EP0124159A2 - Procédé et appareil pour la préparation de gaz de synthèse - Google Patents

Procédé et appareil pour la préparation de gaz de synthèse Download PDF

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Publication number
EP0124159A2
EP0124159A2 EP84200474A EP84200474A EP0124159A2 EP 0124159 A2 EP0124159 A2 EP 0124159A2 EP 84200474 A EP84200474 A EP 84200474A EP 84200474 A EP84200474 A EP 84200474A EP 0124159 A2 EP0124159 A2 EP 0124159A2
Authority
EP
European Patent Office
Prior art keywords
screen
reactor
water bath
slag
wall
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.)
Granted
Application number
EP84200474A
Other languages
German (de)
English (en)
Other versions
EP0124159B1 (fr
EP0124159A3 (en
Inventor
Günter Klaus Eckstein
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0124159A2 publication Critical patent/EP0124159A2/fr
Publication of EP0124159A3 publication Critical patent/EP0124159A3/de
Application granted granted Critical
Publication of EP0124159B1 publication Critical patent/EP0124159B1/fr
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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
    • C10J3/466—Entrained flow processes
    • 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
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • 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
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the invention relates to a process for the preparation of synthesis gas by the partial combustion of a carbon-containing fuel with an oxygen-containing gas in a reactor in which the synthesis gas is discharged through a gas outlet at the top of the reactor and slag is removed through a slag discharge in the bottom of the reactor and passed by gravity into a water bath where it is solidified by quenching.
  • carbon-containing fuel is generally meant coal or another solid fuel, such as brown coal, peat, wood, coke, soot etc., but liquid fuels, such as tar sand oil or shale oil, and mixtures of liquid and particulate solid fuels, are also possible.
  • a moderator is also introduced into the reactor.
  • the object of the moderator is to exercise a moderating effect on the temperature on the reactor. This is ensured by endothermic reaction between the moderator and the reactants and/or products of the synthesis gas preparation.
  • Suitable moderators are steam and carbon dioxide.
  • the gasification is preferably carried out at a temperature in the range from 1200 to 1700°C and at a pressure in the range from 1 to 200 bar.
  • the reactor in which the preparation of synthesis gas takes place may have the shape of a sphere, cone block or a cylinder.
  • the reactor mainly has the shape of a circular cylinder.
  • the supply of carbon-containing fuel and oxygen-containing gas can take place through the bottom of the reactor. It is also possible to supply one of the reactants through the bottom of the reactor and one or more others through the side wall of the reactor. However, both the fuel and the oxygen-containing gas and the moderator are preferably supplied through the side wall of the reactor. This is advantageously performed by means of at least two burners arranged symmetrically in relation to the reactor axis in a low part of the side wall.
  • Part of the slag is entrained by the synthesis gas as small droplets and leaves the reactor via the gas outlet at the top of the reactor.
  • this problem is solved by arranging a screen in the water bath which screen holds back the relatively large clinker agglomerations while the relatively small granules pass through it.
  • the present invention therefore relates to a process for producing synthesis gas by the partial combustion of a carbon-containing fuel with an oxygen-containing gas in a reactor in which the synthesis gas is discharged through a gas outlet at the top of the reactor and molten slag is removed through a slag discharge in the bottom of the reactor and passed by gravity into a water bath where it is solidified by quenching, characterized in that at least part of the slag is passed in the water bath through a sloping screen covering the total horizontal cross section of the bath and slag captured by the screen is conducted to the wall of the bath.
  • the invention also relates to an apparatus for the partial combustion of a carbon-containing fuel with an oxygen-containing gas which apparatus comprises a reactor which is equipped with a gas outlet at the top and a slag discharge in the bottom, debouching into a water bath characterized in that the water bath is provided with a sloping screen covering its total horizontal cross section.
  • the screen is obliquely placed in the water bath. Consequently, the large clinker agglomerates present on the screen slide to the lowest part of the screen, while the small slag granules pass through the openings in the screen to the bottom of the water bath from which they can easily be discharged.
  • the screen is preferably flat and arranged obliquely in the reactor.
  • the retained clinker agglomerates now slide on the screen to the lowest points where the screen is fitted to the water bath wall.
  • the clinker agglomerates are advantageously removed from the screen through one or more openings in the water bath wall which are locked, suitably by one or more removable flanges, during the normal operation of the gasification process.
  • the screen has the shape of a part of a cylinder wall.
  • the convex side of the cylinder wall is directed upwards.
  • the screen then has the shape of a saddle.
  • the slag agglomerates retained by the screen slide to the reactor wall along the saddle surface to both its deepest points. Since these points are situated at the side of the saddle, the slag agglomerates slide over the side of the saddle to the two lowest points of intersection between the cylinder wall of screen and that of the water bath.
  • the solid slag agglomerates are unequally divided over the reactor wall also in said embodiment.
  • the gutter is advantageously fitted in the reactor obliquely, so that the lowest point of the gutter lies against the reactor wall.
  • the captured slag slides to said lowest point.
  • the cylinder radius/reactor radius ratio is preferably 1:1 to 10:1.
  • the captured solidified slag slides to part(s) of the reactor wall, from which it is periodically removed through openings therein, which openings are closed during normal operation of the gasification process.
  • the captured solidified slag downwards is advantageous to pass as evenly as possible distributed over . the circumference of the reactor wall. It is thus ensured that no part of the periphery of the reactor wall is extra heavily loaded with the slag agglomerates.
  • This object is preferably reached by using a screen having the form of a dome-shaped cap. Owing to the domed shape the captured slag agglomerates slide evenly to the lowest points on the screen. In order to ensure that the captured slag agglomerates on the dome-shaped cap start sliding to the lowest points the curve of the dome must be sufficient. Therefore, the radius ratio of the sphere to the reactor is preferably 1:1 to 10:1.
  • the apex of the conical surface is situated on the centre line of the water bath and its base is adjacent to the wall of the water bath.
  • the clinker agglomerates are evenly distributed over the space between the lower part of the conical surface and the inside of the water bath wall. From this space the agglomerates can be removed periodically through openings in the water bath wall which are closed during normal operation.
  • the screens suitably consist of a lattice work of bars.
  • the lattice work may consist of a bundle of parallel bars attached to the reactor wall. It is also possible to make connections between the parallel bars so that the shape of a perforated plate is formed.
  • the total screen is inmersed in the water bath. In this way the screen comes only in contact with solidified slag which does not stick to the screen whereas the molten slag which drops down from the reactor outlet is sticky and would adhere to the screen if not immersed in water.
  • the screen is preferably provided with vibrating means so that the screen is advantageously vibrated continuously or intermittently in order to obviate blocking of the screen.
  • the small solidified slag granules thus easily pass through the openings in the screen.
  • the large clinker agglomerations slide over the screen surface to the space neighbouring the water bath wall. As the large clinker agglomerations are predominantly produced during the start-up, shut-down, disturbance or upset periods of the gasification process only part of the screen surface will be covered by the agglomerations during normal process run.
  • Control and regulating devices, cooling systems, insulation, etc. are not shown in the Figure which gives a diagrammatic representation of part of an apparatus for the partial combustion of a carbon-containing fuel.
  • a carbon-containing fuel, an oxygen-containing gas and possibly a moderator are introduced into the reactor 1.
  • the partial combustion yields synthesis gas and slag.
  • the greater part of the liquid slag formed leaves the reactor via a slag discharge 3 in the bottom of the reactor 1.
  • the synthesis gas flows upwards and leaves the reactor 1 via a gas outlet (not shown) at the top of the reactor.
  • the liquid slag drips down from the outlet 3 and falls into a water bath 4 where it solidifies.
  • the coal powder had an average particle size of 5.10 -5 m and had the following composition on a dry and ashless basis:
  • the ash content was 8% by weight and the moisture content 1% by weight.
  • the oxygen-containing gas consisted of 99% pure oxygen.
  • the pressure in the reactor was 30 bar.
  • the quantity of slag drawn off via the slag discharge was 350 kg per hour. It dripped down into the water bath where it solidified.
  • 10 kg clinker agglomerates were formed having a diameter in the range from 40 to 100 mn. They did not pass through the screen but were kept in the water bath at the bottom of the annular space between the screen and the water bath wall. They were removed through openings in the water bath at the end of the gasification run which lasted 240 hours.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Industrial Gases (AREA)
EP84200474A 1983-05-02 1984-04-03 Procédé et appareil pour la préparation de gaz de synthèse Expired EP0124159B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3315917 1983-05-02
DE3315917 1983-05-02

Publications (3)

Publication Number Publication Date
EP0124159A2 true EP0124159A2 (fr) 1984-11-07
EP0124159A3 EP0124159A3 (en) 1985-07-31
EP0124159B1 EP0124159B1 (fr) 1988-05-18

Family

ID=6197913

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84200474A Expired EP0124159B1 (fr) 1983-05-02 1984-04-03 Procédé et appareil pour la préparation de gaz de synthèse

Country Status (7)

Country Link
EP (1) EP0124159B1 (fr)
JP (1) JPS59207986A (fr)
AU (1) AU557180B2 (fr)
CA (1) CA1249440A (fr)
DE (1) DE3471321D1 (fr)
NZ (1) NZ207998A (fr)
ZA (1) ZA843185B (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0623549Y2 (ja) * 1988-04-30 1994-06-22 石川島播磨重工業株式会社 石炭ガス化炉のスラグ排出装置

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2455127A1 (de) * 1974-11-21 1976-06-10 Shell Int Research Verfahren zum ausschleusen von rueckstaenden aus einem unter erhoehtem druck stehenden vergasungsraum

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5314704A (en) * 1976-07-27 1978-02-09 Gulf Oil Corp Method of gasifying ash containing solid carbonaceous particles
DE2851533A1 (de) * 1978-11-29 1980-06-12 Ruhrkohle Ag Kohlevergasungsanlage
US4220454A (en) * 1978-12-29 1980-09-02 Mcdowell-Wellman Company Process for gasifying pelletized carbonaceous fuels

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2455127A1 (de) * 1974-11-21 1976-06-10 Shell Int Research Verfahren zum ausschleusen von rueckstaenden aus einem unter erhoehtem druck stehenden vergasungsraum

Also Published As

Publication number Publication date
AU557180B2 (en) 1986-12-11
DE3471321D1 (en) 1988-06-23
JPS59207986A (ja) 1984-11-26
AU2750884A (en) 1984-11-08
CA1249440A (fr) 1989-01-31
NZ207998A (en) 1986-07-11
JPH0425993B2 (fr) 1992-05-06
ZA843185B (en) 1984-11-28
EP0124159B1 (fr) 1988-05-18
EP0124159A3 (en) 1985-07-31

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