[go: up one dir, main page]

WO2012014277A1 - Procédé de production d'un gaz contenant de l'hydrogène - Google Patents

Procédé de production d'un gaz contenant de l'hydrogène Download PDF

Info

Publication number
WO2012014277A1
WO2012014277A1 PCT/JP2010/062592 JP2010062592W WO2012014277A1 WO 2012014277 A1 WO2012014277 A1 WO 2012014277A1 JP 2010062592 W JP2010062592 W JP 2010062592W WO 2012014277 A1 WO2012014277 A1 WO 2012014277A1
Authority
WO
WIPO (PCT)
Prior art keywords
hydrogen
sludge
producing
containing gas
organic sludge
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.)
Ceased
Application number
PCT/JP2010/062592
Other languages
English (en)
Japanese (ja)
Inventor
堂脇　直城
堂脇　清志
亀山　光男
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.)
JAPAN PLANNING ORGANIZATION Inc
Original Assignee
JAPAN PLANNING ORGANIZATION Inc
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 JAPAN PLANNING ORGANIZATION Inc filed Critical JAPAN PLANNING ORGANIZATION Inc
Priority to PCT/JP2010/062592 priority Critical patent/WO2012014277A1/fr
Priority to JP2011529797A priority patent/JP5385396B2/ja
Publication of WO2012014277A1 publication Critical patent/WO2012014277A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0405—Purification by membrane separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • the present invention relates to a method for producing a hydrogen-containing gas, and more particularly to a method for producing a hydrogen-containing gas from organic sludge.
  • Non-Patent Document 1 the amount of sludge generated is 193,159,000 dry-t / year in 1996 (partially, 1998 for the manufacturing industry). Among them, the generated amount of organic sludge is 126,9110,000 dry-t / year, while the generated amount of inorganic sludge is 66,249,000 dry-t / year. Thus, the amount of organic sludge generated is very large. Among such organic sludges, the most generated amount is sewer related organic sludge, and the generated amount is 76,527,000 dry-t / year.
  • the second is organic sludge related to pulp and paper, the amount generated is 24,256,000 dry-t / year, the third is organic sludge related to food and beverages, the amount generated is 13,033 000 dry-t / year, the fourth was chemical-related organic sludge, and the amount generated was 4,626,000 dry-t / year.
  • organic sludge related to sewerage hereinafter sometimes referred to as “sewage sludge”
  • sewage sludge organic sludge related to sewerage
  • organic sludge for example, sewage sludge
  • N 2 O in addition to CO 2 during incineration because its components contain a large amount of nitrogen.
  • the global warming potential which is an index of greenhouse gases, is as follows.
  • CO 2 is 1 (standard)
  • N 2 O reaches 310, indicating a greenhouse effect 310 times that of CO 2 . Therefore, as a measure against global warming, it is necessary to suppress the generation of CO 2 and at the same time suppress the generation of N 2 O in the treatment of sewage sludge.
  • Patent Document 1 discloses that organic resources (biomass, garbage, sewage sludge, etc.), coal, etc. are used as hydrocarbon-based solid fuel and are extracted as combustible gas.
  • the alkali and / or alkaline earth metal evaporated during the thermal decomposition of the metal is actively adsorbed to the char in the alkali absorption furnace, and the alkali and / or alkaline earth metal is effectively used as a char gasification catalyst.
  • Sewage sludge contains about 10 to 30% by weight of ash depending on daily, weekly and seasonal variations.
  • alkali and / or alkaline earth metal in ash can be effectively utilized as a gasification catalyst, and it can be expected to obtain a combustible gas with a high yield.
  • Patent Document 1 there is no description of drying before introducing an organic resource such as sewage sludge into an alkali absorption furnace, and of course, there is no description regarding a drying method of the organic resource.
  • the organic resources and the like are introduced into the alkali absorption furnace without being specifically dried.
  • Patent Document 2 sewage sludge gasification method and apparatus for gasifying sewage sludge and using the generated gas for power generation by a gas engine or a gas turbine, waste such as waste plastic or biomass, coal, etc. Fuel is bubbled together with bed material such as sand with fluidizing air and burned, and in a state where a fluidized bed is formed, sewage sludge containing about 70 to 80% by weight of water is dropped on the fluidized bed as it is.
  • bed material such as sand with fluidizing air and burned
  • sewage sludge containing about 70 to 80% by weight of water is dropped on the fluidized bed as it is.
  • a method for simultaneously drying sewage sludge and generating volatile matter is disclosed. According to this method, waste such as waste plastic or biomass, or CO 2 generated by combustion of coal or the like, and H 2 O generated by drying of sewage sludge react with volatile matter generated from sewage sludge.
  • the method uses waste plastics or waste such as biomass, or auxiliary fuel such as coal, so there is concern about a decrease in thermal efficiency, and since these auxiliary fuels are used, the effect of reducing greenhouse gases is expected. Can not.
  • the sewage sludge is directly gasified on the fluidized bed without drying.
  • Patent Document 3 in a gasification method for efficiently gasifying biological sludge, biological sludge is solubilized by a solubilizing device using a cavitation treatment method or the like, and then dehydrated using a dehydrating device.
  • the obtained gas is used for power generation in a generator such as a gas engine.
  • a generator such as a gas engine.
  • Patent Document 4 includes a dryer for heating and drying sewage sludge, a fluidized bed type pyrolysis furnace for pyrolyzing sewage sludge dried by the dryer in a fluidized bed to generate pyrolysis gas, and Heat of sewage sludge comprising a combustion furnace for burning pyrolysis gas, a boiler for generating steam by the combustion energy of the pyrolysis gas in the combustion furnace, and a steam turbine generator for generating electric power by the steam generated by the boiler A cracked gasification power generation system is disclosed. According to this method, by efficiently decomposing and gasifying the sewage sludge, the retained energy of the sewage sludge can be recovered as electric power with high efficiency, and part of the exhaust heat of the steam turbine generator can be recovered.
  • sewage sludge can be efficiently dried.
  • the moisture content of the dried sewage sludge is relatively high at 30-50% by weight.
  • this method is achieved by coupling with a steam turbine generator, there is a drawback that its application is limited.
  • an apparatus for drying organic sludge an apparatus that simultaneously performs drying and gasification on a fluidized bed such as sand, as shown in Patent Document 2, and a high-pressure filter press as shown in Patent Document 3.
  • Mechanical dehydrators, and indirect heating dryers such as a stirring rotation type and a steam heating multi-tube rotation type as described in Patent Document 4, for example, a cylindrical stirring dryer, a steam heating tube rotation drying And direct heating dryers such as fluidized bed, multi-stage disc type, vibrating box type, for example, air dryer, rotary dryer, aeration dryer, band dryer, etc. Yes.
  • the fluidized bed direct heating dryer usually uses a powder having a small particle diameter, such as sand, as a bed material.
  • organic waste such as thinned wood, driftwood, waste wood, waste plastic, garbage, Sludge, mowing grass, paper sludge, etc. are heated at 500-600 ° C in a non-oxidizing atmosphere, the generated pyrolysis gas is mixed with steam at 900-1,000 ° C, and then the resulting reformed gas is purified.
  • a method for recovering hydrogen is known. According to this method, hydrogen can be recovered with high energy efficiency without generating unnecessary carbon dioxide from organic waste.
  • the present invention provides a method for producing a hydrogen-containing gas from organic sludge, which has high thermal efficiency and low cost, and has very little greenhouse gas emissions.
  • the present inventors use the method described in Patent Document 5 described above, which has extremely good energy efficiency and does not generate unnecessary carbon dioxide. Thought.
  • the water content of the organic sludge as a raw material needs to be 50% by weight or less, preferably 30% by weight or less. Further, thermal decomposition can be facilitated and high efficiency can be achieved.
  • Organic sludge with a high water content particularly sewage sludge with a water content of about 70 to 90% by weight, is usually in the form of a paste. It is necessary to dry at a relatively high temperature exceeding ° C. At a low temperature of 200 ° C.
  • the present inventors have found that the water content of organic sludge can be significantly reduced to 20% by weight or less, particularly 15% by weight or less, in a relatively short time and efficiently, and the present invention has been completed. Preferably, it has been found that even better results can be obtained by relatively increasing the maximum diameter of the following predetermined lump.
  • the present invention (1) Drying organic sludge, then pyrolyzing the resulting dried organic sludge, and reforming the generated pyrolysis gas with steam.
  • a metal block and / or a ceramic block at a temperature of 100 to 200 ° C. by hot air obtained using exhaust heat generated in accordance with the method for producing the hydrogen-containing gas.
  • a method for producing a hydrogen-containing gas which is carried out while crushing organic sludge.
  • (2) The method for producing a hydrogen-containing gas according to the above (1), wherein 95% or more of the total number of metal blocks and / or ceramic blocks has a maximum diameter of 11 to 20 mm
  • (3) The method for producing a hydrogen-containing gas according to (1) above, wherein 95% or more of the total number of metal blocks and / or ceramic blocks has a maximum diameter of 12 to 16 mm
  • (4) The method for producing a hydrogen-containing gas according to the above (1), wherein 98% or more of the total number of metal blocks and / or ceramic blocks has a maximum diameter of 11 to 20 mm
  • (5) The method for producing a hydrogen-containing gas according to the above (1), wherein 98% or more of the total number of metal blocks and / or ceramic blocks has a maximum diameter of 12 to 16 mm
  • (6) Any of the above (1) to (5), wherein the drying and crushing of the organic sludge is performed while moving the metal lump and / or ceramic lump in an arbitrary direction by the hot air.
  • a method for producing a hydrogen-containing gas according to any one of the above, (7) The method for producing a hydrogen-containing gas according to any one of (1) to (6) above, wherein the drying temperature of the organic sludge is 140 to 160 ° C.
  • Exhaust heat generated with the implementation of the method for producing hydrogen-containing gas was obtained from hot air obtained by burning tar and pyrolysis residue generated when pyrolyzing dried organic sludge.
  • the material of the metal block is one or more selected from the group consisting of iron, stainless steel, nickel alloy steel and titanium alloy steel, according to any one of (1) to (8) above.
  • a method for producing a hydrogen-containing gas (10)
  • the material for the ceramic mass is one or more selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, and silicon nitride, as described in any one of (1) to (9) above.
  • a method for producing a hydrogen-containing gas, (11) The metal lump and / or the ceramic lump is a ceramic lump, and the material of the ceramic lump is alumina, as described in any one of (1) to (10) above.
  • a method for producing a hydrogen-containing gas of (12) The method for producing a hydrogen-containing gas according to any one of (1) to (11) above, wherein the shapes of the metal mass and the ceramic mass are balls.
  • Organic sludge is selected from the group consisting of livestock waste, compost, sewage sludge, human waste sludge, activated sludge, pulp waste liquid sludge, animal and plant residues, billpit sludge, household waste and food waste.
  • a method of thermally decomposing dried organic sludge and reforming the generated pyrolysis gas with steam is generated by heating the dried organic sludge at 400 to 700 ° C. in a non-oxidizing atmosphere.
  • a method of thermally decomposing dried organic sludge and reforming the generated pyrolysis gas with steam was generated by heating the dried organic sludge at 500 to 600 ° C. in a non-oxidizing atmosphere.
  • the heat source of the hot air used for drying the organic sludge is so-called process exhaust heat
  • the thermal efficiency of the entire process is high, and the organic sludge can be dried at a low cost.
  • fuel from the outside of the process such as waste plastic, coal, heavy oil, etc.
  • the organic sludge is dried while being crushed in the presence of the metal lump and / or ceramic lump, the organic sludge can be efficiently and sufficiently dried in a short time.
  • gasification is performed using sufficiently dried organic sludge as a raw material, a hydrogen-containing gas can be produced with a high yield.
  • FIG. 1 is a diagram showing an outline of a drying apparatus used in Examples 1 to 10 and Comparative Examples 1 and 2.
  • FIG. 2 is a diagram showing an outline of the hydrogen-containing gas production apparatus used in Example 11.
  • organic sludge as a raw material is dried.
  • hot air obtained using exhaust heat generated in accordance with the implementation of the method for producing a hydrogen-containing gas of the present invention is used.
  • the upper limit of the temperature of the hot air is 200 ° C, preferably 160 ° C, and the lower limit is 100 ° C, preferably 140 ° C.
  • Exceeding the above upper limit is effective for drying organic sludge, but at the same time, the organic sludge is thermally decomposed, in particular, oxidatively decomposed, resulting in unnecessary carbon dioxide and pyrolysis residues, etc. Since organic sludge that has been decomposed is used, the efficiency of hydrogen-containing gas production is significantly reduced. In addition, it is necessary to make the dryer material expensive. If it is less than the said lower limit, drying of organic sludge requires a remarkably long time, and is not preferable.
  • the exhaust heat generated with the implementation of the method for producing a hydrogen-containing gas of the present invention is not particularly limited as long as it is exhaust heat obtained from the method of the present invention.
  • the exhaust heat preferably, tar and pyrolysis residue generated when pyrolyzing organic sludge, that is, exhaust gas after heat exchange in the process of high-temperature exhaust gas generated by burning char Sensible heat can be used. Tar and pyrolysis residue generated by pyrolysis of organic sludge are burned together with combustion air in a high-temperature hot air generator, and the high-temperature hot air generated thereby is used to pyrolyze organic sludge.
  • heat exchange is performed.
  • the hot air (exhaust gas) having a temperature of 100 to 200 ° C. after the heat exchange in this way is used for drying the organic sludge.
  • the exhaust gas itself is introduced directly into the organic sludge dryer. In this way, it is possible to effectively use hot air that is inherently low in temperature and exhausted in large quantities as exhaust gas.
  • high-temperature exhaust gas generated from the generator can also be used.
  • the drying of the organic sludge in the present invention is carried out while crushing the organic sludge in the presence of a metal lump and / or a ceramic lump.
  • the maximum diameter of the metal agglomerates and / or ceramic agglomerates is preferably 95% or more of the total number of these agglomerates 11 to 20 mm, more preferably 95% or more of the total number of these agglomerates. Is 12 to 16 mm, more preferably, 98% or more of the total number of these lumps is 11 to 20 mm, and particularly preferably 98% or more of the total number of these lumps is 12 to 16 mm.
  • the maximum diameter of the lump is less than the above lower limit, the effect of pulverizing the organic sludge and exposing it to the inside is poor, and the organic sludge cannot be sufficiently dried in a short time. Moreover, there is a possibility that the lump may be taken into the organic sludge. On the other hand, if the above upper limit is exceeded, in order to move the lump in an arbitrary direction inside the dryer, for example, to make a vertical motion, a vibration motion, etc. Absent. Moreover, it becomes easy for a lump to rest at a dryer bottom part, and the possibility of solidifying with organic sludge arises.
  • the maximum diameter means, for example, the diameter of a true spherical block, and the maximum diameter of the oval or ellipse if the cross section is an oval spherical block or an elliptical cross section.
  • the diameter for example, the length of the diagonal line in the case of a cube or a rectangular parallelepiped.
  • the amount of the metal agglomerate and / or ceramic agglomerate depends on the volume of the dryer and the shape of the bottom of the dryer, but is not particularly limited as long as it can dry and crush organic sludge. Absent. Usually, it is preferably 0.5 to 5.0% by weight, more preferably 0.5 to 3.0% by weight, still more preferably 0.5 to 1% with respect to the organic sludge input weight to the dryer assumed in advance. .5% by weight.
  • the organic sludge input weight to the dryer assumed beforehand is determined, for example, in consideration of the amount of treatment in the thermal decomposition step of the subsequent step.
  • the amount is preferably about 1 to 5 layers, more preferably about 1 to 3 layers on the bottom of the dryer. Too much metal agglomerate and / or ceramic agglomerate is not economical because it requires a significant amount of hot air to move the agglomerate in any direction within the dryer, and In addition, the lump is likely to be stationary inside the dryer, and the effect of crushing organic sludge is reduced. On the other hand, even if there is too little quantity of a metal lump and / or ceramic lump, the effect which crushes organic sludge falls.
  • the amount of hot air varies depending on the maximum diameter, shape, and material of these lumps and the amount of water in the organic sludge.
  • the amount of hot air is preferably 3 to 10 m 3 , more preferably 4 to 8 m 3 with respect to 1 kg of organic sludge. If the upper limit is exceeded, the efficiency decreases due to the use of a large amount of hot air, and if it is less than the lower limit, drying of the organic sludge becomes insufficient.
  • the material of the metal block is at least one selected from the group consisting of iron, stainless steel, nickel alloy steel and titanium alloy steel.
  • the material of the ceramic mass is at least one selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, and silicon nitride. Of these materials, alumina is preferred.
  • Examples of the shape of the metal agglomerate and the ceramic agglomerate include a spherical agglomerate, a spherical agglomerate having an elliptical cross section, a ball agglomerate such as a spherical agglomerate having an elliptical cross section, a conical agglomerate, a triangle
  • Examples thereof include a polygonal pyramidal mass such as a pyramid and a quadrangular pyramid, a cylindrical mass, a polygonal columnar mass such as a triangular prism and a quadrangular prism, and a pulverized product.
  • a ball-like lump such as a true spherical lump, a spherical lump having an oval cross section, and a spherical lump having an elliptical cross section is preferable. used.
  • the organic sludge is preferably selected from the group consisting of livestock waste, compost, sewage sludge, human waste sludge, activated sludge, pulp waste liquid sludge, animal and plant residues, billpit sludge, household waste, and food waste.
  • sewage sludge is preferably used.
  • these organic sludges Prior to drying in the present invention, these organic sludges are, for example, compression dehydrators such as belt press dehydrators and filter press dehydrators, centrifugal dehydrators, filtration dehydrators, sedimentation types Preliminary dehydration with a dehydrator or the like is preferred.
  • the water content of the organic sludge after preliminary dehydration is preferably 95% by weight or less, more preferably 80% by weight or less, and still more preferably 50% by weight or less.
  • the shape of the organic sludge after the preliminary dehydration is paste, paste, cake, flake, etc., but there is no problem in supplying it to the dehydration of the present invention. .
  • the above organic sludge preferably pre-dehydrated organic sludge, is exposed to hot air obtained using exhaust heat generated in accordance with the method for producing a hydrogen-containing gas of the present invention in a dryer.
  • the metal lump and / or the ceramic lump is crushed and dried.
  • the hot air blows the metal lump and / or ceramic lump in any direction inside the dryer, for example, up and down movement, vibration movement, etc., paste, paste, cake, flake, etc. It collides with the organic sludge and is dried while cutting, pulverizing, etc. these organic sludge. In this way, the organic sludge is dried so that the water content is preferably 20% by weight or less, more preferably 15% by weight or less.
  • the dried organic sludge dehydrated in this way is then thermally decomposed.
  • Pyrolysis is preferably performed by heating in a non-oxidizing atmosphere. By the heating, the dried organic sludge undergoes thermal decomposition and generates thermal decomposition gas.
  • the upper limit of the heating temperature is 700 ° C, preferably 600 ° C, more preferably 570 ° C, and the lower limit is 400 ° C, preferably 500 ° C, more preferably 530 ° C.
  • the amount of gas generated can be increased.
  • the lower limit the dried organic sludge is not sufficiently thermally decomposed. If the upper limit is exceeded, the amount of gas generated cannot be increased.
  • the upper limit of the pressure during the heating is preferably 1 MPa, more preferably 0.3 MPa, and the lower limit is preferably 0.1 MPa, more preferably 0.103 MPa.
  • Nitrogen is preferably used as the non-oxidizing atmosphere.
  • the type and type of the heating furnace used are not particularly limited. Any material may be used as long as it has a performance capable of heating the dried organic sludge as a raw material to the above temperature. Examples thereof include a retort furnace, a shaft furnace, a rotary kiln, a fixed bed furnace, a moving bed furnace, and a fluidized bed furnace. For example, alumina, silica, sand or the like can be used as the material for the circulating medium in the moving bed furnace and fluidized bed furnace, and the shape is not particularly limited.
  • the generated pyrolysis gas is mixed with steam.
  • the pyrolysis gas and steam react to reform the pyrolysis gas into a gas rich in hydrogen.
  • the upper limit of the temperature at which the pyrolysis gas is mixed with steam is 1000 ° C., and the lower limit is 700 ° C., preferably 900 ° C., more preferably 950 ° C. If it is less than the lower limit, the reforming reaction does not proceed, and if the upper limit is exceeded, the material of the reforming furnace is adversely affected.
  • the heat for proceeding with the reforming reaction is supplied by a heated heat medium.
  • a heat source for the heat medium heat obtained by combustion treatment of tar and char (carbon and ash) generated when the dried organic sludge is heated in a non-oxidizing atmosphere is used.
  • the combustion treatment is preferably carried out by installing a system different from the system for heating the dried organic sludge in a non-oxidizing atmosphere, for example, a separate hot air generator.
  • tar often interferes with the continuous operation of the furnace when the dried organic sludge is heated in a non-oxidizing atmosphere. Therefore, it is preferable that tar be appropriately discharged from the bottom of the furnace. Thereby, it becomes possible to carry out continuous operation smoothly. Further, if tar and char generated as a by-product are extracted and burned in another system, the by-product tar and char can be effectively utilized in addition to avoiding troubles in the apparatus and maintaining safe operation.
  • Steam for reforming the pyrolysis gas is obtained from industrial water or clean water through a heat exchanger using the heat of the high-temperature reformed gas exiting from the reforming furnace. Alternatively, steam may be obtained by installing a separate boiler.
  • the temperature for supplying the steam is preferably 140 ° C. or higher, and the pressure is preferably 0.376 MPa or higher. Although not limited, the temperature and pressure are, for example, 180 ° C. and 1 MPa.
  • the reforming furnace can be supplied by spraying continuously or intermittently.
  • the type and type of the reforming furnace to be used are not particularly limited. Examples thereof include a retort furnace, a shaft furnace, a rotary kiln, a fixed bed furnace, a moving bed furnace, and a fluidized bed furnace. Usually, the same type as the above heating furnace is used, but it is not limited thereto, for example, a combination of using a rotary kiln as a heating furnace and using a retort furnace as a reforming furnace. Good.
  • alumina, silica, sand or the like can be used as the material for the circulating medium in the moving bed furnace and fluidized bed furnace, and the shape is not particularly limited.
  • the reformed gas exiting the reforming furnace can be preferably passed through the shift reaction layer.
  • the shift reaction is known.
  • a two-stage process is used. In the first stage, an iron-chromium high temperature conversion catalyst is used, and the reaction is preferably performed at 350 to 500 ° C., and the residual carbon monoxide concentration in the gas is set to about 3 to 4% by volume.
  • a copper-zinc based low temperature conversion catalyst is used, preferably reacted at 200 to 250 ° C., so that the residual carbon monoxide concentration in the gas is about 0.3 to 0.4% by volume. Is done.
  • the pressure during the reaction is preferably 1 MPa or more, more preferably 1 to 3 MPa. The pressure can be usually determined in accordance with the pressure of the process before and after the shift reaction layer.
  • the reformed gas obtained as described above is preferably cooled with water, and then the gas is purified to concentrate hydrogen to recover hydrogen.
  • a known method can be used.
  • PSA pressure swing adsorption method
  • a membrane separation method e.g., a membrane separation method
  • a cryogenic separation method e.g., a cryogenic separation method.
  • PSA is suitable because the gas concentration can be freely adjusted and is inexpensive.
  • the concentration of hydrogen to be recovered can be appropriately controlled by changing the adsorption time, the height of the adsorption layer, and the like. In this way, the reformed gas obtained as described above is separated into hydrogen and other gases to recover hydrogen.
  • the high-temperature exhaust gas generated from the generator can also be used for drying organic sludge.
  • Example 2 The raw materials and gasifiers used in the examples are as follows.
  • the properties of each sewage sludge are measured according to the following method.
  • ash, volatile matter and fixed carbon are values calculated on a dry basis. Further, the moisture is that when the raw material is received.
  • ⁇ Gasifier> As the gasifier, the one shown in FIG. 1 was used. The internal volume of the drying zone at the bottom of the dryer (D) in the gasifier was 0.2 m 3 .
  • the pyrolyzer (A) and the reformer (B) were both retort furnaces having a mortar bottom, and their internal volumes were both 0.5 m 3 .
  • Example 1 M city sewage sludge was used as a raw material. Moreover, the drying test of the sewage sludge was implemented as an apparatus using the drying apparatus shown in FIG.
  • the drying device is a cylindrical container having a diameter of 500 mm and a length of 500 mm, and has a structure in which hot air is blown from the side thereof.
  • alumina balls having a diameter of 12 mm were used as a lump used for crushing sewage sludge. The alumina balls were charged into an about 0.5 kg dryer.
  • sewage sludge was fed to the dryer (D) at a rate of 14.6 kg / hr by a feeder. At the same time, 140 ° C. hot air was supplied to the dryer (D) in an amount of 70 m 3 / hr from the line (7). The residence time of the sewage sludge in the dryer (D) was about 5 minutes.
  • the dried substance discharged from the dryer (D) was introduced into the cyclone (E). Here, the dried sewage sludge and the gas were separated, and the dried sewage sludge was taken out from the line (2) in an amount of 3.4 kg / hr.
  • the water content and volatile content of the dried sewage sludge were measured [JIS-M8812 (1993)].
  • the obtained dried sewage sludge had a water content of 12.9% by weight and a volatile content of 62.0% by weight.
  • Example 2 (Examples 2 to 5) Instead of the alumina balls having a diameter of 12 mm, the same amount of alumina balls having a diameter of 16 mm was charged in the dryer (D) as in Example 1, and the supply amount of the sewage sludge to the dryer (D), respectively. , 15.1 kg / hr, 13.7 kg / hr, 13.2 kg / hr, and 14.4 kg / hr. Dried sewage sludge was obtained at 3.5 kg / hr, 3.2 kg / hr, 3.1 kg / hr and 3.3 kg / hr, respectively. The water content of the obtained dried sewage sludge was 13.3% by weight, and the volatile content was 62.0% by weight.
  • Example 6 The test was carried out in the same manner as in Example 1 except that the temperature of the hot air supplied from the line (7) was 200 ° C.
  • the obtained dried sewage sludge had a moisture content of 10.0% by weight and a volatile content of 60.0% by weight.
  • Example 7 The same operation as in Example 1 was performed except that the temperature of the hot air supplied from the line (7) was 170 ° C.
  • the obtained dried sewage sludge had a water content of 10.4% by weight and a volatile content of 62.0% by weight.
  • Example 8 Instead of alumina balls having a diameter of 12 mm, using alumina balls having a diameter of 10 mm, the same amount as in Example 1 was charged into the dryer (D), and the amount of sewage sludge supplied to the dryer (D) was The same operation as in Example 1 was carried out except that 15.1 kg / hr (same as in Example 2) was used. A dried sewage sludge was obtained at 3.0 kg / hr. The water content of the obtained dried sewage sludge was 13.3% by weight.
  • Example 9 Instead of alumina balls having a diameter of 12 mm, using alumina balls having a diameter of 10 mm, the same amount as in Example 1 was charged into the dryer (D), and the amount of sewage sludge supplied to the dryer (D) was The same operation as in Example 1 was carried out except that 13.7 kg / hr (same as Example 3). 2.8 kg / hr of dried sewage sludge was obtained. The water content of the obtained dried sewage sludge was 13.3% by weight. As in Example 8, some sewage sludge adhered to the inner wall of the dryer and formed a lump with alumina balls, and the recovery rate of the dried sewage sludge was reduced compared to Example 1. Moreover, the volatile matter of the obtained sewage sludge dried material was 62.0 weight%.
  • Example 10 Instead of the alumina balls having a diameter of 12 mm, using the alumina balls having a diameter of 20 mm, the same amount as in Example 1 was charged into the dryer (D), and the amount of sewage sludge supplied to the dryer (D) was The same operation as in Example 1 was carried out except that 15.1 kg / hr (same as in Example 2) was used. 3.1 kg / hr of dried sewage sludge was obtained. The water content of the obtained dried sewage sludge was 13.3% by weight.
  • Example 1 Example except that the alumina ball was not inserted into the dryer (D) and the supply amount of the sewage sludge to the dryer (D) was 14.4 kg / hr (same as in Example 5). This was carried out in the same manner as 1. A dried sewage sludge was obtained at 4.4 kg / hr. The resulting dried sewage sludge had a moisture content of 31.5% by weight and a volatile content of 62.0% by weight.
  • Example 2 The same operation as in Example 1 was performed except that the temperature of the hot air supplied from the line (7) was 250 ° C. A dried sewage sludge was obtained at 3.0 kg / hr. The water content of the obtained dried sewage sludge was 10.0% by weight. The volatile content of the dried product was as low as 54.5% by weight.
  • Table 1 shows the results of Examples 1 to 10 and Comparative Examples 1 and 2.
  • Example 1 M city sewage sludge was dried using an alumina ball having a drying temperature of 140 ° C. and a diameter of 12 mm. The moisture content before drying was reduced to 72.9% by weight, indicating that the sewage sludge was successfully dried.
  • the diameter of the alumina ball is 16 mm.
  • the water content of the sewage sludge after drying was 13.3% by weight, indicating that good drying was performed.
  • the drying temperature was increased to 200 ° C. within the scope of the present invention.
  • the water content of the sewage sludge after drying was 10.0% by weight, and the drying was further improved.
  • the volatile content of the sewage sludge after drying was somewhat low at 60.0% by weight.
  • Example 7 the drying temperature was set to 170 ° C.
  • the water content of the sewage sludge after drying was 10.4% by weight, and the volatile content of the sewage sludge after drying was 62.0% by weight, even though the drying was even better than Example 1. This was not different from Example 1.
  • the diameter of the alumina ball is 10 mm, which is smaller than that in Example 1.
  • the water content of the sewage sludge after drying was 13.3% by weight, which was slightly higher than that of Example 1, but showed good results.
  • the diameter of the alumina ball is 20 mm.
  • the water content of the sewage sludge after drying was 13.3% by weight, and good results were obtained.
  • Comparative Example 1 did not use alumina balls.
  • the water content of the collected sewage sludge was extremely high at 31.5% by weight.
  • the drying temperature was raised to 250 ° C., which is outside the scope of the present invention. Although drying was performed well, the volatile content of the sewage sludge after drying was significantly reduced to 54.5% by weight. Thus, it has been found that when the drying temperature is increased, even a gas that can be recovered as a pyrolysis gas in the subsequent process is discharged as an exhaust gas.
  • Example 11 As a raw material, A city sewage sludge was used. Moreover, as an apparatus, the apparatus shown in FIG. 2 was used, Dry sewage sludge, Thermal decomposition of the dried sewage sludge, and modification
  • sewage sludge was fed to the dryer (D) at a rate of 87.6 kg / hr by a feeder.
  • hot air at 170 ° C. was supplied from the line (7) to the dryer (D) in an amount of 500 m 3 / hr.
  • the residence time of the sewage sludge in the dryer (D) was 5 minutes.
  • the dried substance discharged from the dryer (D) was introduced into the cyclone (E).
  • the dried sewage sludge and the gas were separated, and the dried sewage sludge was taken out from the line (2) in an amount of 30.0 kg / hr.
  • the dried sewage sludge was appropriately collected from the line (2) and measured for moisture and volatile content [JIS-M8812 (1993)].
  • the resulting dried sewage sludge was 12.9% by weight, Volatiles were 41.0% by weight.
  • the obtained dried sewage sludge was continuously introduced into a thermal cracker (A) maintained at a temperature of 550 ° C. and a pressure of 0.103 MPa by a feeder.
  • the apparent residence time of the dried sewage sludge in the pyrolyzer (A) was about 1 hour.
  • Gas generated by pyrolysis was obtained from the top of the pyrolyzer (A) in an amount of 14.7 kg / hr.
  • the gas was subsequently introduced into the reformer (B) maintained at a temperature of 950 ° C. and a pressure of 0.103 MPa.
  • superheated steam 180 ° C., 1 MPa was introduced into the reformer (B) in an amount of 20.0 kg / hr from the line (3) for gas reforming.
  • a modified gas at 950 ° C. was obtained in an amount of 34.7 kg / hr.
  • the gas was then cooled to 40 ° C. by contacting with water in a gas cooling device (C).
  • the composition of the gas is as shown in Table 2.
  • the 170 ° C. hot air supplied from the line (7) to the dryer (D) used in this example was obtained as follows. Tar and pyrolysis residue (char) taken out from the bottom of the pyrolyzer (A) via the line (5) were charged into a high-temperature hot air generator (F). In the high-temperature hot air generator (F), the tar and the pyrolysis residue were burned together with the combustion air. The high-temperature hot air of about 1,200 ° C. generated thereby is sent to the heat exchanger 1 (G1) for heat exchange, and a heat source for thermally decomposing organic sludge in the pyrolyzer (A), and Used as a heat source for reforming the pyrolysis gas in the reformer (B).
  • the hot air of about 534 ° C. exiting the heat exchanger 1 (G1) is further sent to the heat exchanger 2 (G2) to exchange heat with air, and the obtained hot air is converted into a high-temperature hot air generator ( Used as combustion air for use in F). And the hot air of 170 degreeC which came out of the heat exchanger 2 (G2) was supplied to the dryer (D) through the line (7). Further, in FIG. 2, white arrows indicate the flow of exhaust heat.
  • organic sludge discharged in the environmental treatment industry, paper industry, food industry, chemical industry, livestock industry, etc. can be used effectively.
  • hydrogen gas can be efficiently produced, so that it is not limited to simple treatment of organic sludge, hydrogen production business using organic sludge, fuel cell industry, power generation business, etc. It is also possible to effectively use the method of the present invention.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Materials Engineering (AREA)
  • Treatment Of Sludge (AREA)
  • Drying Of Solid Materials (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Coke Industry (AREA)

Abstract

La présente invention porte sur un procédé de production à partir d'une boue organique d'un gaz contenant de l'hydrogène qui a un haut rendement thermique, est de faible coût et présente une émission extrêmement faible de gaz à effet de serre. L'invention porte sur un procédé de fabrication d'un gaz contenant de l'hydrogène suivant lequel on sèche une boue organique, puis on soumet la matière sèche de boue organique obtenue à une pyrolyse, et on effectue un reformage à la vapeur d'eau du gaz de pyrolyse généré, le procédé étant caractérisé par le fait que le séchage de la boue organique est effectué tout en craquant la boue organique en présence d'agglomérats métalliques et/ou d'agglomérats céramiques, à une température de 100 à 200°C avec le vent chaud obtenu à l'aide de la chaleur de résiduaire générée lors de la conduite du procédé de production d'un gaz contenant de l'hydrogène.
PCT/JP2010/062592 2010-07-27 2010-07-27 Procédé de production d'un gaz contenant de l'hydrogène Ceased WO2012014277A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/JP2010/062592 WO2012014277A1 (fr) 2010-07-27 2010-07-27 Procédé de production d'un gaz contenant de l'hydrogène
JP2011529797A JP5385396B2 (ja) 2010-07-27 2010-07-27 水素含有ガスの製造方法

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/JP2010/062592 WO2012014277A1 (fr) 2010-07-27 2010-07-27 Procédé de production d'un gaz contenant de l'hydrogène

Publications (1)

Publication Number Publication Date
WO2012014277A1 true WO2012014277A1 (fr) 2012-02-02

Family

ID=45529525

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2010/062592 Ceased WO2012014277A1 (fr) 2010-07-27 2010-07-27 Procédé de production d'un gaz contenant de l'hydrogène

Country Status (2)

Country Link
JP (1) JP5385396B2 (fr)
WO (1) WO2012014277A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017072891A1 (fr) * 2015-10-28 2017-05-04 株式会社ジャパンブルーエナジー Procédé de récupération d'hydrogène
WO2018037481A1 (fr) * 2016-08-23 2018-03-01 株式会社ジャパンブルーエナジー Procédé de récupération d'hydrogène à partir de gaz de pyrolyse de biomasse
JP2018094537A (ja) * 2016-12-16 2018-06-21 月島機械株式会社 有機性廃棄物の処理方法および処理装置
CN108558175A (zh) * 2018-05-07 2018-09-21 浙江大学苏州工业技术研究院 一种畜热式低温热泵污泥干燥系统及方法
JP6590359B1 (ja) * 2018-07-06 2019-10-16 株式会社翼エンジニアリングサービス バイオマスを原料とする水素製造方法
JP2020128325A (ja) * 2019-02-08 2020-08-27 日立造船株式会社 水素製造方法および水素製造装置
JP2020157299A (ja) * 2014-09-23 2020-10-01 アワマ ゲー・エム・ベー・ハーａｗａｍａ ＧｍｂＨ 廃水処理方法及び廃水処理装置

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101900265B1 (ko) * 2016-10-21 2018-09-19 한국에너지기술연구원 미세입자 건조장치

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001028916A1 (fr) * 1999-10-21 2001-04-26 Ebara Corporation Procede de production d'hydrogene par gazeification de combustibles et production d'energie electrique a l'aide d'une pile a combustible
JP2001240878A (ja) * 2000-02-29 2001-09-04 Mitsubishi Heavy Ind Ltd バイオマスのガス化システム及びメタノール合成システム
JP2002338976A (ja) * 2001-05-15 2002-11-27 Ecomeet Solutions Co Ltd 廃油処理装置及び廃油処理方法
JP2004051821A (ja) * 2002-07-22 2004-02-19 Jfe Engineering Kk 水素製造装置

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001028916A1 (fr) * 1999-10-21 2001-04-26 Ebara Corporation Procede de production d'hydrogene par gazeification de combustibles et production d'energie electrique a l'aide d'une pile a combustible
JP2001240878A (ja) * 2000-02-29 2001-09-04 Mitsubishi Heavy Ind Ltd バイオマスのガス化システム及びメタノール合成システム
JP2002338976A (ja) * 2001-05-15 2002-11-27 Ecomeet Solutions Co Ltd 廃油処理装置及び廃油処理方法
JP2004051821A (ja) * 2002-07-22 2004-02-19 Jfe Engineering Kk 水素製造装置

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7167091B2 (ja) 2014-09-23 2022-11-08 アワマ ゲー・エム・ベー・ハー 廃水処理方法及び廃水処理装置
JP2020157299A (ja) * 2014-09-23 2020-10-01 アワマ ゲー・エム・ベー・ハーａｗａｍａ ＧｍｂＨ 廃水処理方法及び廃水処理装置
JPWO2017072891A1 (ja) * 2015-10-28 2018-08-16 株式会社ジャパンブルーエナジー 水素回収法
WO2017072891A1 (fr) * 2015-10-28 2017-05-04 株式会社ジャパンブルーエナジー Procédé de récupération d'hydrogène
US10722836B2 (en) 2015-10-28 2020-07-28 Japan Blue Energy Co., Ltd. Hydrogen recovery method
US11273405B2 (en) 2016-08-23 2022-03-15 Japan Blue Energy Co., Ltd. Method for recovering hydrogen from biomass pyrolysis gas
WO2018037481A1 (fr) * 2016-08-23 2018-03-01 株式会社ジャパンブルーエナジー Procédé de récupération d'hydrogène à partir de gaz de pyrolyse de biomasse
JPWO2018037481A1 (ja) * 2016-08-23 2019-06-20 株式会社ジャパンブルーエナジー バイオマス熱分解ガスからの水素回収方法
JP2018094537A (ja) * 2016-12-16 2018-06-21 月島機械株式会社 有機性廃棄物の処理方法および処理装置
CN108558175A (zh) * 2018-05-07 2018-09-21 浙江大学苏州工业技术研究院 一种畜热式低温热泵污泥干燥系统及方法
CN108558175B (zh) * 2018-05-07 2023-07-04 浙江大学苏州工业技术研究院 一种蓄热式低温热泵污泥干燥系统及方法
JP6590359B1 (ja) * 2018-07-06 2019-10-16 株式会社翼エンジニアリングサービス バイオマスを原料とする水素製造方法
WO2020008621A1 (fr) * 2018-07-06 2020-01-09 株式会社 翼エンジニアリングサービス Méthode de production d'hydrogène à l'aide de biomasse en tant que matière première
JP2020128325A (ja) * 2019-02-08 2020-08-27 日立造船株式会社 水素製造方法および水素製造装置

Also Published As

Publication number Publication date
JPWO2012014277A1 (ja) 2013-09-09
JP5385396B2 (ja) 2014-01-08

Similar Documents

Publication Publication Date Title
JP5385396B2 (ja) 水素含有ガスの製造方法
DK1799796T3 (en) Slurry drainage and sludge conversion into a renewable fuel
Hu et al. Syngas production by catalytic in-situ steam co-gasification of wet sewage sludge and pine sawdust
McKendry Energy production from biomass (part 3): gasification technologies
US20110239620A1 (en) Method for processing organic waste and a device for carrying out said method
JPH10156314A (ja) 廃棄物からのエネルギ回収方法
JP3916179B2 (ja) 廃棄物の高温ガス化方法及び装置
JP2000351979A (ja) 廃棄物のガス化処理方法
JP5683575B2 (ja) 有機廃棄物の熱分解ガス化のための新規な方法
JP5857340B2 (ja) 石炭をチャー・原料ガス製造と発電に利用する複合システム
JP2009233619A (ja) 有機性廃棄物処理方法、ガス化炉、改質炉、有機性廃棄物処理装置
ZA200703757B (en) Slurry dewatering and conversion of biosolids to a renewable fuel
JP3079051B2 (ja) 廃棄物のガス化処理方法
KR101507956B1 (ko) 유기성 폐기물을 이용한 열병합 발전 통합 에너지화 시스템 및 방법
JP2006205135A (ja) 複合廃棄物処理システム
JP2005274122A (ja) バイオマスを利用する廃棄物溶融処理方法
JP4218443B2 (ja) フェロコークスの製造方法
JP4155507B2 (ja) バイオマスのガス化方法およびガス化装置
CN104593080A (zh) 一种高效等离子炉气化系统
CN204529755U (zh) 一种移动床自热式加压气化富氢环境干馏炉
JP4397424B1 (ja) ガス化方法
JP4397423B1 (ja) ガス化方法
Bauer 98102892 Manufacture of synthetic fuel gas from downstream products of petrochemicals

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 2011529797

Country of ref document: JP

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10855288

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 10855288

Country of ref document: EP

Kind code of ref document: A1