Patent US4444568A successfully refreshed from Google Patents.
US4444568A
Expired / Lapsed
US
⏱️ 0.0 years remaining
Method of producing fuel gas and process heat fron carbonaceous materials
Assignee: GEA Group AG
•
Filing: 1982-03-26
•
Granted: 1984-04-24
•
Expires: 2002-03-26
Abstract
Abstract In a process of simultaneously producing fuel gas and process heat from carbonaceous materials wherein the carbonaceous materials are gasified in a first fluidized bed stage and the combustible constituents left after the gasification are subsequently burnt in a second fluidized bed stage the throughput rate and the flexibility are increased in that the gasification is carried out at a pressure of up to 5 bars and a temperature of 800° to 1100° C. by a treatment with oxygen-containing gases in the presence of steam in a circulating fluidized bed and 40 to 80% of the carbon contained in the starting material are thus reacted. Sulfur compounds are removed from the resulting gas in a fluidized state at a temperature in the range from 800° to 1000° C. and the gas is then cooled and subjected to dust collection. The gasification residue together with the by-products which have become available in the purification of the gas, such as laden desulfurizing agent, dust and aqueous condensate, are fed to another circulating fluidized bed and the remaining combustible constituents are burnt there with an oxygen excess of 5 to 40%.
Inventors
- 👤 Hans Beisswenger
- 👤 Georg Daradimos
- 👤 Martin Hirsch
- 👤 Ludolf Plass
- 👤 Harry Serbent
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-04 11:16
CPC Classifications
C; C10; C10J; C10J3/00; C10J3/72; C10J3/82; C10J3/84; C10J3/46; C10J3/463; C10J3/54; C10J3/721; C10J3/86; C10K; C10K1/00; C10K1/002; C10K1/003; C10K1/004; C10K1/02; C10K1/026; C10K1/08; F; F23; F23C; F23C10/00; F23C10/005; F23C10/02; F23C10/04; F23C10/08; F23C10/10; C10J2300/00; C10J2300/09; C10J2300/0953; C10J2300/0959; C10J2300/18; C10J2300/1807; C10J2300/1861; C10J2300/1884; F23C2206/00; F23C2206/10; F23C2206/101
Claims Analysis
Total Claims: 14
Claim 1
Independent Claim
254 words
A method of generating a fuel gas and process heat from a carbonaceous material which comprises: (a) reacting said carbonaceous material with oxygen-containing gases in the presence of steam in a circulating fluidized bed of a fluidized bed reactor at a temperature of 800° C. to 1100° C. in a first fluidized bed stage in which solids are entrained by gases from the fluidized bed, separating the entrained solids from the gas phase and recycling at least a portion of the separated solids to the fluidized bed to react 40 to 80% of the carbon contained in said material and produce a fuel gas therefrom contained in said gas phase; (b) contacting thereafter said gas phase at a temperature of 800° C. to 1000° C. with particles of a sulfur-trapping solid which are fluidized in said gas phase thereby removing sulfur therefrom; (c) recovering sulfur-trapping particles from the gas phase following step (b); (d) cooling the gas phase following the recovery of the sulfur-trapping particles therefrom and subjecting the cooled gas phase to at least one dust collection step to obtain said fuel gas and collect dust from the cooled gas phase; and (e) feeding solids withdrawn from said first circulating fluidized bed stage, the dust collected in step (d), the particles recovered in step (c), and aqueous condensate, to a second circulating fluidized bed stage and burning combustible constituents therein with an oxygen excess of 5 to 40% to produce a waste gas which is discharged to the atmosphere after process heat recovery.
Claim 2
Independent Claim
254 words
A method of generating a fuel gas and process heat from a carbonaceous material which comprises: (a) reacting said carbonaceous material with oxygen-containing gases in the presence of steam in a circulating fluidized bed of a fluidized bed reactor at a temperature of 800° C. to 1100° C. in a first fluidized bed stage in which solids are entrained by gases from the fluidized bed, separating the entrained solids from the gas phase and recycling at least a portion of the separated solids to the fluidized bed to react 40 to 80% of the carbon contained in said material and produce a fuel gas therefrom contained in said gas phase; (b) contacting thereafter said gas phase at a temperature of 800° C. to 1000° C. with particles of a sulfur-trapping solid which are fluidized in said gas phase thereby removing sulfur therefrom; (c) recovering sulfur-trapping particles from the gas phase following step (b); (d) cooling the gas phase following the recovery of the sulfur-trapping particles therefrom and subjecting the cooled gas phase to at least one dust collection step to obtain said fuel gas and collect dust from the cooled gas phase; and (e) feeding solids withdrawn from said first circulating fluidized bed stage, the dust collected in step (d), the particles recovered in step (c), and aqueous condensate, to a second circulating fluidized bed stage and burning combustible constituents therein with an oxygen excess of 5 to 40% to produce a waste gas which is discharged to the atmosphere after process heat recovery.
Claim 3
Dependent Claim
25 words
The method defined in claim 1 wherein 40 to 60% by weight of the carbon contained in the starting material are reacted in step (a).
Claim 4
Dependent Claim
40 words
The method defined in claim 1 wherein the fluidized bed of step (a) is fed with steam at least primarily in the form of fluidizing gas and with oxygen-containing gas at least primarily in the form of secondary gas (5).
Claim 5
Dependent Claim
41 words
The method according to claim 1, wherein the fluidized bed has an inlet and a residence time of 1 to 5 seconds of the gas is maintained in the fluidized bed of step (a) above the inlet for the carbonaceous material.
Claim 6
Dependent Claim
111 words
The method defined in claim 1 wherein the gases leaving the gasifying stage of step (a) are desulfurized in a fluidized bed reactor by a treatment with lime or dolomite or the corresponding calcined products having a particle diameter of d p 50=30 to 200 μm and for this purpose the fluidized bed reactor is operated to maintain therein a suspension having a mean solids density of 0.1 to 10 kg/m 3 and solids are passed through said reactor at such a rate that the weight of the solids passed through the fluidized bed per hour is at least 5 times the weight of the solids contained in the reactor shaft.
Claim 7
Dependent Claim
32 words
The method defined in claim 5 wherein said reactor is part of a circulating fluidized bed stage and the mean solids density in said reactor is 1 to 5 kg/m 3 .
Claim 8
Dependent Claim
29 words
The method defined in claim 1 wherein a gas velocity of 4 to 8 meters per second, calculated as empty-pipe velocity, is maintained during the desulfurization in step (b).
Claim 9
Dependent Claim
34 words
The method defined in claim 1 wherein all of the desulfurizing agent, including the sulfur-trapping solid of step (b) and any required for the combustion stage of step (e), is fed to step (b).
Claim 10
Dependent Claim
27 words
The method defined in claim 1 wherein the combustion of step (e) is effected in two stages with the aid of oxygen-containing gases fed at different levels.
Claim 11
Dependent Claim
73 words
The method defined in claim 9 wherein in step (e) fluidizing and secondary gases are supplied and the rates thereof controlled to maintain a suspension having a mean solids density of 15 to 100 kg/m 3 above the upper gas inlet and at least a substantial part of the heat generated by the combustion is dissipated through cooling surfaces provided within the free space of the fluidized bed above the upper gas inlet.
Claim 12
Dependent Claim
84 words
The method defined in claim 9 wherein in step (e) fluidizing gas and secondary gas are supplied and the rates thereof controlled to maintain above an upper gas inlet a mean solids density of the suspension of 10 to 40 kg/m 3 , hot solids are withdrawn from the circulating fluidized bed and are cooled by direct and indirect heat exchange in a fluidized state, and at least one partial stream of cooled solids is recycled to the circulating fluidized bed of step (e).
Claim 13
Dependent Claim
19 words
The method defined in claim 1 wherein additional carbonaceous materials are fed to the combustion stage of step (e).
Claim 14
Dependent Claim
44 words
A method according to claim 1, wherein a portion of the solids are recovered in a recirculating cyclone and a second portion of solids is recovered in subsequent stages, the latter recovered solids also being recycled into the fluidized bed of said second stage.
References Cited (Backward Citations)
US3807090A
Cited
US4085707A
Cited
US4026679A
Cited
US4165717A
Cited
US4069304A
Cited
US4111158A
Cited
US4347064A
Cited
USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1987-04-24 | 1987-10-24 | 1988-04-24 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1991-04-24 | 1991-10-24 | 1992-04-24 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1995-04-24 | 1995-10-24 | 1996-04-24 | $7700.00 | Window Closed / Lapsed |