EP0040868A1 - Procédé pour la préparation de gaz de synthèse - Google Patents

Procédé pour la préparation de gaz de synthèse Download PDF

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Publication number
EP0040868A1
EP0040868A1 EP81200474A EP81200474A EP0040868A1 EP 0040868 A1 EP0040868 A1 EP 0040868A1 EP 81200474 A EP81200474 A EP 81200474A EP 81200474 A EP81200474 A EP 81200474A EP 0040868 A1 EP0040868 A1 EP 0040868A1
Authority
EP
European Patent Office
Prior art keywords
reactor
fuel
oxygen
side wall
synthesis gas
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
EP81200474A
Other languages
German (de)
English (en)
Other versions
EP0040868B1 (fr
Inventor
Maarten Johannes Van Der Burgt
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
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Publication of EP0040868A1 publication Critical patent/EP0040868A1/fr
Application granted granted Critical
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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
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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 application relates to a process for the preparation of synthesis gas by the partial combustion of finely divided carbon-containing fuel by supplying oxygen-containing gas axially into a vertically arranged reactor and feeding the fuel through one or more passages in the side wall of the reactor.
  • the application also relates to a reactor suitable for carrying out the process.
  • the synthesis gas thus prepared substantially consists of carbon monoxide and hydrogen and contains in addition, inter alia, miner quantities of carbon dioxide and methane. If the partial combustion is not carried out with pure oxygen but with air, the product of course also contains much nitrogen.
  • carbon-containing fuel is preferably meant coal and other solid fuels, such as brown coal, peat, lignite, waste wood etc., but liquid fuels such as oil optionally derived from tar sand, are suitable.
  • the reactor is preferably mainly cylindrical, but oval, conical or rectangular reactors are also suitable.
  • the invention therefore relates to a process for the preparation of synthesis gas by the partial combustion of finely divided carbon-containing fuel by supplying oxygen-containing gas axially into a vertically arranged reactor and feeding the fuel via one or-more passages in the side wall of the reactor, characterized in that the oxygen-containing gas is supplied into the reactor bottom, the fuel is fed at an angle of 90° ( ⁇ 15°) with the centre line of the reactor and that the syrithesis gas formed is discharged at the top of the reactor.
  • the invention relates to a vertically arranged reactor for the preparation of synthesis gas by the partial combustion of a finely divided carbon-containing fuel, provided with an axial supply line for oxygen-containing gas and one or more passages in the side wall for feeding the fuel, characterized in that the supply line for oxygen-containing gas is fitted in the . bottom. of the reactor, that the passage(s) in the side wall is/are at an angle of 90 0 ( ⁇ 15 0 ) with the centre line of the reactor, and that a discharge for synthesis gas is fitted at the top.
  • the orifice angle of the sprayer or sprayers In order to charge the whole cross-section of the gas stream or of the reactor equally with fuel, the orifice angle of the sprayer or sprayers must be 180 0 . The result, however, is that a large proportion of the finely divided fuel strikes against the reactor side wall before it has fully reacted, as a result of which erosion and overheating take place. Therefore, the orifice angle of the sprayer is made somewhat smaller. The greater the number of sprayers, the higher the temperature at which the fuel is divided over the cross-section of the reactor. It is assumed that the inside of the reactor has a circular cross-section. It- is of course also possible to choose another shape that is adapted to the spraying pattern of the fuel inlets,. such as a square or an ellipse with the sprayers at two or all four angular points or ends of the centre lines.
  • the synthesis gas formed rises in the reactor since it has a higher temperature than the oxygen-containing gas and it has a lower molecular weight. It is therefore advantageous that the discharge is fitted at the top of the reactor. This discharge may be designed as described in the Netherlands patent applications Nos. 7408036 and 7704399.
  • the oxygen-containing gas is supplied at the bottom of the reactor, as a result of which it contacts the descending hot fuel and/or slag particles on its way up.
  • the oxygen-containing gas In cases where the slag is drained in liquid form it may happen that the slag cools off excessively and does not flow any more with the result that the discharge and the bottom will be blocked. In order to prevent this it may be useful to preheat the oxygen-containing gas in a higher degree and/or to locate the inlet(s) thereof at a higher level in the bottom of the reactor.
  • the fuel is preferably fed through at least two passages in the side wall of the reactor, which are fitted at the same height and symmetrically in relation to the centre line of the reactor.
  • the result is that a kind of flat disc of fuel particles is formed at said level in the reactor space.
  • the fuel particles are introduced into the reactor at such a speed that they do not fall at once, but not at such a speed that they hit the opposite side wall.
  • the upward pressure of the oxygen-containing gas balanc-es the downward-acting gravity, so that the fuel particles remain at the same height in the reactor until they have fully reacted with the oxygen.
  • this is not feasible in practice, since the fuel particles disintegrate during the partial combustion and the lighter particles are entrained more readily by the oxygen-containing gas.
  • the non-combustible remainders such as silicate
  • the non-combustible remainders are in the molten state owing to the high temperature and tend to agglomerate.
  • the heaviest ash particles descend, exchanging heat with the stream of oxygen-containing gas, to the bottom of the reactor where they form the slag and ash, the lighter particles leaving the reactor through the discharge with the synthesis gas as fly ash.
  • the slag is preferably discharged via the bottom of the reactor.
  • the reactor bottom is preferably shaped as a diffuser. This results in better utilization of the complete reactor space of the oxygen-containing gas and also in a decrease in the gas velocity. At a certain height the gas velocity has become so low that the injected fuel starts descending.
  • the finely divided fuel is preferably fed at the height of this point, a kind of shield being formed in this manner between the oxidizing preheating zone and the endothermic reduction zone.
  • the reactor diameter is determined as a function of the oxygen supply rate and temperature.
  • the bottom of the reactor becomes the side wall.
  • the fuel is preferably fed to the reactor at the height of the place where the bottom becomes the side wall of the reactor.
  • reaction temperature is approx. 1800°C, preferably between 1700 and 1900°C.
  • the feed of carbon-containing fuel is about 0.6 kg/s/m 3 of reactor space,-the oxygen-containing gas being supplied to the reactor in such quantities that the carbon/oxygen weight ratio lies between 0.6 and 0.9.
  • Fig. 1 is a diagrammatic longitudinal section of a reactor according to the invention
  • Fig. 2 is a cross-section along the line II-II in Fig. 1. Cooling and insulation, valves,thermometers, etc., are not shown in the drawings.
  • a discharge 2 for synthesis gas and fly ash is provided in a top 1.
  • passages 4 for fuel dust for example coal dust that has been pressurized in some known device and can be blown into the reactor with an inert gas, for example synthesis gas, steam or nitrogen.
  • a bottom 5 is conical downward and becomes a slag discharge--6 in the centre of which an oxygen supply line 7 is located.
  • the fuel passages 4 are located at regular intervals in the side wall 3. By way of example four passages are drawn and the sprayers have an orifice angle of about 90°.
  • the fuel dust is drawn as dots.
  • a quantity of 40,000 kg/h of a finely ground coal dust and 133 kg of nitrogen at 40°C as carrier gas were blown through the passages 4 into a reactor having the above-mentioned shape and an internal volume of 18 cu.m.
  • the coal dust had an average particle size of 50 p and had the following composition on a dry ashless basis:
  • the ash content was 12.6% by weight and the moisture content was 2% by weight.
  • the reactor had a pressure of 30 atm.
  • a quantity of 33,500 kg/h of gas of 200°C and of the following composition was introduced through the supply line 7:
  • the synthesis gas formed was practically free from soot and contained 3% by weight of fly ash which was separated off in a cyclone. The remaining solids were discharged as molten slag through 6 and dropped in a water bath to be cooled. The cooled slag-water mixture was drained through a lock system, the high pressure in the reactor being maintained.

Landscapes

  • 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)
EP81200474A 1980-05-23 1981-05-04 Procédé pour la préparation de gaz de synthèse Expired EP0040868B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL8002989 1980-05-23
NL8002989 1980-05-23

Publications (2)

Publication Number Publication Date
EP0040868A1 true EP0040868A1 (fr) 1981-12-02
EP0040868B1 EP0040868B1 (fr) 1984-08-01

Family

ID=19835352

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81200474A Expired EP0040868B1 (fr) 1980-05-23 1981-05-04 Procédé pour la préparation de gaz de synthèse

Country Status (5)

Country Link
EP (1) EP0040868B1 (fr)
AU (1) AU541700B2 (fr)
CA (1) CA1173250A (fr)
DE (1) DE3165192D1 (fr)
ZA (1) ZA813409B (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1010028B (zh) * 1985-05-29 1990-10-17 国际壳牌研究有限公司 褐煤气化器

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
LU29330A1 (fr) *
DE880623C (de) * 1951-04-10 1953-06-22 Hans Schmalfeldt Verfahren und Vorrichtung zum Vergasen von Kohlenstaub
USB541376I5 (fr) * 1975-01-15 1976-02-17
US4200495A (en) * 1978-09-18 1980-04-29 Barry Liss Prevention of defluidization in the treatment of caking carbonaceous solids

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US541376A (en) * 1895-06-18 Box-trimming machine

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
LU29330A1 (fr) *
DE880623C (de) * 1951-04-10 1953-06-22 Hans Schmalfeldt Verfahren und Vorrichtung zum Vergasen von Kohlenstaub
USB541376I5 (fr) * 1975-01-15 1976-02-17
US4200495A (en) * 1978-09-18 1980-04-29 Barry Liss Prevention of defluidization in the treatment of caking carbonaceous solids

Also Published As

Publication number Publication date
CA1173250A (fr) 1984-08-28
AU541700B2 (en) 1985-01-17
ZA813409B (en) 1982-06-30
EP0040868B1 (fr) 1984-08-01
AU7090381A (en) 1981-11-26
DE3165192D1 (en) 1984-09-06

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