WO2005090526A1 - Gazeification de matiere carbonee - Google Patents

Gazeification de matiere carbonee Download PDF

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Publication number
WO2005090526A1
WO2005090526A1 PCT/IB2005/050830 IB2005050830W WO2005090526A1 WO 2005090526 A1 WO2005090526 A1 WO 2005090526A1 IB 2005050830 W IB2005050830 W IB 2005050830W WO 2005090526 A1 WO2005090526 A1 WO 2005090526A1
Authority
WO
WIPO (PCT)
Prior art keywords
particle size
feedstock
gasifier
coal
lower limit
Prior art date
Application number
PCT/IB2005/050830
Other languages
English (en)
Inventor
Martin Jakobus Keyser
Roelof Lodewyk Jacobus Coetzer
Johannes Christoffel Van Dyk
Original Assignee
Sasol Technology (Proprietary) Limited
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 Sasol Technology (Proprietary) Limited filed Critical Sasol Technology (Proprietary) Limited
Priority to CA002559191A priority Critical patent/CA2559191A1/fr
Priority to MXPA06010237A priority patent/MXPA06010237A/es
Priority to US10/592,542 priority patent/US20080034660A1/en
Priority to AU2005223495A priority patent/AU2005223495A1/en
Publication of WO2005090526A1 publication Critical patent/WO2005090526A1/fr

Links

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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous 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
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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

  • THIS INVENTION relates to gasification of carbonaceous material.
  • it relates to a process for gasifying a particulate carbonaceous feedstock.
  • gasifiers for the conversion of carbonaceous feedstocks, usually and predominantly coal, to crude gas which includes steam, carbon dioxide, hydrogen, carbon monoxide, methane and a broad range of hydrocarbons such as heavy oils, tars and pitches, is well known.
  • a gasifier is a fixed bed dry bottom gasifier (also known as a moving bed dry ash gasifier).
  • These gasifiers can make use of lump coal with a typical particle size distribution range from about 4 mm or 8 mm up to about 70 mm or 100 mm.
  • these gasifiers do not require much feedstock preparation.
  • particle top size is determined by a crusher opening of a crusher used for crushing the feedstock, while the particle bottom size is determined by a bottom screen aperture in a screening plant, which is typically located before a gasification plant.
  • a process for gasifying a carbonaceous particulate feedstock including dividing the carbonaceous particulate feedstock into at least two feedstock fractions, each feedstock fraction including particulate material within a predetermined particle size range so that there are at least a smaller particle size feedstock and a larger particle size feedstock; and feeding the smaller particle size feedstock to at least one gasifier and the larger particle size feedstock to at least one other gasifier.
  • a gasifier receives only one of the feedstocks and typically none of the gasifiers receives more than one of the feedstocks.
  • the carbonaceous particulate feedstock is typically coal.
  • each feedstock fraction has a narrower particle size distribution range than the particulate carbonaceous feedstock from which the feedstock fractions have been derived.
  • the smaller particle size feedstock may have a particle size distribution with an upper limit which is at least about 5 times its lower limit, preferably at least about 6 times its lower limit, more preferably at least about 7 times its lower limit, e.g. between about 8 and about 9 times its lower limit.
  • Lower and upper limits are typically determined by screen sizes used to prepare the two or more feedstocks each with a predetermined particle size range.
  • the larger particle size feedstock may have a particle size distribution with an upper limit which is at least about 1.5 times its lower limit, preferably at least about twice its lower limit, more preferably at least about 2.5 times its lower limit, e.g. between about 2.6 and about 3 times its lower limit.
  • the aforementioned particle size distribution ranges are thus substantially narrower than the particle size distribution range of a typical conventional coal feedstock, in which the upper particle size limit is typically at least about 12 times, e.g. about 15 times the lower particle size limit of the range.
  • the upper limit of the particle size distribution range of the smaller particle size feedstock is typically about the same as the lower limit of the particle size distribution range of the larger particle size feedstock.
  • This particle size which thus lies between the lower limit of the particle size distribution range of the smaller particle size feedstock and the upper limit of the particle size distribution range of the larger particle size feedstock, depends on a number of factors, such as the effect of the mining method on the particle size distribution of run- of-mine coal, the mechanical strength of the coal deposit and the number of gasifiers which have to be supplied with each feedstock fraction.
  • the smaller particle size feedstock is fed to a gasifier or gasifiers at a mass flow rate at least about twice, more preferably at least about 2.5 times, even more preferably at least about 2.75 times, e.g. about 3 times the mass flow rate at which the larger particle size feedstock is fed to a gasifier or gasifiers.
  • the larger particle size feedstock may include more non-carbonaceous material on a percentage by mass basis, such as out-of-seam matter, than the smaller particle size feedstock.
  • Non-carbonaceous material is often present in a coal feedstock due to accidental extraction of the roof and the floor of the coal seam during mining, or because a coal deposit contains mineral intrusions inside the seam which are thus inadvertently extracted with the coal.
  • the process may include subjecting at least the larger particle size feedstock to a beneficiation or an upgrading stage.
  • the upgrading stage may include removing at least a portion of the non-carbonaceous material from the larger particle size feedstock.
  • the upgrading stage may include a dense medium separation step.
  • the upgrading stage may include a size reduction step in which the average particle size of the particulate carbonaceous material of the larger particle size feedstock is reduced.
  • the gasifier or gasifiers fed with the smaller particle size feedstock may be operated with an oxygen to pure gas volumetric ratio of between 0.19 and 0.21 and coal as feedstock and may produce a raw gas comprising between 26 and 28 mole % CO 2 , preferably between 27 and 28 mole % CO 2 at a pure gas yield of at least 1640 Nm 3 /ton of dry ash free coal (DAF coal), preferably at least 1660 Nm 3 /ton of dry ash free coal.
  • the pure gas yield may be delivered at a standard deviation of not more than 28, preferably not more than 17 Nm 3 /ton of dry ash free coal.
  • Figure 1 shows a graph of coal feedstock stone content
  • Figure 2 graphically illustrates feasible areas of an operating regime for a gasifier receiving a feedstock with a broad particle size distribution of 70x4 mm
  • Figure 3 graphically illustrates feasible areas of an operating regime for a gasifier receiving a feedstock with a narrow particle size distribution of 35x4 mm
  • Figure 4 graphically illustrates feasible areas of an operating regime for a gasifier receiving a feedstock with a narrow particle size distribution of 35x4 mm, with stone content as one parameter
  • Figure 5 shows a graph of oxygen to pure gas ratios versus raw gas CO 2 concentration for reference tests and invention tests
  • Figure 6 shows a graph of pure gas yield versus raw gas CO 2 concentration in raw gas for the reference tests and invention tests
  • Figure 7 shows a graph of pure gas yield versus stone content of the coal feedstock for the reference tests and invention tests
  • Figure 8 shows a graph of gasifier bed pressure drop versus oxygen load for the reference tests and invention tests.
  • the final particle size distribution of the coal fed to the test gasifier was obtained by a process of dry and wet screening.
  • Run-of-mine coal was first dry screened with a 35 mm screen, an overflow providing a coarse (100x35 mm) fraction or test material, and an underflow of the screen (-35 mm) providing a fine fraction or test material.
  • the second step in the preparation was to screen the -35 mm material in order to remove the -4 mm fines and size the fine test material (35x4 mm). This polishing step was done by means of a wet screening process. Multiple size distributions can be prepared in a single screening unit equipped with multiple screens.
  • the coarse test material was handled and stockpiled by means of machines which generated some fine material.
  • the coarse test material was also polished by means of a wet screening process to remove the -10 mm material.
  • test gasifier was operated manually according to a statistically designed test programme. Some of the most critical measurements, including gas liquor flow and CO 2 content of the raw gas, were verified with additional measurements. Reliable crude gas composition determinations were made through on-line analysers and frequent hand samples. This data was used for determining mass balances.
  • a load condition of approximately 10 kNm 3 /h to 13 kNm 3 /h oxygen was aimed for.
  • the CO 2 in raw gas concentrations aimed for were ⁇ 26 % and ⁇ 28 % CO 2 in the dry raw gas.
  • the test schedule which was executed for the reference tests is given in Table 1.
  • test schedule for the invention tests is given in Table 2.
  • the stone content of the 35x70 mm fraction also showed a much larger variation than the stone content of the 35x4 mm fraction and the previous reference tests.
  • the coarse fraction was not beneficiated or crushed down, but was used as is for gasification coal feed.
  • Figure 3 demonstrates the improved robustness of the gasifier when operated with a 35 x 4 mm coal particle size fraction compared to a typical broad particle fraction (70 x 4 mm) of the standard coal blend ( Figure 2).
  • Figure 3 depicts the feasible areas of operating regimes according to specific criteria for pure gas (PG) yield and the standard deviation (SD) of PG yield.
  • PG pure gas
  • SD standard deviation
  • the standard deviation indicates the variation in PG yield production due to gasifier instability. The smaller the standard deviation the more stable or robust PG yield is produced. The following are observed:
  • the invention tests were compared to the reference tests based on the predictions obtained with the statistical models. Predictions with the statistical models could not be performed for the 35x70 mm fraction since this size fraction was not included and tested in the historical tests. Weighted averages of PG yield and utility consumption were calculated for the combined 35x4 mm and 35x70 mm fraction tests and compared with the predictions for the reference tests (70x4 mm). When the particle size distribution of the standard feedstock was screened into the 35x4 mm and 35x70 mm fractions, it was found that 75% of the material reported to the 35x4 mm fraction and only 25% reported to the 35x70 mm fraction. Therefore, when the weighted average was calculated, the following formula was used:
  • a graph for the O 2 /pure gas ratios is shown in Figure 5.
  • the ratios for both the 35x4 mm and 35x70 mm coal fractions are within the normal scatter of the historical data.
  • the invention tests demonstrate that, surprisingly, significant higher oxygen consumption was not required for the coarse fraction (35x70 mm), as was expected.
  • Figure 6 indicates that the 35x70 mm fraction gave lower pure gas yields than the reference tests with the normal broad particle size distribution, and the yields for the 35x4 mm fraction is higher than the reference test values.
  • the stone content explains the higher ash content of the 35x70 mm coal fraction.
  • the 35x70 mm coal fraction is however much smaller than the 35x4 mm coal fraction, the capital cost of equipment provided only to beneficiate the larger fraction will be less than in conventional processes treating the total coal feed whilst providing a similar overall benefit.
  • the 35x70 mm fraction gave lower pure gas yields than the reference tests with the normal broad particle size distribution, and the yields for the 35x4 mm fraction are higher than the reference test values.

Abstract

L'invention concerne un procédé de gazéification d'une matière de charge particulaire carbonée. Ce procédé comporte les étapes consistant à : diviser la matière de charge en au moins deux fractions, chaque fraction comprenant une matière particulaire de classe granulométrique prédéterminée, de manière à obtenir au moins une matière de charge à dimensions inférieures de particules et une matière de charge à dimensions supérieures de particules. La matière de charge à dimensions inférieures est chargée dans au moins un gazogène, et la matière de charge à dimensions supérieures de particules est chargée dans au moins un autre gazogène.
PCT/IB2005/050830 2004-03-11 2005-03-07 Gazeification de matiere carbonee WO2005090526A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
CA002559191A CA2559191A1 (fr) 2004-03-11 2005-03-07 Gazeification de matiere carbonee
MXPA06010237A MXPA06010237A (es) 2004-03-11 2005-03-07 Gasificacion de material carbonoso.
US10/592,542 US20080034660A1 (en) 2004-03-11 2005-03-07 Gasification of Carbonaceous Material
AU2005223495A AU2005223495A1 (en) 2004-03-11 2005-03-07 Gasification of carbonaceous material

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ZA2004/1989 2004-03-11
ZA200401989 2004-03-11

Publications (1)

Publication Number Publication Date
WO2005090526A1 true WO2005090526A1 (fr) 2005-09-29

Family

ID=34960870

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2005/050830 WO2005090526A1 (fr) 2004-03-11 2005-03-07 Gazeification de matiere carbonee

Country Status (7)

Country Link
US (1) US20080034660A1 (fr)
CN (1) CN1930272A (fr)
AU (1) AU2005223495A1 (fr)
CA (1) CA2559191A1 (fr)
MX (1) MXPA06010237A (fr)
WO (1) WO2005090526A1 (fr)
ZA (1) ZA200607440B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101833283A (zh) * 2010-04-21 2010-09-15 武汉钢铁集团江南燃气热力有限责任公司 一种焦化物料平衡方法
CN105080377A (zh) * 2014-04-23 2015-11-25 中国石油化工股份有限公司 一种混配煤比例在线监控方法

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2472938C1 (ru) * 2011-07-28 2013-01-20 Государственное образовательное учреждение высшего профессионального образования "Кузбасский государственный технический университет" (ГУ КузГТУ) Способ предупреждения самовозгорания угля в шахтах
CN103160324B (zh) * 2013-03-29 2014-12-10 陕西煤业化工技术研究院有限责任公司 一种原煤多粒径分级热解气化一体化系统及方法
CN104726137B (zh) * 2015-03-04 2016-10-05 湖南谷力新能源科技股份有限公司 一种高利用率的生物质气化反应装置
CN115247083A (zh) * 2022-08-22 2022-10-28 安徽科达洁能股份有限公司 一种分级气化系统及方法

Citations (3)

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Publication number Priority date Publication date Assignee Title
WO1980000974A1 (fr) * 1978-10-30 1980-05-15 Kaiser Eng Inc Procede de gazeification du charbon
US4211540A (en) * 1978-12-29 1980-07-08 Fluor Corporation Process for the manufacture of fuel gas
GB2167431A (en) * 1984-11-22 1986-05-29 British Gas Corp Coal gasification process

Family Cites Families (4)

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Publication number Priority date Publication date Assignee Title
US4278447A (en) * 1979-11-16 1981-07-14 Conoco, Inc. Methods for producing feedstock for a fixed bed gasifier from finely-divided coal
DE3032949A1 (de) * 1980-09-02 1982-04-22 Metallgesellschaft Ag, 6000 Frankfurt Verfahren und vorrichtung zum aufgeben fester brennstoffe in die festbett-vergasung
DE3441757A1 (de) * 1984-11-15 1986-05-15 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum herstellen kohlehaltiger pellets fuer die vergasung
FI873735A0 (fi) * 1987-08-28 1987-08-28 Ahlstroem Oy Foerfarande och anordning foer foergasning av fast kolhaltigt material.

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1980000974A1 (fr) * 1978-10-30 1980-05-15 Kaiser Eng Inc Procede de gazeification du charbon
US4211540A (en) * 1978-12-29 1980-07-08 Fluor Corporation Process for the manufacture of fuel gas
GB2167431A (en) * 1984-11-22 1986-05-29 British Gas Corp Coal gasification process

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101833283A (zh) * 2010-04-21 2010-09-15 武汉钢铁集团江南燃气热力有限责任公司 一种焦化物料平衡方法
CN105080377A (zh) * 2014-04-23 2015-11-25 中国石油化工股份有限公司 一种混配煤比例在线监控方法

Also Published As

Publication number Publication date
AU2005223495A1 (en) 2005-09-29
CN1930272A (zh) 2007-03-14
US20080034660A1 (en) 2008-02-14
MXPA06010237A (es) 2007-04-23
ZA200607440B (en) 2008-06-25
CA2559191A1 (fr) 2005-09-29

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