothermal reformer. Application of the complete combustion process described in claim 1, in the process of secondary steam reforming with complete combustion to obtain syngas, characterized in that in the combustion zone of a reactor for secondary reforming with complete combustion, by complete combustion of fuel gas stream with oxygen from oxidant stream and after mixing the products of complete combustion with a stream of crude syngas coming from the primary steam reforming, heat is provided for the endothermic catalytic process of steam reforming of residual methane in the crude syngas, which process takes place in the catalyst zone of complete combustion secondary reforming reactors. Application of the processes described in claim 1 and claim 2 for the production of syngas from natural gas, light hydrocarbons, associated and waste gases in refineries, alcohol ethers Application of the processes described in claim 1 and claim 2, after reconstruction of existing conventional syngas plants, by replacing existing conventional reactors with new full combustion reactors, or by upgrading existing reactors. 5. Supply in the combustion zones and mixing of the reactors for autothermal reforming with full combustion and of the secondary reforming with full combustion, of fuel gas in different ratios to the oxygen in the oxidant and / or of oxidizer with different oxygen content, in order to reactions of both full and partial combustion, and obtaining with improved efficiency of syngas with the ratio required for the production of the final product between the components contained in syngas Page 12 of 14 Obtaining Syngas for hydrogen production by steam reforming of hydrocarbons with application of a process of full combustion of a stream of fuel gases in Autothermal Reforming Application of the processes described in claim 1 and claim 2 for the construction of high-capacity autothermal reforming plants, characterized in that they consist of more than one ATP reactor connected to one or more complete combustion combustion chambers . Application of the processes described in claim 1 and claim 2 for the production of hydrogen for use in stationary and mobile Fuel Cell installations. Application of the processes described in claim 1 and claim 2 for the production of hydrogen in combustion plants for use as a fuel or as an additive in the fuel for combustion in furnaces, boilers, preheaters, for combustion in internal combustion engines, for gas turbines, or in other installations using fuels, in cases where the use of ordinary (fossil) fuels is undesirable or limited. Application of the processes described in claim 1 and claim 2 for the production of hydrogen for use in local stationary and mobile installations for non-combustible applications.