Ammonia synthesis

• US 4,792,441 A
• Filed: 01/19/1988
• Issued: 12/20/1988
• Est. Priority Date: 01/19/1988
• Status: Expired due to Fees

• Current Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Original Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Inventors: Allam, Rodney J., Wang, Shoou-I, Sircar, Shivaji, Patel, Nitin M.
• Primary Examiner(s): Doll, John
• Assistant Examiner(s): Langel, Wayne A.
• Application Number:
  US07/145,782
• Time in Patent Office: 336 Days
• Field of Search: 252/373, 252/376, 423/359, 423/360, 423/361
• US Class Current: 423/359
• CPC Class Codes: C01B 3/025 Preparation or purification of gas mixtures for ammonia synthesis

Abstract

An ammonia synthesis gas mixture comprised of substantially pure hydrogen and nitrogen in approximately 3/1 molar ratio is obtained form two stage reforming of a methane-rich hydrocarbon charge such as natural gas. About 40% of the fresh natural gas is charged to primary steam reforming and the obtained primary reformate product, containing about 17 volume percent of unreacted methane, is mixed with the other 60% of the fresh natural gas and the mixture is subjected to oxidative reforming with enriched air containing 30 to 35 of O₂, said enriched air being supplied in an amount to produce a secondary reformate containing principally hydrogen and nitrogen, accompanied by a minor amount of oxides of carbon (CO and CO₂). The secondary reformate subjected to shift reaction with steam results in conversion of contained CO to CO₂, thereby releasing hydrogen in an amount which together with the hydrogen previously present in said reformate obtains a H₂ /N₂ molar ratio of about 3/1. Carbon dioxide is removed and recovered from the shift reaction product by pressure swing adsorption in a first adsorbent bed. The other contaminants remaining are largely removed by further adsorption in second adsorbent bed in flow-communication with the first bed, the unadsorbed effluent being a syngas mixture consisting essentially of hydrogen and nitrogen in stoichiometric ratio for production of NH₃.

Claims

1. In the production and recovery of ammonia synthesis gas, the method which comprises:

providing a hydrocarbon vapor stream rich in methane and substantially free of sulfur compounds;

(b) dividing said stream into a minor portion comprising less than 45% by volume of said stream and a major portion;

(c) subjecting said minor portion to catalytic steam reforming at elevated temperature and pressure, thereby producing a primary reformate;

(d) subjecting said major portion to oxidative reforming in admixture with the obtained primary reformate by catalytic reaction

with an oxygen-enriched air stream containing 30-35% oxygen by volume, thereby producing a secondary reformate comprised principally of hydrogen, nitrogen and carbon oxides and containing a minor amount of contaminants including methane and argon;

the hydrogen content of said secondary reformate being less than that providing a 3;

1 mol ratio of hydrogen to nitrogen in said secondary reformate;

(e) subjecting said secondary reformate to a water gas shift reaction whereby contained carbon monoxide is converted to carbon dioxide and thereby also producing a further quantity of hydrogen, such that the H₂ /N₂ mol ratio in the shift reaction product is approximately 3;

1;

(f) removing carbon dioxide from the shift reacted secondary reformate by passing the same at superatmospheric pressure through a first bed of solid particulate adsorbent selective in retention of carbon dioxide, thereby producing a hydrogen-rich product effluent freed of carbonddioxide;

(g) passing said hydrogen-rich effluent into and through a second bed of solid particulate adsorbent selective in retention of carbon monoxide and methane as opposed to hydrogen and nitrogen and recovering from said second bed a mixture of hydrogen and nitrogen in approximately 3;

1 molar ratio and containing less than 25% of impurities on a dry basis.

2. The method as defined in claim 1 wherein said hydrocarbon vapor stream is desulfurized natural gas.

3. The method as defined in claim 2 wherein said minor portion subjected to steam reforming constitutes at least about 35 volume percent of said hydrocarbon vapor stream.

4. The method as defined in claim 2 wherein said minor portion subjected to steam reforming constitutes about 40 volume percent of said hydrocarbon vapor stream.

5. The mehod as defined in claim 2 wherein said catalytic steam reforming is carried out under operating conditions such that the primary reformate contains 15 to 20% by volume of unreacted methane.

6. The method as defined in claim 5 wherein said primary reformate contains about 17% by volume of unreacted methane.

7. The method as defined in claim 1 wherein the quantity of oxygen enriched air and unreacted methane in the gas adm-xture subjected to oxdative reforming is balanced with respect to the nitrogen content of said enriched air so as to produce a secondary reformate heaving a total hydrogen content, after water gas shift reaction, approximately in the ratio of 3 mols hydrogen per mol of nitrogen.

8. The method as defined in claim 1 wherein the mol percent oxygen in said enriched air stream is controlled with respect to the total methane content in the admixed feed charged to oxidative reforming so as to maintain an exit temperature of secondary reformate of 1680°

to 1720°

F.

9. The method as defined in claim 1 wherein said fist and second beds of adsorbent are provided in groups of columns of an integrated pressure swing adsorption system and wherein individual columns of the first group are arranged for controlled fluid flow communication with individual columns of the second group.

10. The method as defined in claim 9 wherein said adsorption system is arranged to provide a group of six columns, each containing a first bed of solid adsorbent and a group of three cllumns each containing a second bed of solid adsorbent.

11. The method as defined in claim 10 wherein retained carbon dioxide is desorbed from said first adsorbent bed by gas withdrawal from said bed to about ambient pressure level followed by evacuation.

12. The method as defined in claim 11 wherein part of said desorbed carbon dioxide is employed in rinsing a carbon dioxide laden bed at superatmospheric pressure prior to desorption. at least part of the remainder being recovered as product comprising over 98% CO₂

13. The method as defined in claim 10 wherein impurities including carbon monoxide and methane retained in a second adsorbent bed are removed therefrom by purging said bed with nitrogen-containing gas.

14. The method as defined in claim 2 wherein the mixture of hydrogen and nitrogen recovered from said second bed is compressed to a level of 1100-1200 psig and charged to a catalytic reaction fo production of ammonia.