Process for producing ammonia synthesis gas

Patent metadata

Field	Value
Publication number	US-10464818-B2
Application number	US-201715637547-A
Country	US
Kind code	B2
Filing date	Jun 29, 2017
Priority date	Aug 8, 2007
Publication date	Nov 5, 2019
Grant date	Nov 5, 2019

Abstract

A process for producing ammonia synthesis gas from the reforming of hydrocarbons with steam in a primary reformer ( 1 ) equipped with a plurality of externally heated catalytic tubes and then together with air in a secondary reformer ( 2 ) is characterized in that the reaction of said hydrocarbons with said steam in said primary reformer ( 1 ) is performed at an operating pressure of more than 35 bar in the catalytic tubes, in that air is added to said secondary reformer in excess over the nitrogen amount required for ammonia synthesis and in that the excess of nitrogen is removed downstream the secondary reformer preferably by cryogenic separation or by molecular sieves of the TAS or PSA type. This process allows to obtain high synthesis gas production capacities and lower investment and energy costs.

First claim

The invention claimed is:

1. A process for producing ammonia synthesis gas, comprising the steps of:
feeding a gas flow comprising hydrocarbons and a gas flow comprising steam to a primary reformer equipped with a plurality of externally heated catalytic tubes,
reacting said hydrocarbons with said steam in the catalytic tubes of said primary reformer at an operating pressure of more than 35 bar in the catalytic tubes, obtaining a product gas,
feeding said product gas and a flow of air to a secondary reformer in the absence of added hydrocarbons, said air being added in excess over the nitrogen amount required for ammonia synthesis for reforming all the hydrocarbons content of said product gas exiting the primary reformer,
subjecting said product gas to reaction with said air and then to secondary reforming, obtaining a reformed gas comprising nitrogen in excess over the amount required for ammonia synthesis, hydrogen, carbon oxides and unreacted steam, and
removing carbon oxides and excess nitrogen from said reformed gas to obtain said synthesis gas,
wherein the outlet temperature of said gas product from the tubes of the primary reformer does not exceed 750° C. so as to increase the lifetime of said tubes;
wherein said step of removing carbon oxides and excess nitrogen from said reformed gas comprises the following operative stages:
removing carbon monoxide from said reformed gas by catalytic conversion with unreacted steam into carbon dioxide and hydrogen,
removing carbon dioxide by scrubbing said reformed gas with a solution or solvent after said step of carbon monoxide removal, so obtaining a reformed gas still including carbon oxides, and
one of:
removing said carbon oxides from said reformed gas containing them by catalytic conversion to methane, obtaining a reformed gas deprived of carbon oxides, and removing excess nitrogen from said reformed gas deprived of carbon oxides by cryogenic separation; and
removing said carbon oxides and said excess nitrogen by passing said reformed gas still including carbon oxides through a PSA or TSA molecular sieve.

2. The process according to claim 1 , wherein said excess of air is comprised in the range of 15% to 100% over the air amount necessary to produce the nitrogen content required for ammonia synthesis.

3. The process according to claim 1 , wherein said operating pressure in the catalytic tubes of the primary reformer is in the range of 40-100 bar.

4. The process according to claim 3 , wherein said operating pressure in the catalytic tubes of the primary reformer is about 60 bar and wherein said outlet temperature is in the range of 650-750° C.

5. A process for producing ammonia from gas synthesis, comprising the steps of:
feeding a gas flow comprising hydrocarbons and a gas flow comprising steam to a primary reformer equipped with a plurality of externally heated catalytic tubes,
reacting said hydrocarbons with said steam in the catalytic tubes of said primary reformer at an operating pressure of more than 35 bar in the catalytic tubes, obtaining a product gas,
feeding said product gas and a flow of air to a secondary reformer in the absence of added hydrocarbons, said air being added in excess over the nitrogen amount required in the final synthesis gas for ammonia synthesis for reforming all the hydrocarbons content of said product gas exiting the primary reformer,
subjecting said product gas to reaction with said air and then to secondary reforming, obtaining a reformed gas comprising nitrogen in excess over the amount required for ammonia synthesis, hydrogen, carbon oxides and unreacted steam,
removing carbon oxides excess nitrogen from said second reformed gas to obtain said synthesis gas, and
feeding said synthesis gas to a ammonia synthesis loop and reacting it under conditions effective to obtain ammonia,
wherein the outlet temperature of said gas product from the tubes of the primary reformer does not exceed 750° C.

6. The process according to claim 5 , wherein said step of removing carbon oxides and excess nitrogen from said reformed gas comprises the following operative stages:
removing carbon monoxide from said reformed gas with unreacted steam by catalytic conversion into carbon dioxide and hydrogen,
removing carbon dioxide by scrubbing said reformed gas with a solution or solvent after said step of carbon monoxide removal, so obtaining a reformed gas still including carbon oxides,
removing said carbon oxides from said reformed gas containing them by catalytic conversion to methane, obtaining a reformed gas deprived of carbon oxides, and
removing excess nitrogen from said reformed gas deprived of carbon oxides by cryogenic separation.

7. The process according to claim 5 , wherein said step of removing carbon oxides and said excess nitrogen from said reformed gas comprises the following operative stages:
removing carbon monoxide from said reformed gas by catalytic conversion with some unreacted steam into carbon dioxide and hydrogen,
removing carbon dioxide by scrubbing said reformed gas with a solution or solvent after said step of carbon monoxide removal, so obtaining a reformed gas still including carbon oxides,
removing said carbon oxides and said excess nitrogen by passing said reformed gas still including carbon oxides through a PSA or TSA molecular sieve.

8. The process according to claim 2 , wherein said excess of air is comprised in the range of 20% to 40% over the air amount necessary to produce the nitrogen content required for ammonia synthesis.

9. The process according to claim 3 , wherein said operating pressure in the catalytic tubes of the primary reformer is in the range of 60-80 bar.

Assignees

• Casale Sa

Inventors

• Filippi Ermanno
• Badano Marco
• Skinner Geoffrey Frederick

Classifications

• C01B3/384

  with external heating of the catalyst · CPC title

• C01B2203/043

  Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration · CPC title

• C01B3/56

  by contacting with solids; Regeneration of used solids · CPC title

• C01B2203/0415

  Purification by absorption in liquids · CPC title

• C01B3/48 Primary

  followed by reaction of water vapour with carbon monoxide · CPC title