Method for production of synthesis gas for ammonia production

 

The invention relates to methods of producing synthesis gas for ammonia production. Method for production of synthesis gas for ammonia production involves feeding a source gas, at least one pair of reactors for the implementation of the reforming unit, with each reactor has towards the implementation of the method, fuel and toward the implementation of combustion, and each pair of reactors connected in parallel on the side of the method and fuel supply and consistently-side implementation of combustion, and control the temperature of the flame in each pair of reactors by feeding excess air for combustion in the first reactor of specified pairs of reactors and oxygen-depleted flue gas from the first reactor to the combustion in the second reactor of the specified pair of reactors. The invention reduces the costs of obtaining synthesis gas. 10 C.p. f-crystals, 2 Il.

The invention relates to a process of steam reforming, particularly to a method for producing synthesis gas for ammonia production.

The known method for production of synthesis gas for ammonia production, including the supply of the source gas, at least one pair of reactors for the implementation of the reformer, with cardsonline is the optimization of operating parameters, lowering costs for obtaining synthesis gas.

The problem is solved in a method of producing synthesis gas for ammonia production, including the supply of the source gas in at least one pair of reactors for the implementation of the reformer due to the fact that each reactor has towards the implementation of the method, fuel and toward the implementation of combustion, and each pair of reactors connected in parallel on the side of the method and fuel supply and consistently-side implementation of combustion, and control the temperature of the flame in each pair of reactors by feeding excess air for combustion in the first reactor of specified pairs of reactors and oxygen-depleted flue gas from the first reactor to the combustion in the second reactor of the specified pair of reactors.

The source gas, preferably in desulfuromonas form, can be mixed with the flue gas withdrawn from the second reactor each pair of reactors, and the resulting gas mixture can be fed in at least two pairs of reactors, and each pair of reactors connected to another pair of reactors in series on the side implementation burning. The quantity of flue gas is mixed with ex is from the second reactor can be extended to obtain, at least part of the energy required to compress the air.

The flame temperature in each pair of reactors support below approximately 1400oC.

The combustion air is preferably fed to the first reactor in excess of about 105%. The total excess air in the second reactor supported by about 5%.

The combustion air supplied to the first reactor, is compressed to a pressure slightly higher than the pressure of the initial gas in place at the entrance to the reactor.

The main advantages of the method according to the invention over the known method as follows: stoichiometric synthesis gas for production of ammonia are in heat-exchange installation for the implementation of the reforming without the use of enriched air or cryogenic separation of excess nitrogen; the use of two reactors for the implementation of the reforming consistently on the side implementation combustion provides control over the flame temperature without excess total excess air for combustion, the allocation of nitrogen oxide (NOxfrom the process of reforming in the atmosphere is reduced to a minimum; the allocation of sulfur dioxide is prevented; carbon dioxide and steam produced during combustion, partially used as raw material in the bottom compensate the excessive expansion of the combustion gases.

In addition, steam reforming of the source gas mixed with nitrogen-containing, and carbon dioxide in flue gas produced at a later stage heat exchange steam reformer, provides a higher conversion of hydrocarbons in a steam reformer and, thus, a lower concentration of unreacted hydrocarbons, upon exiting the reactor gas.

In the reactor for the implementation of the steam reforming heat necessary for carrying out endothermic reactions of steam reforming, produced by indirect heat exchange with compressed flue gas.

To receive flue gas for use in the process of heat exchange steam reformer, the fuel burn of the first stage heat exchanger steam reforming with the above excess air, which provides a lower combustion temperature in the reactor. Oxygen-containing flue gas is then withdrawn from the first stage of reforming, cooled and then used for burning additional fuel in one or more subsequent stages of reforming.

The invention is described below with reference to the drawing.

Thus in Fig.1 presents a diagram of the method according the image is, is which usually use natural gas, disulfiram and divided into two streams. The source gas is mixed with steam 30 and pre-calculated number purified from oxygen and compressed gas furnace 40 (see below) to obtain the ratio of hydrogen to nitrogen required to obtain synthesis gas. The gas mixture is used as process gas in two heat exchange reactor 60, 80 for the implementation of the reforming along the side of the method and fuel supply and consistently on the side of the air supply for combustion. The temperature at the outlet of each layer 62, 82 of the catalyst located in the reactor for the implementation of reforming, high enough to ensure a sufficiently low loss of methane.

The 100 air is compressed up to the pressure that is slightly above the pressure of process gas station at the entrance to the heat exchangers. This air is first used as the combustion air in the first heat exchanger burner 64, which operates at high excess air (about 105% excess) in order to maintain the flame temperature below 1400oC.

After completion of the heat exchange tube for the implementation of the reformer in the first reactor compressed furnace. is the flue gas depleted in oxygen, which reduces the flame temperature below about 1400oS, while the total excess air support low, around 5%.

The combustion gas 104, leaving the second reactor is divided into two streams 106, 108. Stream 106 extend to receive a portion of the energy required to compress the air. The remainder of the combustion gas 108 serves to deoxygenator to remove remaining traces of oxygen and forth in the stream fed to the reactor source gas as described above.

According Fig.2 containing methane process gas is subjected to steam reforming in the four heat exchange reactors I, II, III and IV for the implementation of steam reforming.

Apparatus for the implementation of the reforming - conventional shell & tube type, i.e. devices in which the inner tube is coaxially arranged in the outer pipe shell (casing). The steam reforming catalyst is loaded into the annular space between the walls of the inner and outer pipes.

The necessary heat for the endothermic steam reforming reaction occurring in the process gas supply passing hot flue gas from the outside along the walls of the outer tube.

Before the introduction of those. the flask gas 4 is removed from the reactor II after the implementation of the heat transfer in the steam reforming reaction occurring in the reactor. Flue gas 4 is mixed with the process gas in such quantity to create the desired ratio of hydrogen to nitrogen for the synthesis gas produced by steam reforming in a reactor I-IV.

Reactors I-IV are connected in parallel to the input of the processed gas mixture 6. On the side implementation combustion and feed flue gas reactors arranged in groups I, II and III, IV, and both groups of reactors connected in series.

Reactors I and II are heated by burning fuel with compressed air 8. Burning in the reactor I is carried out with excess air to achieve acceptable combustion temperatures and provide the necessary oxygen content in the flue gas 10, which is removed from the reactor I and injected into the reactor II for further combustion. Flue gas 12, which is removed from the reactor II, served in deoxygenator 14 having a layer of conventional oxidation catalyst to remove residual oxygen from the gas. From deoxygenator 14 flue gas 4 containing mainly nitrogen, carbon dioxide and water is fed to the mixing with the source gas 2.

willow at atmospheric pressure. Flue gas 16 leaving the reactor III, served on combustion in reactor IV. After heat transfer to the reactor IV fuel gas is fed to the conventional heat recovery from exhaust gases.

Claims

1. Method for production of synthesis gas for ammonia production, including the supply of the source gas, at least one pair of reactors for the implementation of the reformer, wherein each reactor has towards the implementation of the method, fuel and toward the implementation of combustion, and each pair of reactors connected in parallel on the side of the method and fuel supply and consistently-side implementation of combustion, and control the temperature of the flame in each pair of reactors by feeding excess air for combustion in the first reactor of specified pairs of reactors and oxygen-depleted flue gas from the first reactor to the combustion in the second reactor of the specified pair of reactors.

2. The method according to p. 1, characterized in that the source gas is mixed with the flue gas to obtain a gas mixture.

3. The method according to p. 1, characterized in that the temperature of the flame support below approximately 1400oC.

4. The method according to p. 1, characterized in that the air supplied to the reactor supported by about 5%.

6. The method according to p. 1, characterized in that the combustion air supplied to the first reactor, is compressed to a pressure slightly higher than the pressure of the initial gas in place at the entrance to the reactor.

7. The method according to p. 1, characterized in that the flue gas from the second reactor is expanded to receive at least part of the energy required to compress the air.

8. The method according to p. 2, characterized in that the flue gas is mixed with the source gas, is removed from the second reactor each pair of reactors.

9. The method according to p. 2, characterized in that the gas mixture is fed to at least two pairs of reactors, and each pair of reactors connected to another pair of reactors in series on the side implementation burning.

10. The method according to p. 2, characterized in that the quantity of flue gas is mixed with the source gas is chosen so as to achieve a specified ratio of hydrogen to nitrogen in the synthesis gas.

11. The method according to p. 1, characterized in that the source gas disulfiram.

 

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