Method for using fast fluidized bed dry bottom coal gasification

• US 4,400,181 A
• Filed: 01/28/1982
• Issued: 08/23/1983
• Est. Priority Date: 01/28/1982
• Status: Expired due to Term

• Current Assignee: United States Department of Energy (Government of the United States of America)
• Original Assignee: Hydrocarbon Research Incorporated
• Inventors: Kydd, Paul H., Snell, George J.
• Primary Examiner(s): LINDSAY JR, ROBERT
• Application Number:
  US06/343,626
• Time in Patent Office: 572 Days
• Field of Search: 48/197 R, 48/206, 48/202, 48/203, 48/62 R, 48/63, 48/73, 48/76, 48/77
• US Class Current: 48/197.00R
• CPC Class Codes: C10J 2200/152 Nozzles or lances for introducing gas, liquids or suspensions
• CPC Class Codes: C10J 2300/093 Coal
• CPC Class Codes: C10J 2300/0943 Coke
• CPC Class Codes: C10J 2300/0946 Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
• CPC Class Codes: C10J 2300/0956 Air or oxygen enriched air
• CPC Class Codes: C10J 2300/0959 Oxygen
• CPC Class Codes: C10J 2300/0976 as steam
• CPC Class Codes: C10J 2300/1884 with one stream being synthesis gas
• CPC Class Codes: C10J 2300/1892 with one stream being water/steam
• CPC Class Codes: C10J 3/54 Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
• CPC Class Codes: C10J 3/56 Apparatus; Plants
• CPC Class Codes: C10J 3/74 Construction of shells or jackets
• CPC Class Codes: C10J 3/78 High-pressure apparatus

Abstract

Carbonaceous solid material such as coal is gasified in a fast fluidized bed gasification system utilizing dual fluidized beds of hot char. The coal in particulate form is introduced along with oxygen-containing gas and steam into the fast fluidized bed gasification zone of a gasifier assembly wherein the upward superficial gas velocity exceeds about 5.0 ft/sec and temperature is 1500°-1850° F. The resulting effluent gas and substantial char are passed through a primary cyclone separator, from which char solids are returned to the fluidized bed. Gas from the primary cyclone separator is passed to a secondary cyclone separator, from which remaining fine char solids are returned through an injection nozzle together with additional steam and oxygen-containing gas to an oxidation zone located at the bottom of the gasifier, wherein the upward gas velocity ranges from about 3-15 ft/sec and is maintained at 1600°-200° F. temperature. This gasification arrangement provides for increased utilization of the secondary char material to produce higher overall carbon conversion and product yields in the process.

Claims

1. A process for gasifying particulate hydrocarbon feed materials to produce a fuel gas product, having low-to-medium heating value, comprising:

(a) introducing the hydrocarbon feed material with steam and oxygen into a gasification zone containing a fast fluidized bed of char particles for gasification therein, said zone being maintained at temperature of 1500°

-1850°

F., at pressure exceeding about 30 psig, and at upward superficial gas velocity exceeding about 5 ft/sec to heat and gasify the feed and produce a gaseous material;

(b) withdrawing said gaseous material along with char particles from the upper portion of the gasification zone and passing the materials to a primary gas-solids separation step for char solids removal;

(c) withdrawing a first gas stream from said primary gas-solids separation step and returning particulate char solids to the gasification zone;

(d) passing said first gas stream to a secondary gas-solids separation step and removing fine char solids therefrom;

(e) returning the fine particulate char solids from the secondary gas-solids separation step to the lower end of a fluidized bed oxidation zone located immediately below the fast fluidized bed gasification zone;

said oxidation zone having temperature maintained within the range of 1600°

-2000°

F.; and

(f) withdrawing a fuel gas product stream from the secondary gas-solids separation step.

2. The process of claim 1, wherein the feed stream is introduced into the gasification zone through a shrouded injection nozzle, and the velocity in the solids injection nozzle is between about 6 and about 100 ft/sec.

3. The process of claim 1, wherein the feed is coal and the weight ratio of gasification zone char to coal is between about 20 and 30.

4. The process of claim 1, wherein the fine char solids from the secondary cyclone separator are returned to the oxidation zone through a gas shrouded nozzle together with an oxygen-containing gas.

5. The process of claim 1, wherein the gasification zone temperature is within the range of 1600°

-1800°

F., the pressure is 50-750 psig, and the upward superficial gas velocity is 6-20 ft/sec.

6. The process of claim 1, wherein the temperature of the oxidation zone is maintained within the range of 1650°

-1950°

F.

7. The process of claim 1, wherein the feed material is anthracite coal having particle size within the range of 0.040-0.004 inch (18-140 mesh U.S. Sieve Series).

8. The process of claim 4, wherein the secondary char solids are injected into the oxidation zone at a velocity within the range of 3-10 ft/sec and the shroud gas has exit velocity within the range of 20-80 ft/sec to provide a grinding effect on the char solids.

9. The process of claim 1, wherein the coarse ash particles are withdrawn from the lower portion of the oxidation zone.

10. A process for gasifying coal to produce a fuel gas product, having low-to-medium heating value, comprising:

(a) introducing coal feed into a gasification zone containing a fast fluidized bed of char particles for gasification therein, said zone being maintained at 1500°

-1850°

F. temperature range, at pressure exceeding about 30 psig and at upward superficial gas velocity exceeding about 5 ft/sec, and a weight ratio of char to coal feed maintained between about 20 to 30 to heat and gasify the coal and produce a gaseous material;

(b) withdrawing said gas and substantial char from the upper portion of the fast fluidized bed gasification zone and passing the materials to a primary gas-solids separation step for char solids removal;

(c) withdrawing a first gas stream from said primary solids separation step and returning particulate char solids to the gasification zone;

(d) passing said first gas stream to a secondary gas-solids separation step and removing a fine char solids therefrom;

(e) returning the fine particulate char solids from the secondary gas-solids separation step through a gas shrouded nozzle into the lower end of a fluidized bed oxidation zone maintained at temperature within the range of 1600°

-2000°

F. and located immediately below the fast fluidized bed gasification zone; and

(f) withdrawing a fuel gas product stream from the secondary gas-solids separation step.

11. The process of claim 10, wherein the percentage conversion of carbon in the coal exceeds about 50 W %.