CN103314083A - Process for producing synthesis gas - Google Patents
Process for producing synthesis gas Download PDFInfo
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- CN103314083A CN103314083A CN2011800654541A CN201180065454A CN103314083A CN 103314083 A CN103314083 A CN 103314083A CN 2011800654541 A CN2011800654541 A CN 2011800654541A CN 201180065454 A CN201180065454 A CN 201180065454A CN 103314083 A CN103314083 A CN 103314083A
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- 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
- C10J3/723—Controlling or regulating the gasification process
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- 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
- C10J3/30—Fuel charging devices
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- 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
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- 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
- C10J2300/0916—Biomass
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- 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
- C10J2300/0926—Slurries comprising bio-oil or bio-coke, i.e. charcoal, obtained, e.g. by fast pyrolysis of biomass
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- 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
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- 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
- C10J2300/094—Char
-
- 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
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- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process for controlling the carbon conversion of a gasifier fuelled with a carbonaceous feedstock by mixing in biomass, the process comprising the steps of (a) pressurizing the biomass and carbonaceous feedstock; (b) introducing the biomass and carbonaceous feedstock into the gasification reactor vessel;(c) partially oxidizing the carbonaceous feedstock/biomass with a molecular oxygen-comprising gas to obtain a synthesis gas comprising carbon monoxide and hydrogen; (d) measuring the C02 content of the syngas and comparing with a pre-determined value range;(e) adjusting the biomass/carbonaceous feedstock ratio by changing the biomass feed rate; wherein said biomass and carbonaceous feedstock comprises from 10 wt% to 50 wt% of biomass and wherein the level of biomass is adjusted within this range to control the carbon conversion.
Description
The present invention relates to a kind of method of producing synthesis gas stream from carbon raw material, the method is included under the given gasification temperature in gasification, transforms as means control carbon with biomass fuel.
WO03/012013 has described one way of life waste incomplete combustion to produce the method for synthetic gas.Described method also comprise by control be fed to oxygen-containing gas wherein temperature, control waste feeding rate and due to waste charging and the ratio of oxygen-containing gas charging, reach the thermal isolation reaction compartment and in the different piece of reaction compartment, control temperature.
JP2002194363 has described a kind of method of pressurized air flow bed coal-gasification, pass through the method, biomass can effectively for reducing the high calorie that produces by gasification, reduce ash content and produce the problem of gathering and melting in the operation of gasification furnace of pressurized aerated bed thus.The method is characterized in that bottom that coal particle is incorporated into gasification furnace of pressurized aerated bed producing coal gas of high temperature, biomass fuel is incorporated into top to bring and the contacting and gasified bio-matter fuel of coal gas of high temperature.Therefore, the height of the heat recovery boiler of gasification is can be controlled.
Among the present invention, before mixture being incorporated into the burner part of gasifier, carbon raw material (for example coal) can mix with biomass.Biomass and coal so are mixed with the synergy that helps to guarantee between oxygen enrichment biomass and the oxygen deprivation carbon raw material.Because the high oxygen concentration in the biomass material, under given gasification temperature, obtain the demand to moderator gas that carbon raw material fully transforms and decrease, and this demand even in coal/biomass mixture, be eliminated under the sufficiently high biomass mark.Usually use steam or carbonic acid gas or its combination as moderator gas.
The object of the present invention is to provide a kind of simplification, that energy efficiency is arranged and reproducible by carbon raw material being mixed into the method for controlling described carbon raw material conversion in the biomass fuel.Biomass generally have high oxygen concentration and can provide part to be used for carbon raw material and all transform required oxygen, and this has reduced again conversely to the moderator gas demand of steam for example.Need a certain minimum biomass mark to eliminate steam in biomass/carbon raw material mixture.This mark is determined by the final composition of lignocellulose-like biomass and carbon raw material.The common minimum score that obtains completely carbon conversion is the biomass of 10-30 % by weight in carbon raw material/biomass mixture; But also can use any mark between 10% to 50%.
Adopt following methods to realize above purpose.
A kind of by carbon raw material being mixed into the method for the carbon conversion of controlling the gasifier that acts as a fuel with described carbon raw material in the biomass, the method may further comprise the steps:
(a) to biomass and carbon raw material pressurization;
(b) biomass and carbon raw material are incorporated in the gasification reactor vessels;
(c) use the gaseous partial oxidation carbon raw material/biomass that comprise molecular oxygen to comprise the synthetic gas of carbon monoxide and hydrogen with acquisition;
(d) measure CO in the synthetic gas
2Content and compare with predetermined numerical range;
The ratio of (e) regulating biomass/carbon raw material by the feeding rate of change biomass;
Wherein said gasifier feed comprises the biomass of minimum 10wt% to 50wt%, preferred 10wt% to 30wt%, and wherein the level of biomass can be regulated in this scope as required with the conversion of control carbon and reduction or the elimination demand to moderator gas.The synthetic gas of producing by this method can also comprise water, hydrogen sulfide and carbonic acid gas.
The applicant finds by 10wt% is mixed with carbon-containing feeding to the biomass of 30wt% to 50wt%, preferred 10wt%, temperature in the gasifier can be used the ratio control of oxygen/carbonaceous fuel, and the conversion energy of carbon uses biomass/carbonaceous fuel ratio control, simplifies thus process control.The adding of described biomass has extra favourable effect to steam saving and oiler feed consumption and has reduced the whole carbon footprint of gasifier.
Below with more detailed description the present invention.
Can realize pressurization by lock-hopper system or (solid dispels) pump in the step (a).Lock-hopper system generally is used for the raw material pressurization to dry and solid.Pump can be used for liquid or the pressurization of slurry (mixture of solid and liquid) raw material.Solid pump can also be used for solid material is pressurizeed.
Pulverize in the step (b) or liquid slurry biomass energy is mixed with carbon-containing feeding or is fed to separately gasifier.Independent biomass feed duct to the gasifying reactor charging is preferred, because it will transform the time of response that reduces significantly the controller on step from carbon.The mixing energy of biomass and carbon-containing feeding carries out in a plurality of positions of preparation of fuel and pressurised zone.
In the step (c), can use coal or the oil-firing burner structure of any type.When being fed to separately biomass in the gasifying reactor, biomass can also be incorporated in the burner region of gasifying reactor by nozzle subsequently.Then will need oxygen for the biomass partial oxidation via the supply of carbonaceous fuel burner.
In the step (c), carbon containing/biomass material stands to comprise the partial oxidation of the gas of molecular oxygen.Described partial oxidation preferably carries out under the temperature between 1000 to 1800 ℃, and more preferably carries out under the temperature between 1200 to 1800 ℃.Carry out the residing pressure of partial oxidation preferably between 0.3 to 12MPa and preferably between 3 to 10MPa.When use comprises the raw material of ash content, select temperature condition so that will form slag layer in the inside of the reactor vessel that partial oxidation occurs.
In the step (d), CO
2Content preferably cleaned and cold synthetic gas in measure the downstream of wet scrubber for example.Preferred Quick Measurement is to minimize CO
2Time between concentration step and the control action kou.An example of this rapid measurement device based on infrared analyser.
In the step (d), the CO of synthetic gas
2Content is compared with predefined value.Step (e) middle controller is the preferred ratio of passing through the setpoint adjustments biomass/coal of change biomass feeding rate controller subsequently.
Carbon raw material is preferably coal, for example hard coal, brown coal, bituminous coal and sub-bituminous coal.The raw-material example of substituting carbon containing is the petroleum coke, mud coal and the heavy residue that extract from Tar sands or in deasphalting process, the pitch fractions of separating from described residue.From refinery the residual oil fraction of boiling more than 360 ℃ (for example), and directly derived from crude oil or also can be used as carbon raw material from the residue of oily method for transformation (such as thermo-cracking, catalytic pyrolysis, hydrocracking etc.).
Any biomass derived raw material that comprises the low moisture content that is usually less than 20wt% and can be milled to the particle with the size between 10 to 1000 microns all is suitable solid biologic raw material, and described solid biologic raw material consists of (comprising) carbon raw material 10wt% to the biomass components of 50wt%.The raw material that roasting by biomass sources obtains is very suitable and preferably it occupies higher biomass mark in mixture.Roasting is preferably made up in order to make the biomass charging be more suitable for gasification with compacting or granulation step, and wherein when the particle of roasting mixed with carbonaceous liquid, the biomass charging was with so-called dried forms or slurry form supply.The roasting of biomass material is known and for example at M.Pach, R.Zanzi and E.Bjornbom, Torrefied Biomass a Substitute for Wood and Charcoal.6th Asia-Pacific International Symposium on Combustion and Energy Utilization.May2002, Kuala Lumpur and in Bergman, P.C.A., " Torrefaction in combination with pelletisation-the TOP process ", ECN Report, ECN-C-05-073, Petten is described in 2005.
Another kind of suitable solid biomass fuel obtains by dry and slow pyrolysis biomass sources in the inventive method.In slow pyrolytic process, usually obtain the solid carbon feed component.Slowly pyrolysis is known and for example is described in " Pyrolysis and Other Thermal Processing " .US DOE14-08-2007.
Be used for the suitable liquid or solid biomass material of the inventive method by drying and the flash pyrolysis acquisition of biomass sources.In flash pyrolysis method, usually obtain solid carbon and liquid bio matter feed component.The two can both be with the raw material that acts on gasification process.Flash pyrolysis is known and for example at EP-A-904335; Dinesh Mohan, Charles U.Pittman, Jr., and Philip H.Steele.Pyrolysis of Wood/Biomass for Bio-oil:A Critical Review.Energy﹠amp; Fuels2006,20,848-889; And in E.Henrich:Clean syngas from biomass by pressurised entrained flow gasification of slurries from fast pyrolysis.In:Synbios, the syngas route to automotive biofuels, conference held from18-20May2005, Stockholm, Sweden is described in (2005).The present invention is also for the embodiment of wherein using so-called biomass slurry as raw material.Described slurry can obtain by mixed pyrolysis oil and charcoal.
Suitable biomass sources is weeds or agriculture residues.The logistics that the example of suitable residual product is plam oil industry, corn is industrial, biofuel is industrial, forestry is industrial, produce in wood processing industry and the paper industry.Some biomass is relatively costly, for example wooden pill.Therefore, for lowland as far as possible keeps process cost, the biomass sources of preferred lower cost, for example trunk of oil palm and sawdust.But the low amount that substitutes the required biomass of moderator steam has increased the chance of using from the biomass of waste material logistics, a small amount of acquisition in the common marked down ground of described biomass from waste material logistics.
The present invention provides a kind of method now, carries out the partial oxidation of carbon raw material with efficient manner by described method, and acquisition is applicable to the synthetic gas of the carbon footprint with minimizing of catalytic conversion reaction thus.Making us especially interested catalytic conversion reaction is hydrocarbon synthesis process.In hydrocarbon synthesis process, syngas catalytic conversion is the hydrocarbon compound in from methane to the high molecular weight molecules scope that comprises 200 carbon atoms of as many as (or under particular case even higher).The example of hydrocarbon synthesis process is the Fischer-Tropsch process of for example describing among WO02/02489, WO01/76736, WO02/07882, EP510771 and the EP450861.
Step (c) can be undertaken by different gasification process, for example at Gasification, by Christofer Higman and Maarten van der Burgt, 2003, Elsevier Science, Burlington MA, so-called moving-bed method, fluidized-bed gasifier method or the entrained flow gasifiers method described among the Pages85-128.The preferred entrained flow gasifiers of using because the method can be processed plurality of raw materials, and because has prepared the synthetic gas that does not contain tar.In this method, raw material and oxygen and stream are introduced in the reactor, preferably in the mode of suitable burner.Having described the example of suitable burner among US-A-4510874 and the US-A-4523529 preferably uses with them.This operational condition this means that service temperature is higher than the fusing point of ash content so that the method turns round under the slagging pattern.The gas of carbon raw material and molecule-containing keto provides described reactant in the burner that is present in the gasifying reactor and is converted into suitably synthetic gas by (and under preferred pressure between 4 to 8MPa) under the pressure between 3 to 10MPa.Service temperature is suitably between 1200 to 1800 ℃.Synthetic gas preferably with the direct chilling of water of evaporation, with the direct chilling of methanol-water mixtures, by with the indirectly heat exchange or uniting of these cooling steps be cooled to be lower than 1000 ℃ temperature of water of evaporation, preferably be lower than 500 ℃.In the bottom of described reactor, the solid of slag and other melting is discharged from gasifying reactor suitably.
Solid carbon raw material/biomass incoming mixture can be provided in the burner of air-flow gasifier reactor as the slurry in the water.Coal slurry material feed process has for example been described in EP-A-168128.Preferably solid carbon raw material/biomass material is provided in the burner in the gas-solid mixture of the feeding-in solid body that comprises powder type and suitable vector gas.Suitable vector gas is nitrogen, carbonic acid gas, Sweet natural gas or synthetic gas, namely comprises CO and H
2Mixture.Vector gas is preferably carbonic acid gas.The use of this vector gas has for example been described in WO-A-2007042562.
Fig. 1 has shown the preferred embodiment of the invention.
Fig. 1 schematically show for the production of with the system of cleaning synthetic gas.In gasifying reactor 9, introduce carbon-containing feeding, biomass charging and contain the oxygen charging.Oxygen and carbonaceous stream are respectively via pipeline 19 and 8 chargings.Biomass energy is fed to separately in the gasifying reactor 9 via pipeline 25, but can also mix with carbonaceous stream in charging and pressing section 7 via pipeline 5.Carbonaceous stream 8 and biomass logistics 25 at least in part oxidation in gasifying reactor 9 obtains original synthetic gas 10 and slag thus.For this reason, usually there are a plurality of burner (not shown)s to be present in the gasifying reactor 9.Biomass logistics 25 can also be incorporated into via the nozzle in the gasifying reactor combustion zone in the gasifying reactor 9, for example at burner charge level place.Then the oxygen that is used for the biomass partial oxidation will add the burner oxygen of carbonaceous stream 8 to.
The carbon of gasifier transforms with controller 18 controls.The input value that is used for carbon conversion controller is to use CO
2Analyser 17 is measured the CO of wet scrubber 15 downstream synthetic gas 16
2Content.CO
2Content one is reduced to and is lower than preset value, then needs to increase by the flow that changes biomass charging 3 and increase pipeline 5 or 25 ratio of biomass/coal.CO
2Concentration one surpass maximum predetermined value, then can reduce biomass/coal ratio by the flow that changes biomass charging 3 and reduce pipeline 4 or 25.Among WO2008125556A1 and the W0200768684A2 CO has been described
2The usefulness of the ratio of analyser and control steam and oxygen and carbon (O/C).
The advantage of using biomass control carbon to transform is to have used CO
2Natural matter, this has reduced the CO of factory
2Footprint.In addition, this application has also reduced being used for the gasify high pressure steam on island and the demand of high-quality oiler feed.
The original synthetic gas of producing is fed in the cooling zone 11 via pipeline 10; Here original synthetic gas is cooled to about 200-400 ℃ usually.Cooling zone 11 can be indirect heat exchanger or quench vessel.In the situation that quench vessel, preferably via pipeline 23 liquid water is injected in the synthesis gas stream.Liquid water preferably injects with the form of mist.
Cooling zone 11 can be integrated in the gasifying reactor pressurized vessel of reactor bottom or as independent container and install.When synthetic gas and slag all, are integrated into cooling zone 11 in the pressurized vessel out the time in the bottom of gasifying reactor, and synthetic gas and flying dust and slag will enter the cooling zone.When synthetic gas at the top and slag when leaving gasifying reactor 9 in the bottom, then only have synthetic gas and flying dust will enter in the cooling zone of installing as the single area of reactor downstream.
Shown in the embodiment of Fig. 1, the original synthetic gas that leaves cooling zone 10 is further processed.For this reason, described original synthetic gas is fed to drying or wet solid via pipeline 12 and removes in the unit 13 in order to remove at least in part ash content in the original synthetic gas.Because it is known to persons of ordinary skill in the art that solid is removed unit 13, does not further discuss here.Remove the unit except deashing via pipeline 24 from solid.Solid is removed after the unit 13, and original synthetic gas can be fed in the gas washer 15 and subsequently via pipeline 14 and be fed to the production area via pipeline 16.Further process after the synthetic gas, remaining synthetic gas can be used for multiple use, for example generating, H
2, fertilizer, fischer-tropsch liquid and other chemical production.
Computer simulation to moderator steam along with modeling is carried out in the minimizing of adding biomass in coal.For the Drayton coal gasification of selecting, carbon transforms in order to obtain completely under 1500 ℃ gasification temperature with the about 76kg steam of needs coal per ton.As shown in table 1, follow timber to add coal and will reduce gradually demand to moderator.Replace with timber 25% coal, can eliminate moderator steam.
Show common moderator consumption under the biomass marks different in 1--biomass/coal mixtures
Claims (14)
1. the method for the carbon conversion by carbon raw material being mixed in the biomass gasifier that control acts as a fuel with described carbon raw material, the method may further comprise the steps:
(a) to biomass and carbon raw material pressurization;
(b) biomass and carbon raw material are incorporated in the gasification reactor vessels;
(c) use the gaseous partial oxidation carbon raw material/biomass that comprise molecular oxygen to comprise the synthetic gas of carbon monoxide and hydrogen with acquisition;
(d) measure CO in the synthetic gas
2Content and compare with predetermined numerical range;
The ratio of (e) regulating biomass/carbon raw material by the feeding rate of change biomass; Wherein said biomass and carbon raw material comprise 10wt% to the biomass of 50wt% and wherein regulate the level of biomass with the conversion of control carbon in this scope.
2. according to claim 1 method wherein is incorporated into carbon raw material and biomass in the gasifying reactor respectively.
3. according to claim 1 method is wherein introduced carbon raw material and biomass in the gasifying reactor as mixture.
4. each method according to claim 1-3, the raw material that wherein is fed in the gasifier comprises 10wt% to the biomass fuel of 30wt%.
5. each method according to claim 1-4, wherein biomass are the solid biomass that obtain by roasting.
6. each method according to claim 1-5, wherein biomass are the solid biomass that obtain by the slow pyrolysis of biomass sources.
7. each method according to claim 1-6, wherein biomass are the solid biomass that obtain by the biomass sources flash pyrolysis.
8. according to claim 4 method, wherein biomass are the liquid bio matter that obtains by the biomass sources flash pyrolysis.
9. according to claim 4 method, wherein biomass are the slurry biomass by the compositions of mixtures of the pyrolysis oil that obtains by the biomass sources flash pyrolysis and charcoal.
10. each method according to claim 1-9, wherein carbon raw material is coal.
11. each method according to claim 1-9, wherein carbon raw material is residual oil.
12. each method according to claim 1-11, wherein in the step (c), to be present in pressure be to be converted into synthetic gas in the burner in 1 to 10MPa the gasifying reactor by described reactant is provided to for carbon raw material/biomass fuel material mixture and the gas that comprises molecular oxygen.
13. each method according to claim 1-12, wherein CO in the step (d)
2Content use based on infrared analyser and measure.
14. each method according to claim 1-13, wherein step (e) the middle controller ratio that will regulate biomass/coal by the setting point that changes biomass feeding rate controller.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP10196098.7 | 2010-12-21 | ||
| EP10196098 | 2010-12-21 | ||
| PCT/EP2011/073417 WO2012084953A1 (en) | 2010-12-21 | 2011-12-20 | Process for producing synthesis gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103314083A true CN103314083A (en) | 2013-09-18 |
| CN103314083B CN103314083B (en) | 2015-07-22 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201180065454.1A Active CN103314083B (en) | 2010-12-21 | 2011-12-20 | Process for producing synthesis gas |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US20130326954A1 (en) |
| EP (1) | EP2655566A1 (en) |
| CN (1) | CN103314083B (en) |
| AU (1) | AU2011347466B2 (en) |
| MY (1) | MY165497A (en) |
| WO (1) | WO2012084953A1 (en) |
| ZA (1) | ZA201304552B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103838265A (en) * | 2014-03-07 | 2014-06-04 | 西北化工研究院 | Control system for controlling ratio of hydrogen and carbonic oxide in synthesis gas production process |
| CN106574195A (en) * | 2014-07-28 | 2017-04-19 | 可持续废料电力系统有限公司 | Method of synthetic fuel gas production |
| CN108905962A (en) * | 2018-06-26 | 2018-11-30 | 江苏新亿源环保科技有限公司 | A kind of preparation method of biomass carbon adsorbent material |
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- 2011-12-20 EP EP11799698.3A patent/EP2655566A1/en not_active Withdrawn
- 2011-12-20 US US13/995,970 patent/US20130326954A1/en not_active Abandoned
- 2011-12-20 CN CN201180065454.1A patent/CN103314083B/en active Active
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| CN103838265B (en) * | 2014-03-07 | 2016-09-28 | 西北化工研究院 | A kind of in the control system producing synthesis gas time control hydrogen and carbon monoxide ratio |
| CN106574195A (en) * | 2014-07-28 | 2017-04-19 | 可持续废料电力系统有限公司 | Method of synthetic fuel gas production |
| CN108905962A (en) * | 2018-06-26 | 2018-11-30 | 江苏新亿源环保科技有限公司 | A kind of preparation method of biomass carbon adsorbent material |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2011347466B2 (en) | 2015-07-16 |
| EP2655566A1 (en) | 2013-10-30 |
| ZA201304552B (en) | 2014-03-26 |
| US20130326954A1 (en) | 2013-12-12 |
| MY165497A (en) | 2018-03-27 |
| WO2012084953A1 (en) | 2012-06-28 |
| CN103314083B (en) | 2015-07-22 |
| AU2011347466A1 (en) | 2013-07-11 |
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