EP0381254B1 - Process for obtaining synthesis gas either from solid fuels derived from urban solid waste, or from industrial solid waste - Google Patents

Process for obtaining synthesis gas either from solid fuels derived from urban solid waste, or from industrial solid waste Download PDF

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Publication number
EP0381254B1
EP0381254B1 EP90200063A EP90200063A EP0381254B1 EP 0381254 B1 EP0381254 B1 EP 0381254B1 EP 90200063 A EP90200063 A EP 90200063A EP 90200063 A EP90200063 A EP 90200063A EP 0381254 B1 EP0381254 B1 EP 0381254B1
Authority
EP
European Patent Office
Prior art keywords
solid waste
atm
abs
mpa
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.)
Revoked
Application number
EP90200063A
Other languages
German (de)
French (fr)
Other versions
EP0381254A1 (en
Inventor
Luigi Carvani
Giuliano Garuti
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.)
Eni Tecnologie SpA
Original Assignee
Eniricerche SpA
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Filing date
Publication date
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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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • C10J3/14—Continuous processes using gaseous heat-carriers
    • 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
    • C10J3/16—Continuous processes simultaneously reacting oxygen and water with the carbonaceous material
    • 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
    • C10J3/80—Other features with arrangements for preheating the blast or the water vapour
    • 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
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
    • C10K1/122—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing only carbonates, bicarbonates, hydroxides or oxides of alkali-metals (including Mg)
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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

Definitions

  • the present invention relates to a process for obtaining synthesis gas either from the solid fuels derived from urban solid waste, or from industrial solid waste.
  • the solid fuels derived from the urban solid waste are the lightest, combustible fraction of the urban solid waste, i.e., they are constituted by plastics, paper, wood, and textile materials (with the possible presence of organic matter). said fuels have a net heat value comprised within the range of from 10450 kJ/kg to 18850 kJ/kg (2,500 to 4,500 kcal/kg), according to the separation degree, as well as to their moisture content.
  • a general scheme of the process for producing said RDF comprises the following operations:
  • RDF The use of said RDF is for being burnt in boilers, and, above all, in cement factories.
  • the present Applicant has found now that said RDF or said solid industrial waste can be gasified under suitable conditions, in order to obtain synthesis gas.
  • the present invention therefore, provides a process for gassifying the combustible fraction of municipal- or industrial solid waste to produce synthesis gas by gassification with a pressurized oxygen-containing gas at a minimum temperature of 1000°C, characterized by comprising the steps of:
  • the exhausted tyres can be mentioned in particular; anyway, also other types of industrial waste can be selected.
  • the preferred range if of from 1,5 MPa to 5 MPa (15 to 50 abs.atm) in case RDF are used, and of from 0,1 MPa to 5 MPa (1 to 50 abs.atm) in case industrial solid waste is used.
  • the temperature of the gasifier is defined both as a function of the moisture content of RDF or of the industrial waste, and of their heat value, and as a function of the amount and of the temperature of the oxygen fed to the process.
  • Oxygen, before being fed to the gasifier, can be pre-heated at a temperature equal to, or higher than, the temperature-of the same gasifier.
  • Said oxygen can be produced, e.g., in an air fractionating facility, or in an equivalent facility.
  • a portion of the synthesis gas obtained (such as, e.g., about 10%), in order to have the necessary power for managing said air fractionating facility, or an equivalent facility, can be advantageous.
  • the treatment of the gas leaving the gasifier in order to remove the acidic gases can be carried out, e.g., by means of a washing step with sodium hydroxide.
  • cooling the gas leaving the gasifier before such a treatment is carried out can be advantageous.
  • a solid fuel derived from urban solid waste (RDF) was used, which had a net heat value of 16330 kJ/kg (3,900 kcal/kg), and contained 22.4% of moisture.
  • the gasification was carried out in a gasifier as adiabatic as possible, with 104 kg/hour of RDF and 48 kg/hour of essentially pure oxygen being co-currently fed to the process, under the following conditions:
  • 163 Nm3/hour of synthesis gas was obtained, which had a net heat value of 12430 kJ/Nm3 (2,969 kcal/Nm3), as referred to dry gas.
  • a stream of 17 Nm3/hour was diverted from the produced stream of 163 Nm3/hour of gas in order to generate the necessary electric power for operating the air fractionating facility.
  • the gasification was carried out in a gasifier as adiabatic as possible, with 102 kg/hour of exhausted tyres and 69 kg/hour of essentially pure oxygen being co-currently fed to the process, under the following conditions:
  • a stream of 25 Nm3/hour was diverted from the produced stream of 195 Nm3/hour of gas in order to generate the necessary electric power for the operations of the air fractionating facility.
  • a solid fuel deriving from urban solid waste (RDF) was used, which had a net heat value of 16540 kJ/kg (3,950 kcal/kg), and contained 7% of moisture.
  • the gasification was carried out in a gasifier as adiabatic as possible, with 127 kg/hour of RDF and 47 kg/hour of essentially pure oxygen being co-currently fed to the process, under the following conditions:
  • a stream of 19 Nm3/hour was diverted from the produced stream of 162 Nm3/hour of gas in order to generate the necessary electric power for operating the air fractionating facility.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

A process is disclosed, by means of which synthesis gas can be obtained either from solid fuels derived from urban solid waste (RDF), or from industrial solid waste, characterized in that said solid fuels (RDF) or said industrial solid waste are gasified with essentially pure oxygen under a pressure comprised within the range of from 1 to 100 abs.atm, by co-currently feeding said reactants to a gasifier as adiabatic as possible, and that the gas leaving the gasifier is treated in order to remove the polluting, acidic gases, by means of a washing step.

Description

  • The present invention relates to a process for obtaining synthesis gas either from the solid fuels derived from urban solid waste, or from industrial solid waste.
  • The solid fuels derived from the urban solid waste (commonly denominated as "RDF", or, in Italy, as "CsdR"), are the lightest, combustible fraction of the urban solid waste, i.e., they are constituted by plastics, paper, wood, and textile materials (with the possible presence of organic matter). said fuels have a net heat value comprised within the range of from 10450 kJ/kg to 18850 kJ/kg (2,500 to 4,500 kcal/kg), according to the separation degree, as well as to their moisture content.
  • A general scheme of the process for producing said RDF comprises the following operations:
    • trituration of the urban solid waste;
    • magnetic separation;
    • air sorting in order to separate the light fractions from the heavy fractions;
    • drying of the light material;
    • possible pelletizing of the resulting product.
  • Among the many factors of differentiation of RDF, besides the composition of the urban solid waste used as the starting material, there is the technology used in order to select the derived fuel.
  • The use of said RDF is for being burnt in boilers, and, above all, in cement factories.
  • The present Applicant has found now that said RDF or said solid industrial waste can be gasified under suitable conditions, in order to obtain synthesis gas. The present invention, therefore, provides a process for gassifying the combustible fraction of municipal- or industrial solid waste to produce synthesis gas by gassification with a pressurized oxygen-containing gas at a minimum temperature of 1000°C, characterized by comprising the steps of:
    • cocurrently feeding said combustible fraction and technically pure oxygen pressurized at a pressure of from 0,1 MPa to 10 Mpa (1 abs.atm to 100 abs.atm) to an adiabatic gassifier, and
    • washing the as-produced synthesis gas to remove the acidic gaseous components.
  • Both in case of RDF, and in case of industrial solid waste, it is recommended that they should have a net heat value of a least 12560 kJ/kg (3,000 kcal/kg), and a moisture content lower than, or at maximum equal to, 30%.
  • Among the industrial solid waste which an be used, the exhausted tyres can be mentioned in particular; anyway, also other types of industrial waste can be selected.
  • As regards the gasification pressure, the preferred range if of from 1,5 MPa to 5 MPa (15 to 50 abs.atm) in case RDF are used, and of from 0,1 MPa to 5 MPa (1 to 50 abs.atm) in case industrial solid waste is used.
  • The temperature of the gasifier is defined both as a function of the moisture content of RDF or of the industrial waste, and of their heat value, and as a function of the amount and of the temperature of the oxygen fed to the process.
  • Oxygen, before being fed to the gasifier, can be pre-heated at a temperature equal to, or higher than, the temperature-of the same gasifier.
  • Said oxygen can be produced, e.g., in an air fractionating facility, or in an equivalent facility.
  • In such case, using a portion of the synthesis gas obtained (such as, e.g., about 10%), in order to have the necessary power for managing said air fractionating facility, or an equivalent facility, can be advantageous.
  • The treatment of the gas leaving the gasifier in order to remove the acidic gases can be carried out, e.g., by means of a washing step with sodium hydroxide.
  • Furthermore, cooling the gas leaving the gasifier before such a treatment is carried out, can be advantageous.
  • Some examples are given now in order to better illustrate the invention without limiting it.
    • Example 1
  • A solid fuel derived from urban solid waste (RDF) was used, which had a net heat value of 16330 kJ/kg (3,900 kcal/kg), and contained 22.4% of moisture.
  • The gasification was carried out in a gasifier as adiabatic as possible, with 104 kg/hour of RDF and 48 kg/hour of essentially pure oxygen being co-currently fed to the process, under the following conditions:
    • P
    = 5 MPa (50 abs.atm);
    average T
    = 1,000°C
  • After the washing, 163 Nm³/hour of synthesis gas was obtained, which had a net heat value of 12430 kJ/Nm³ (2,969 kcal/Nm³), as referred to dry gas.
  • A stream of 17 Nm³/hour was diverted from the produced stream of 163 Nm³/hour of gas in order to generate the necessary electric power for operating the air fractionating facility.
    • Example 2
  • Exhausted tyres were used as the industrial solid waste, which had a net heat value of 25100 kJ/kg (6,000 kcal/kg) and showed an accidental moisture content of 15%.
  • The gasification was carried out in a gasifier as adiabatic as possible, with 102 kg/hour of exhausted tyres and 69 kg/hour of essentially pure oxygen being co-currently fed to the process, under the following conditions:
    • P
    = 0,1 MPa(1 abs.atm);
    average T
    = 1,200°C
  • After the washing, 195 Nm³/hour of synthesis gas was obtained, which had a net heat value of 11820 kJ/Nm³ (2,824 kcal/Nm³), as referred to dry gas.
  • A stream of 25 Nm³/hour was diverted from the produced stream of 195 Nm³/hour of gas in order to generate the necessary electric power for the operations of the air fractionating facility.
    • Example 3
  • A solid fuel deriving from urban solid waste (RDF) was used, which had a net heat value of 16540 kJ/kg (3,950 kcal/kg), and contained 7% of moisture.
  • The gasification was carried out in a gasifier as adiabatic as possible, with 127 kg/hour of RDF and 47 kg/hour of essentially pure oxygen being co-currently fed to the process, under the following conditions:
    • P
    = 1,5 MPa (15 abs.atm);
    average T
    = 1,220° C
  • After the washing, 162 Nm³/hour of synthesis gas was obtained, which had a net value of 10870 kJ/Nm³ (2,596 kcal/Nm³), as referred to dry gas.
  • A stream of 19 Nm³/hour was diverted from the produced stream of 162 Nm³/hour of gas in order to generate the necessary electric power for operating the air fractionating facility.

Claims (6)

  1. Process for gassifying the combustible fraction of municipal- or industrial solid waste to produce synthesis gas by gassification with a pressurized oxygen-containing gas at a minimum temperature of 1000°C, characterized by comprising the steps of:
    - cocurrently feeding said combustible fraction and technically pure oxygen pressurized at a pressure of from 0,1 MPa to 10 Mpa (1 abs.atm to 100 abs.atm) to an adiabatic gassifier, and
    - washing the as-produced synthesis gas to remove the acidic gaseous components.
  2. Process according to Claim 1, wherein the pressure of the technically pure oxygen is from 1,5 MPa to 5MPa (15 abs.atm to 50 abs.atm).
  3. Process according to Claim 1, wherein the combustible fraction of industrial solid waste is gassified under an oxygen pressure of from 0,1 MPa to 5 MPa (1 abs.atm to 50 abs.atm).
  4. Process according to Claim 1, wherein the oxygen feedstock is preheated at a minimum temperature equal to the temperature obtaining in the adiabatic gassifier.
  5. Process according to Claim 1, wherein said combustible fraction has a minimum net heating value of 12560 kJ/kg (3000 kcal/kg) and a maximum moisture content of 30% by weight.
  6. Process according to Claim 1, wherein the industrial waste solid combustible fraction derives from used tyres.
EP90200063A 1989-01-31 1990-01-10 Process for obtaining synthesis gas either from solid fuels derived from urban solid waste, or from industrial solid waste Revoked EP0381254B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT8919251A IT1229516B (en) 1989-01-31 1989-01-31 PROCEDURE FOR OBTAINING SYNTHESIS GAS FROM SOLID FUELS DERIVED FROM URBAN SOLID WASTE OR FROM INDUSTRIAL SOLID WASTE.
IT1925189 1989-01-31

Publications (2)

Publication Number Publication Date
EP0381254A1 EP0381254A1 (en) 1990-08-08
EP0381254B1 true EP0381254B1 (en) 1993-03-31

Family

ID=11156132

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90200063A Revoked EP0381254B1 (en) 1989-01-31 1990-01-10 Process for obtaining synthesis gas either from solid fuels derived from urban solid waste, or from industrial solid waste

Country Status (6)

Country Link
EP (1) EP0381254B1 (en)
AT (1) ATE87647T1 (en)
DE (1) DE69001181T2 (en)
DK (1) DK0381254T3 (en)
ES (1) ES2041113T3 (en)
IT (1) IT1229516B (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2150045C1 (en) * 1998-01-22 2000-05-27 Институт проблем химической физики РАН Method for recovery of combustible solid domestic wastes
DE19906891C2 (en) * 1999-02-19 2002-07-18 Schwarze Pumpe Energiewerke Ag Process for recycling dusty and sludge-like carbonaceous substances in fixed bed gasification

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR681147A (en) * 1928-02-11 1930-05-09 Process for the manufacture of gas mixtures, especially for the synthesis of methyl alcohol and the like
DE740734C (en) * 1941-04-25 1943-10-27 Koppers Gmbh Heinrich Process for the continuous generation of water gas
DE816284C (en) * 1949-03-29 1951-10-08 Vogogas S A Process for the gasification of non-bituminous solid fuels
DE2309248A1 (en) * 1973-02-24 1974-08-29 Koppers Gmbh Heinrich METHOD FOR GENERATING FUEL GAS
GB1555703A (en) * 1976-10-08 1979-11-14 Steag Ag Process for producing a gas rich in methane from waste materials

Also Published As

Publication number Publication date
IT8919251A0 (en) 1989-01-31
EP0381254A1 (en) 1990-08-08
DE69001181D1 (en) 1993-05-06
ES2041113T3 (en) 1993-11-01
DK0381254T3 (en) 1993-08-02
DE69001181T2 (en) 1993-08-05
IT1229516B (en) 1991-09-03
ATE87647T1 (en) 1993-04-15

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