CN1025867C - Method for operating gasifying equipment of solid fuels and devices of utilization of process - Google Patents
Method for operating gasifying equipment of solid fuels and devices of utilization of process Download PDFInfo
- Publication number
- CN1025867C CN1025867C CN89108236A CN89108236A CN1025867C CN 1025867 C CN1025867 C CN 1025867C CN 89108236 A CN89108236 A CN 89108236A CN 89108236 A CN89108236 A CN 89108236A CN 1025867 C CN1025867 C CN 1025867C
- Authority
- CN
- China
- Prior art keywords
- flying dust
- gasification
- fuel
- gasification combustor
- oxygen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/1223—Heating the gasifier by burners
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Abstract
Process for operating a plant for the gasification of fine-grained to dusty solid fuels, having a gasification reactor equipped with gasification burners, a device for separating fly dust from the crude gas, a fly dust receiver and a device for recycling fly dust into the gasification reactor. The gasification burners burn into the gasification reactor with a fuel/reactant jet which is rotationally symmetrical at the gasification burner outlet. The fly dust with its crude gas content and its residual carbon is introduced by a carrier gas stream into the axis of at least one fuel/reactant jet, introduced by the fuel/reactant jet into the primary reaction zone and fused therein. Plant suited for operating the process is also indicated.
Description
Relate generally to particulate of the present invention is to the solid-fuelled gasification of dust-like.Solid fuel especially refers to similar substances such as coal, coke, petroleum coke.Gasification occurs in oxygen and/or air, also occurs under the flowing water vapor action in case of necessity, and forms a kind of raw gas that mainly consists of carbon monoxide and hydrogen at last.The flying dust that raw gas carries has the residual carbon composition.This gasification is a pressurized gasification.
The present invention is specifically related to a kind of working method of particulate and dust-like solid combustion gasification installation.This device comprises the gasifying reactor that is equipped with gasification combustor, the device of separating out flying dust from raw gas, flying dust collector and makes flying dust return the device of gasifying reactor.In this process, the fuel/reagent beam of gasification combustor exit symmetry rotation enters in the gasifying reactor always, and forms a high temperature primary reaction zone by fuel/reagent beam in gasifying reactor.The invention still further relates to a kind of device, this device is particularly useful for the enforcement of aforesaid method.In fuel/this word of reagent beam, reagent had both referred to that oxygenant also referred to established reaction product, also referred to buffer gas (Moderatorgas) and carrier gas in case of necessity.
(109B1), flying dust mixes mutually with fresh fuel and enters gasification combustor together with fuel for european patent application the 0th, 072,457B1 and 0.109 in the prior art measure scope as starting point of the present invention.This method is very expensive, and requires flying dust is carried out special processing, promptly requires to have many complicated technology facilities of very big protection safety.By being full of the raw gas that contains carbon monoxide and hydrogen in the hole of the flying dust of extracting out in the coal gas or the space, have only by repeatedly just being diluted to below the limiting danger line or being eliminated with indifferent gas flushing and displacement.To also very complicated and expensive by the processing of isolated raw gas in the flying dust, reason is, sulfur-bearing usually in the raw gas falls for the combustion of can not lighting a fire of the cause of protection environment, can not burn or enters in the atmosphere with other any methods.Problem in addition also has: because the flying dust that mixes in the fresh fuel reduces the calorific value of fuel, and the thermodynamics and the reaction kinetics of gasification exerted an influence.
Task of the present invention is, when implementing the method for this paper one switch narration, flying dust is not being done special processing, is not being influenced under the situation of gasification thermodynamics or reaction kinetics, makes flying dust fully enter slag and while burning residual carbon.
For finishing this task, the present invention points out: flying dust and raw gas composition thereof and residual carbon are gone into the axle center of at least one fuel/reagent beam with gas delivery, send into primary reaction zone by this beam again and melt in this reaction zone.According to embodiment preferably of the present invention, flying dust is introduced along the axle of gasification combustor.The present invention utilizes this fact, promptly comes in the process of gasification of solid fuels at the fuel/reagent beam with the symmetry rotation, and fuel/reagent beam is very stable aspect gasdynamics, one flying dust can be sent into the primary reaction zone.Gasification reaction obviously just begins in fuel-stream of reactants, this and in the primary reaction zone gasification reaction be not subjected to the influence of flying dust, this situation helps to make residual carbon wherein also to be gasified.In any case the flying dust flow can not be excessive.Common high-temperature condition appears in the primary reaction zone, 2000 ℃ of degree or higher for example, and this is that the fusing flying dust is necessary.It is shocking, although returned flying dust by the present invention,, the flying dust of being discharged by primary reaction zone increases hardly, and in the raw gas of non-purification, flying dust has not produced dysgenic enrichment, and therefore, described cyclic motion is possible.Say that in principle flying dust returns gasifying reactor, promptly returning gasifying reactor by delivery nozzles special, that be separated with gasification combustor is known (DE2409008 C2).This method affect gasification reaction almost is not applied.In the practice more commonly (DE-AS 2325204), in a reactor flying dust top blast is become slag, in this process, the residual carbon of together bringing into also becomes slag usually.
Also have many multiple possibilities of improving the inventive method in every respect.Adopt following gasification combustor to have superiority, this gasification combustor have one with the concentric oxygen delivery passage of gasification combustor axle, circumjacent outside annular fuel transfer passage and one are close to or non-adjacent landing around the annular secondary oxygen delivery passage of above-mentioned passage.At this, the present invention's suggestion is carried the flying dust in the oxygen delivery channel axis one time with a special transfer passage.Elementary Oxygen Flow can be divided into two concentric tributaries.For not influencing gasification reaction, being preferably the gasification combustor that some are used for the transporting flying dust is set, makes the little about 0.01-0.15 of flying dust throughput ratio fuel flow doubly.This in fact correspondingly is applicable to other design variables of gasification combustor.Carry by all gasification combustors as flying dust, just this proportionlity can realize on the general gasifying reactor of the described structure of beginning without difficulty.Need not take additional measures aspect oxygen delivery and the oxygen delivery adjusting.On the contrary, just be enough to according to the oxygen of content ratio raising of residual carbon in the flying dust and/or the amount of secondary oxygen.
Content of the present invention also comprises and is particularly useful for implementing a device of the present invention.To be described further it by an accompanying drawing below.This unique figure is the sketch map according to apparatus of the present invention.
The essential structure of installing shown in the figure is: gasification reactor 1 that is equipped with gasification combustor 2, one be used for from raw gas separate out the device 3 of flying dust, flying dust collector 4(it have make flying dust return the device of gasification reactor 1). The fuel of gasification combustor 2 exit symmetrical rotaries/reactant beam 5 enters gasification reactor 1 always, and produces a high temperature primary reaction zone 6 at this. Shown in the section A that has amplified, gasification combustor 2 has a flying dust central transport channel 7. It is carried the circular passage 8 of primary oxygen to center on by one. In addition, the structure of this device makes central transport channel 7 join by a dosage setter 9 and flying dust collector 4. Clearly, can by general during to solid fuel gasification common the sort of mode gasification combustor 2 is set.
Enter flying dust by the raw gas that is loaded with flying dust that comes out in the gasification reactor 1 by pipeline 10 and separate out device 3, this device is cyclone separator. Flying dust is separated at this. Separated flying dust (also containing raw gas in its hole or space) sinks in the flying dust collector 4 by pipeline 11. Handle dosage setter 9 by these flying dust collector 4 places. Dosage setter 9 comprises two measurers 12. Flying dust timing free-falling from the flying dust collector enters measurer 12 by pipeline 13. Make measurer 12 pressurizeds that fill separately flying dust by pipeline 14 usefulness purification raw gas or inert gas, this pressure independent is critical, as long as be higher than the pressure in the gasification reactor 1. Under enough pressure, enter the pipeline that pass into gasification combustor 2 through piping 16 by pipeline 15 flying dust. Gasification combustor 2 passes into central flying dust transfer passage 7, and this passage is centered on by primary oxygen annular transfer passage 8. Pipeline 17 is the gas relief line of each sky measurer 12, passes into by flying dust and separates out the purification raw gas pipeline 18 that device 3 stretches out. Clearly, the method must be aided with the technological means of modern process engineering aspect. Assembled common measurement and controlling organization, (referring to P 3813357.1) implemented in necessary regulation and control measure under area of computer aided for this reason.
These the relationship between quantities are drawn by following reason:
Dropping into 80% of ash in the gasifying reactor together with fuel becomes slag row, and 20% ash adds that the coal dust and the gas of gasification are not discharged from together.Be contained in 80% of solid matter (flying dust) in the gas and in the flying dust separator, separated out and return under the described conditions gasification combustor.
Embodiment
Fuel (coal) is analyzed C 68.40 weight %wf
H 4.40 weight %wf
O 6.03 weight %wf
N 1.60 weight %wf
S 1.10 weight %wf
Cl 0.17 weight %wf
Ash 18.30 weight %wf
Totally 100.00 weight %wf
Hu 27.1326 MJ/kgwf
Coal dust amount 13,005 kgwf/h of each burner
Chemical heat 352,860 MJ/h of the coal of each burner
Dust Capacity 540 kgwf/h of each burner
Chemical heat 2,824 MJ/h of the dust of each burner
Amount 17.25 m of raw gas in the dust gap
3 Ntr/ h
Chemical heat 192.8 MJ/h of raw gas
Claims (7)
1, particulate is to the treatment process of the solid-fuelled combusted gas generant flying dust of dust-like, use a kind of gasification installation in this method, this device comprises a gasifying reactor that is equipped with gasification combustor, a device that is used for separating out flying dust from raw gas, a flying dust collector and a device that makes flying dust return gasifying reactor, fuel/reagent the beam of gasification combustor exit symmetry rotation enters gasifying reactor always, fuel/reagent beam forms a high temperature primary reaction zone in gasifying reactor, it is characterized in that, flying dust and raw gas composition thereof and remaining char are sent into the axle center of at least one fuel/reagent beam by delivery air, and bring primary reaction zone into and in this fusing by fuel/reagent beam.
According to the method for claim 1, it is characterized in that 2, flying dust is introduced along the axle of each gasification combustor.
3, according to the method for one of claim 1 or 2, work with gasification combustor, gasification combustor have one with the concentric oxygen delivery passage of gasification combustor axle, a circumjacent outside annular fuel transfer passage, and one more outside round the secondary oxygen of annular transfer passage annular transfer passage, it is characterized in that one time the interior flying dust of oxygen delivery channel axis is carried by a central transport channel (7).
According to the method for claim 1, it is characterized in that 4, gasification combustor is used to carry one flying dust stream, the little about 0.01-0.15 of this strand flying dust throughput ratio fuel flow doubly.
5, according to the method for claim 1, it is characterized in that, improve the amount of oxygen and/or secondary oxygen according to remaining char content in the flying dust.
According to the method for claim 1, it is characterized in that 6, flying dust is sent into through all gasification combustors.
7, enforcement is according to the device of the method for one of claim 1-5, it has the basic structure that provides in the claim 1, it is characterized in that, gasification combustor (2) has a central transport channel (7) that is used for flying dust, this passage is centered on by an oxygen annular transfer passage (8), and central transport channel (7) is joined by a dosage setter (9) and flying dust collector (4).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3837587.7 | 1988-11-05 | ||
| DE3837587A DE3837587C1 (en) | 1988-11-05 | 1988-11-05 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1042560A CN1042560A (en) | 1990-05-30 |
| CN1025867C true CN1025867C (en) | 1994-09-07 |
Family
ID=6366555
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89108236A Expired - Fee Related CN1025867C (en) | 1988-11-05 | 1989-10-30 | Method for operating gasifying equipment of solid fuels and devices of utilization of process |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP0370201B1 (en) |
| CN (1) | CN1025867C (en) |
| DD (1) | DD285990A5 (en) |
| DE (3) | DE3837587C1 (en) |
| DK (1) | DK548489A (en) |
| ES (1) | ES2033504T3 (en) |
| PL (1) | PL161778B1 (en) |
| ZA (1) | ZA897381B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4132770A1 (en) * | 1991-10-02 | 1993-04-08 | Kurt Kugler | Treatment of incinerator airborne ash and dust - comprises sepg. into coarse and fine fractions and removing heavy metals |
| DE4407651C1 (en) * | 1994-03-08 | 1995-10-26 | Rheinische Braunkohlenw Ag | Prodn. of synthesis gas from by-prods., by steam-oxygen@ gasification, |
| US7540891B2 (en) | 2003-10-31 | 2009-06-02 | Shell Oil Company | System and method for stripping toxigas from a powder |
| PL224212B1 (en) | 2012-10-12 | 2016-11-30 | Sarre Piotr | Method for gasification of coal-bearing raw materials, and coal char and layout of equipment for performing this process |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL171691C (en) * | 1973-02-26 | 1983-05-02 | Shell Int Research | PROCESS FOR THE PREPARATION OF HYDROGEN AND / OR CARBON MONOXIDE-CONTAINING GASES BY INCOMPLETE BURNING OF FUELS AND SEPARATION OF THE SOLID PARTICLES THEREFORE. |
| US3929429A (en) * | 1974-09-26 | 1975-12-30 | Texaco Inc | Fuel gas from solid carbonaceous fuels |
| US4168956A (en) * | 1977-08-18 | 1979-09-25 | Combustion Engineering, Inc. | Method of operating a coal gasifier |
| DE2947222A1 (en) * | 1979-11-23 | 1981-05-27 | Carbon Gas Technologie GmbH, 4030 Ratingen | METHOD FOR GASIFYING SOLID, DUST-MADE TO PIECE-LIKE CARBONATED MATERIAL |
| DE3132506A1 (en) * | 1981-08-18 | 1983-03-03 | Hoechst Ag, 6000 Frankfurt | METHOD AND DEVICE FOR PRODUCING SYNTHESIS GAS |
| DE3372867D1 (en) * | 1982-11-11 | 1987-09-10 | Shell Int Research | Process for the partial combustion of solid fuel with fly ash recycle |
| US4480559A (en) * | 1983-01-07 | 1984-11-06 | Combustion Engineering, Inc. | Coal and char burner |
-
1988
- 1988-11-05 DE DE3837587A patent/DE3837587C1/de not_active Expired - Fee Related
-
1989
- 1989-09-26 ES ES198989117731T patent/ES2033504T3/en not_active Expired - Lifetime
- 1989-09-26 DE DE8989117731T patent/DE58901693D1/en not_active Expired - Fee Related
- 1989-09-26 EP EP89117731A patent/EP0370201B1/en not_active Expired - Lifetime
- 1989-09-28 ZA ZA897381A patent/ZA897381B/en unknown
- 1989-10-26 PL PL89282032A patent/PL161778B1/en unknown
- 1989-10-30 CN CN89108236A patent/CN1025867C/en not_active Expired - Fee Related
- 1989-11-01 DD DD89334112A patent/DD285990A5/en not_active IP Right Cessation
- 1989-11-03 DK DK548489A patent/DK548489A/en not_active Application Discontinuation
- 1989-12-19 DE DE3941816A patent/DE3941816A1/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| EP0370201B1 (en) | 1992-06-17 |
| PL161778B1 (en) | 1993-07-30 |
| ES2033504T3 (en) | 1993-03-16 |
| EP0370201A1 (en) | 1990-05-30 |
| DE58901693D1 (en) | 1992-07-23 |
| ZA897381B (en) | 1990-07-25 |
| DK548489A (en) | 1990-05-06 |
| DD285990A5 (en) | 1991-01-10 |
| DE3941816A1 (en) | 1991-06-20 |
| DK548489D0 (en) | 1989-11-03 |
| DE3837587C1 (en) | 1990-05-23 |
| CN1042560A (en) | 1990-05-30 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |