CN102076830A

CN102076830A - A two-stage high-temperature preheated steam gasifier

Info

Publication number: CN102076830A
Application number: CN2009801244320A
Authority: CN
Inventors: W·布拉斯亚克; W·杨
Original assignee: Boson Energy SA
Current assignee: Boson Energy SA
Priority date: 2008-05-29
Filing date: 2009-05-29
Publication date: 2011-05-25
Also published as: EA201001822A1; WO2009145724A2; AU2009251931A1; SE534810C2; SE0801266A0; EP2300568A2; AP2010005514A0; JP2011522084A; US20110078951A1; SE1051371A1; WO2009145724A3; CA2726250A1; ZA201009075B; EA017739B1; BRPI0912280A2

Abstract

A gasifier is disclosed combing two reactors using externally generated preheated high temperature steam injection into the first reactor, where the heating demand for gasification is supplied by the sensible energy from the steam. The gasifier can produce a medium and higher LCV syngas. The first reactor is a fixed bed gasification section where the coarse feedstock is gasified, and the second reactor is an entrained-bed gasification section where the liquid and fine feedstock is gasified. Solid coarse feedstock is devolatilized in the first fixed bed reactor of the gasifier by means of high-temperature steam, and subsequently, in the second reactor subjected to a higher temperature sufficient to crack and destroy tars and oils. Activated carbon may be formed as co-product. The gasifier may be used with various solid and liquid feedstocks. The gasifier is capable of gasifying such different feedstocks simultaneously.

Description

Two sections high temperature preheating steam gasification devices

Invention field

The present invention relates generally to and be used for producing synthetic gas and optional two sections high-temperature steam gasifiers of gac by thick carbon-containing feeding, and the gasifier of relate more specifically to gasify simultaneously thick solid carbon charging and thin solid carbon charging or liquid carbon-containing charging.The invention still further relates to and use the thick carbon-containing feeding that gasifies of the two stage gasification device with two reactors, to produce synthetic gas and optional process of active carbon, wherein not to first section reactor feeding oxygen, only feeding temperature be at least 700 ℃ pre-hot steam.

Background of invention

Gasification is to use reagent as separately or the air that is used in combination arbitrarily, steam and oxygen, and with feeding-in solid body such as solid coal, refinery coke, biomass and/or solid waste, liquid feeding such as black liquor oil or gaseous feed are converted into mainly by hydrogen (H ₂) and carbon monoxide (CO) composition, contain amounts of carbon dioxide (CO ₂), water (H ₂O), methane (CH ₄), higher hydrocarbons and nitrogen (N ₂) the elevated temperature heat decomposition course of fuel gas.

Described hot gas process is the chemical reaction that highly absorbs heat.One of be used for to the common method of described gasification heat supply in the following ways: a) external heat source, sensible heat as hot coke (char) recirculation, and/or the sensible heat of the vaporized chemical that is heated, the reaction heat of b) part charging (carbonaceous material of input) oxidation, and c) non-carbonaceous material such as unslaked lime and CO ₂Thermopositive reaction heat.

The quoting of partial combustion technology of the carbonaceous material of input is widely adopted.When using this technology, produced non-flammable gas CO ₂, and, cause forming the synthetic gas of dilution, and the LCV of gained synthetic gas (lower calorific value, the tolerance of the fuel value of dry gas material) is restricted owing to it is not removed.In addition, the CO that partial combustion (oxidation) produces ₂Existence cause the little dividing potential drop of other gaseous matter, this is unfavorable for other valuable gasification reaction, such as for example water gas shift reaction.Thereby the hydrogen content in the described synthetic gas is subjected to negative impact.

Considered in the recent period and used sensible heat to replenish the idea of the required main energy of gasification, and demonstrated positive result.For example, US 2004/0060236A1 has instructed the small scale gasification systems that is used for solid fuels is turned to the economy of pyrolysis gas, and wherein heating gas mixture and the described pyrolysis gas with steam and air together imports in the reformer, produces the thick gas of reforming of high temperature.The gas mixture of air and steam preferably is heated at least 300 ℃, and more preferably at least 400 ℃.The interchanger of any kind or well heater all can be used as the air heating unit of the gas mixture of described air of heating and steam.

US 6,837, and 910 have instructed and are used for gasified liquid or solid-fuelled equipment and method, wherein the hot gas mixture of steam and air imported in the reformer section of the pyrolysis zone of described solid or liquid fuel and thermolysis gas at least one.The gas mixture of air and steam is heated at least 700 ℃ temperature, and more preferably is higher than 800 ℃.

Other known system that will high temperature air/steam/oxygen gas be used for biomass/waste gasification process (Lucas C. that also is applied up to 1000 ℃, Szewczyk D., Blasiak W., Mochida S., High Temperature Air and Steam Gasification of DensifiedBiofuels, Biomass and Bioenergy, Vol.27, No.6, December 2004, pages563-575).Ponzio Anna, Yang Weihong, Lucas, C, Blasiak W. is at Development of a Thermal Homogenous Gasifier System using HighTemperature Agent, CLEAN AIR-International Journal on Energy for aClean Environment., Vol.7, No.4., proposed not contain burnt hydrogen-rich gas in 2007, wherein said process only 1000 ℃ of use temperatures steam and under the normal pressure of about 1atm, carry out.

In US 2003/0233788A1, disclose that to be used for gasification of carbonaceous materials be the method for fuel gas.It comprises formation temperature be about 1316 ℃ to about 2760 ℃, mainly comprise water vapour, carbonic acid gas and hyperergy free radical thereof surpass hot steam (USS) composition.The described USS composition that comprises thermal-flame contacts with carbonaceous material, makes its gasification/reformation rapidly.Described USS forms by the fuel that does not contain ash content substantially that burns with " artificial air " that comprise enhanced oxygen and water vapour, and wherein said " artificial air " is at least about 60 moles of %.Must control oxygen/fuel ratio, thereby not generate cigarette ash.Strengthen the running cost that the use of oxygen in described method can significantly improve described method.

According to US 2003/0233788A1, from the just also commercial after deliberation gasification process of only using steam that used of about 1950-1960.Yet because the heat in the steam is limited, the problem of only using the gasification process of steam to follow comprises that attainable temperature of reaction is lower, promptly is usually less than about 815 ℃, and wherein long residence time and high energy account for leading.

All above-mentioned prior aries are only used first stage reactor, or fixed bed or fluidized-bed gasifier.

Also the thermal transition of known organism matter/refuse/coal can be regarded as and comprises two main high endothermic phases: the conversion with coke of removing that is volatile matter respectively.Studies show that of early stage, if be heated to above 600 ℃, 90% volatile content can abrupt release in the biomass gross weight.Subordinate phase is that coke transforms.In order not contained the ash content of coke, promptly 100% coke transforms, and needs high a lot of temperature to carry out the thermal transition of coke.Usually, this temperature should be higher than 1000 ℃, specifically depends on the fusing point of ash content.

Generate (＜10MW at the small-scale energy _Th) in be extensive use of the fixed bed gasifiers type because its structure and operation are very simple.Have been found that if above-mentioned two stages are followed in the design of the fixed-bed reactor that gasify, see that from multiple angles it all can become more effective.

This operating method for fixed bed gasifiers has a large amount of work to do.Usually adopt secondary air is injected gasifier.For example, (Y.G.Pan such as Pan, X.Roca, E.Velo and L.Puigjaner are at Removal of tar by secondary air injection in fluidized bedgasification of re-sidual biomass and coal, Fuel 78 (1999) (14), among the pp.1703-1709) reported by only be positioned at temperature 840-880 ℃ fluidized-bed the biomass feed points above inject the tar that secondary air has reduced 88.7wt.%.

(Biomass gasification with air in an atmospheric bubblingfluidized bed.Effect of six operational variables on the quality ofproduced raw gas such as Narv, Industrial and Engineering Chemistry Research 35 (1996) (7), pp.2110-2120) in the freeboard of fluidized-bed gasifier, carry out the injection of secondary air, and observe about 70 ℃ temperature and rise, this causes tar to drop to 16g/Nm from 28 ³

The Asian Institute of Technology of Thailand (AIT) has transformed the gasifying biomass device, and it can obtain the about 50mg/Nm of tar output ³Fuel gas, this is than low about 40 times (the T.A.Milne and R.J.Evans of the first stage reactor under the similar operations condition, Biomass Gasification " Tars ": Their Nature, Formation and Conversion.NREL, Golden, CO, USA, Report No.NREL/TP-570-25357 (1998)).Inferior pumping type (downdraft) gasifier with secondary air air inlet has been adopted in this design.The tar that produces in biomass pyrolysis process can and can at high temperature decompose by being positioned at the high temperature residual coke bed of bottom.

Bhattacharya etc. are at A study on wood gasification for low-tar gasproduction, Energy 24 (1999), reported similar gasifier among the pp.285-296, wherein the inner coke that produces of gasifier itself serves as strainer and comes further tar output significantly to be reduced to 19mg/Nm ³, CO in the fuel gas and H ₂Concentration is higher.

Cao etc. have reported the research of two district's fluidized-bed reactors at A novel biomass air gasification process for producingtar-free higher heating value fuel gas among Fuel Processing Technology 87 (2006) 343-353.In this research, with the upper area of auxiliary fuel gas and secondary air streams injecting reactor to reduce tar composition.Test-results shows about 5MJ/Nm ³Calorific value.

US 6,960, and 234 disclose multiaspect (multi-faceted) gasifier and methods involving.This gasifier has merged fixed bed gasification section and entrained flow gasification section.Form gac in top fixed bed section and air flow bed Duan Zhongke.

US 6,647, and 903 disclose the method and apparatus that is used to produce and utilize combustible gas, and it has used the gasifier that comprises first and second conversion zones, wherein oxidizing gas injected two sections.This invention is decomposed the fuel gas of formation output simultaneously product H to strengthen tar ₂Operate with the mode of CO.In addition, also can form part methane.In some operator scheme, can produce gac.

JP 6256775 discloses and has been used for two sections methods that are gasified totally of methane synthetic organic substance, wherein organic substance gasifies in the presence of steam and oxygen in first section gasification, and gaseous state unreacted matters and tar gas gasify under the higher temperature in than first section gasification in second section gasification.Also disclose and comprised two sections gasifier.In order to stop solid carbon-containing material to be passed to second section gasification, can or can between two sections, strainer be set with the channel narrows between two sections from first section gasification.Described gasifier comprises two input apertures that are used for oxygen and steam, and one at first section and another is at second section.

In above-mentioned research, secondary air/oxygen and/purpose that fuel injects is the temperature that improves in the freeboard, to decompose tar and to improve steam reforming reaction.Yet the injection of secondary air not only can improve the especially content of nitrogen of thinner, but also can reduce the combustible content that gasification produces.This causes the LCV of the fuel gas that generates to descend.In addition, the feasible composition that is difficult to control the gas that generates of the injection of secondary air.

Above-mentioned US 6,960,234 points out that also the fixed bed gasification requirement typically has a diameter from the thick fuel of 1/4 " 2 ", and the restricted technical characterictic of fixed bed gasification comprises: tar and oil are synthesized gas and carry; They are difficult to use coal/fuel powder, because can block the void space between the interior thick fuel of fixed bed; And be difficult to use the liquid hydrocarbon charging.

In order to produce the inflammable gas of medium and higher low heat value (LCV), and gasify simultaneously solid and liquid/thin charging, and producing other additional valuable substance such as gac, this paper provides a kind of novel fixed bed gasifiers.Described in this class gasifier such as the claim 1.And; the two stage gasification device that also open and claimed use has two reactors gasifies thick carbon-containing feeding to produce synthetic gas, optional process of active carbon; wherein not to first section reactor feeding oxygen, but only feeding temperature be at least 700 ℃ pre-hot steam.This method is documented in the claim 4.

Summary of the invention

Therefore, for the two stage gasification device of prior art, for example the two stage gasification device of putting down in writing in disclosed and claim 1 preamble among the JP 6256775 comprises: be equipped with the inlet that is used for thick carbon-containing feeding and be used for first reactor of first inlet of steam; And be equipped with and be used for steam, optional with air or oxygen, second reactor of second inlet; And the outlet that is used for synthetic gas; The crevice that wherein said first and second reactors are had the cross section that reduces is separated, this crevice is used to limit the circulation of unreacted solid carbonaceous substance from first reactor to second reactor, wherein said first reactor can move under at least 600 ℃ temperature, and wherein said second reactor can move under higher temperature, above-mentioned purpose realizes by the technical characterictic of described claim characteristic, according to described second reactor of this claim is the bottom reactor, described first reactor is a upper reactor, bottom at first reactor is equipped with grid, described first inlet that is used for steam is set to close on the bottom of described first reactor, thereby the pre-hot steam of temperature at least 700 ℃ can be fed to described first reactor from described grid below via described inlet, described first reactor is equipped with the outlet that is used for synthetic gas, described second reactor is equipped with the inlet that is used for thin solid carbon charging and/or liquid carbon-containing charging, described second inlet that is used for steam is set to close on the bottom of described second reactor, thereby can be at least 700 ℃ pre-hot steam with temperature, randomly with the preheated air or the oxygen of uniform temp, be fed to described second reactor from the below via described inlet, and be equipped with second crevice with the cross section that reduces in the bottom of described second reactor.

Therefore, in one aspect of the invention, relate to aforesaid two stage gasification device.

In gasifier of the present invention, the thin and/or fluent material of can gasify simultaneously solids crude material and solid.The carbon containing roughage is fed in first reactor, and carbon containing (giving up) liquid and/or the thin solid material of carbon containing are fed in second reactor.

In the further preferred embodiment of described two stage gasification device, one or more and preferably all inlets that is used for steam, air, oxygen and carbon containing (giving up) liquid and/or the thin solid material of carbon containing all tangentially enter in the described gasifier in the corresponding section of described gasifier, and these parts have circular interior cross section.

In the further preferred embodiment of described two stage gasification device, the inlet that is used for carbon containing (giving up) liquid and/or the thin solid material of carbon containing comprises the inlet that at least two apart maximum distances of the circumference along described circular cross section distribute.

In another aspect of this invention, relating to using and have two reactors, is respectively first and second reactors, the two stage gasification device thick carbon-containing feeding that gasifies, to produce synthetic gas and optional process of active carbon.These class methods are documented in the claim 4, and comprise the steps: that (a) is fed into thick carbon-containing feeding in first section reactor of gasifier; (b) under at least 600 ℃ reactor service temperature, make steam in first section reactor of described thick carbon-containing feeding contact, to realize the gasification of described carbon-containing feeding, feeding oxygen in described first section reactor not in the method, and only feeding temperature be at least 700 ℃ pre-hot steam, and described method also comprises step (c), the any solid and/or liquid carbon-containing material the choosing wantonly in the second section reactor that moves under at least 700 ℃ temperature of step (b) gained are contacted, to obtain the arbitrary combination of following product: gac with the pre-hot steam of air or oxygen; CO; CO ₂, and the combustion heat.

In preferred embodiment, described method comprises another step (d), wherein thin solid carbon of feeding and/or liquid carbon-containing charging in second section reactor of gasifier simultaneously.Therefore, in this embodiment, can be simultaneously to the thick charging of described gasifier feeding and thin solid and/or liquid carbon-containing charging.

In another preferred implementation of described method, also be at least 700 ℃ pre-hot steam to the outside temperature that generates of described second section reactor feeding.By this embodiment, the internal-combustion in the gasifier is also referred to as partial combustion or oxidation, can keep minimum, because required energy is provided by the outside.Therefore, in this embodiment, do not need to be used for gas or the oxygen supply that heat is given birth in internal-combustion.And when not to the second reactor feeding air or oxygen, it is maximum that the yield of gac can reach.

In the further preferred embodiment of described method, to the second reactor feeding air (promptly except that described high-temperature steam).By this embodiment, can obtain very high-quality synthetic gas, because carbon also is converted into CO, and be not only gac.And,, still can avoid internal-combustion (promptly to produce CO according to the ratio of steam/air ₂).Simultaneously, can also recently control CO by the control steam/air: the ratio of gac.

In the further preferred embodiment of described method, use purity oxygen (replaces air).In this embodiment, described method can be used for industrial purposes.Simultaneously, the demand of separation of by-products is reached minimum, and undesirable diluting effect of gaseous product is kept minimum.

With reference to describing in detail and claim, other embodiment and advantage are conspicuous.

Term " internal-combustion ", " partial combustion " and " partial oxidation " are used for being illustrated in the burning that takes place in the gasifier interchangeably.

Description of drawings

Fig. 1 has shown that general description is used for the system flowchart of the gasification process of the present invention of biomass and solid waste.

Fig. 2 has shown the sectional view of the embodiment of gasifier 21.

Fig. 3 is the vertical view of gasifier of the present invention, has shown that the tangential liquid feeding by inlet 19a and 19b injects.

Embodiment

Gasifier of the present invention has merged two reactors, uses the outside preheating high-temperature steam that generates to inject first reactor, and wherein being used to the demand for heat that gasifies is provided by the sensible heat of this steam.Described gasifier can produce the synthetic gas of medium and higher LCV.First reactor is the fixed bed gasification section that thick charging is gasified, and second reactor is the entrained flow gasification section that liquid and thin charging are gasified.By high-temperature steam, make the solids crude charging in first fixed-bed reactor of gasifier, remove volatile component, and in second reactor, it is applied the higher temperature that is enough to cracking and destroys tar and oils subsequently.

Can form gac as by product.Described gasifier can use various solids and liquid feeding.These the different chargings of can gasifying simultaneously of described gasifier.

As shown in Figure 1, design of the present invention is that gasifier 21 is divided into two sections: first epimere 3 is used for removing of volatile component, this first section is only used the outside pure steam of high temperature preheating (preferred 700 ℃-1000 ℃) that generates, and second hypomere 4 is used for the thermal transition of coke, it uses air and steam, oxygen and steam or the high temperature of steam (preferred 700 ℃-1600 ℃, more preferably 800 ℃-1200 ℃) preheated mixture only.Reactor 3 comprises the fixed bed with grid 8.

In first reactor 3, the energy that is used for the volatile component subtractive process is by 7 being fed to the sensible heat of the steam in first reactor and providing jointly via the hot logistics of crevice 20 from second reactor by entering the mouth.The level that amount by being fed to the steam in the described reactor and temperature are controlled at the temperature in described first reactor at least 600 ℃.

In first reactor 3, with high-temperature steam with via the inlet the 2 thick chargings (biomass) 1 that enter mix.When biomass were heated by high-temperature steam, the volatile component subtractive process carried out as follows:

Simultaneously, because the existence of steam, steam and volatile component reaction:

CO+H ₂O→CO ₂+H ₂ (3)

React according to following reaction formula by the minor amounts of oxygen that the pyrolytic process (it occurs in first reactor, and also occurs in second reactor when injecting liquid and/or the thin charging of solid) and second reactor 4 discharge:

C _mH _n+(m/2+n/4)O ₂→mCO+n/2H ₂O (4)

CO+ ¹/ ₂O ₂→CO ₂ (5)

H ₂+ ¹/ ₂O ₂→H ₂O (6)

CO+H ₂O→CO ₂+H ₂ (7)

Because the temperature of reactor in first section reactor 3 are controlled at least 600 ℃ level, and the residence time also is controlled, and the gas in first reactor is in the environment that lacks very much oxygen, therefore any solid that in first reactor, produces and/or liquid coke not can with any oxidant reaction in the described reactor.Thereby any solid and/or liquid coke can be subjected to the effect of gravity and fall in second reactor 4.

In second reactor 4, the energy that is used for the coke conversion process preferably provides by the sensible heat of steam and air mixture and from the partial oxidation of coke.In order to realize not having the conversion of coke, the temperature in second reactor should be higher than the fusing point of ash content, so that ash content forms slag.Usually, for the timber biomass, the fusing point of ash content can be 1300 ℃.Reactor 4 comprises the air flow bed with grid 5.

When not having other charging (liquid and fine particle) to inject, principal reaction is:

Gasification:

C+O ₂＝＞CO ₂-393.5kJ/mol(8)

C+H ₂O＝＞CO+H ₂+131.3kJ/mol(6)

C+2H ₂O＝＞CO ₂+H ₂+90.2kJ/mol(10)

-partial oxidation:

C+0.5O ₂＝＞CO-110.5kJ/mol(11)

-Boudouard reaction (Boudouard reaction):

C+CO ₂＝＞2CO-172.4kJ/mol(12)

-water-gas shift:

CO+H ₂O＝＞CO ₂+H ₂-41.1kJ/mol(13)

-methanation:

CO+3H ₂＝＞CH ₄+H ₂O-206.1kJ/mol(14)

-hydrogenation:

C+2H ₂＝＞CH ₄-75kJ/mol(15)

When second charging (liquid and fine particle) was injected in second reactor, (1)-(15) that respond all can take place.

Many reactions take place simultaneously, and are difficult to the described process of like that accurately controlling as shown here.Yet,, may make some maximization of required product, for example gac and synthetic gas by the processing parameter among careful selection the present invention (temperature, the residence time and oxygen/steam ratio).

In addition, gac can be used as the by product of carbon-based material after via thermal transition of the present invention and handles.Usually, the preparation of gac in the prior art comprised for two steps: under the condition of high temperature (500-1000 ℃) anaerobic raw material is carried out carbonization, to remove the oxygen and the protium of maximum, and under higher temperature, simultaneously carbonized product is activated at oxidizing gas such as water, carbonic acid gas or both.Described activation should be carried out under the condition of fully control, to realize required conversion.

In the present invention, charging is at first gasified by the pure steam of high temperature (600 ℃ levels) in first reactor 3 at least, preferably by high-temperature steam carbon is activated in second reactor 4 subsequently.

In the present invention, roughly as shown in Figure 1, high-temperature steam and optional air or oxygen (above 700 ℃) mainly obtain by use honeycomb regenerator formula interchanger, described interchanger is incorporated herein by reference in this associated viscera with these open source literatures described in for example EP0607921 or common unsettled PCT/SE2009/050019.

Fig. 2 has shown the sectional view of gasifier 21.Carbon-containing feeding 1 enters via feed entrance 2 at the gasifier top, and moves ahead downwards and move through first reactor 3, by grid 8, enters second reactor 4 then subsequently, 6 becomes fused ash content up to it in the bottom by grid 5 again.Charging can comprise biomass, coal, municipal solid waste or their arbitrary combination.The granularity of thick carbon-containing feeding 1 is generally 0.5cm to 1.8cm, is preferably 0.5 to 1.2cm.

In first reactor 3, the combination of the sensible heat that the stack gas that sensible heat that carries by high-temperature steam (above 700 ℃) and coke oxidation and gasification in second reactor 4 are produced is entrained adds hot feed.The high-temperature steam that is used for the charging gasification in first reactor that pipeline 7 carries enters crevice or throat 20 via port (or a plurality of port) 11.The amount of the high-temperature steam that adds at port 7 places is set at the temperature that site 3 (first reactor) located and remains between 600-900 ℃, and preferably is higher than 700 ℃.Near 8 (grids) site, in the time of in air or oxygen is fed to second reactor, the combustion flame that heat may occur, because the pyrolysis gas firing that superfluous oxygen discharges charging 1, and form any liquid and/or the thin feeding-in solid body that is fed in second reactor.

Temperature in the reactor 3 is passed through the temperature and the flow of 7 steam that inject from the site, and comes the temperature and the amount of the superfluous oxygen of autoreactor 4 to control.The residence time of charging 1 in reactor 3 mainly controlled by the gap of grid 8.

Good mixing in order to realize gasifying between reagent (steam) and the charging 1 provides throat 20.The diameter of throat 20 is usually less than the diameter of reactor 3 sieges.The gradient of tapered section 14 should be preferably about 45-60 °.The diameter of steam injection port 11 should be preferably than the little 2-3 of diameter of throat 20 doubly.

Described thick carbon-containing feeding is removed volatile component by high-temperature steam in first reactor 3 after, remaining fixed carbon becomes gac coke and ash content solid, they continue to move down by grid 8, enter throat 20 then, enter second gas 4 that hardens subsequently, they are by high temperature air (or oxygen) and steam mixture institute's oxidation and gasification therein.When not having air or oxygen and described steam together to be fed in the reactor 4, oxidation can not take place, and only be gasification in reactor 4.Temperature in second reactor 4 further is increased to the ash content softening temperature of the fuel at a little higher than grid 5 places.Pipeline 9 is carried to port one 0 with preheating high-temperature steam or high temperature air (or oxygen) with steam mixture, enters second throat 18 subsequently.

For the wood substance grain of being produced by the timber of growing in Sweden, the ash content softening temperature is generally 1350-1400 ℃.If avoid ash content to form slag, the peak-peak temperature in the run duration reactor 4 should remain on than low 50 ℃ of described ash content softening temperature at least so, and common and preferred maximal condition is low 100 ℃.

Temperature in the reactor 4 are by preheating temperature, flow and the steam ratio to carbon, and when air or oxygen and steam together used, steam was controlled the ratio of the oxygen of mixture.

The diameter of second crevice or throat 18 is usually less than the diameter of reactor 4, and preferred also less than the diameter of first crevice or throat 20.The gradient of tapered section 17 should be preferably about 45-60 °.The diameter of steam injection port 10 should be preferably than the little 3-5 of diameter of throat 18 doubly.

Ash content is fallen into bottom 6 by throat 18, and can take out from reactor off and on.

Synthetic gas flows out by outlet pipe 12.Because the temperature in first reactor 3 is enough high, and has steam, therefore most tar is destroyed and be converted into synthetic gas.The main chemistry of synthetic gas is hydrogen, carbon monoxide and methane, carbonic acid gas.

Gasifier designs of the present invention has the hydrogen advantageously controlled in the synthetic gas and the ability of carbon monoxide ratio, because described gasifier makes it possible to steam in very wide scope inner control gasifier to the ratio of oxygen.

In a kind of embodiment of the operation of described reactor, by the temperature in second reactor 4 is controlled at 700 ℃, promptly the temperature with first reactor 3 is identical, and passes through only to the second reactor feeding steam, and all tar and oils are all consumed by described high-temperature steam.This is converted into gac with most fixed carbon in gasifier.Therefore, gasifier described herein and method also can produce gac effectively.This operating method can produce gac very effectively, and has improved the quality of gained gac.On the other hand, if make the gasification maximization, second reactor should be operated under than the higher temperature of first reactor so.

Therefore, the present invention also can be used for producing gac.There are two kinds of methods can generate gac at reactor.In first method, only use first reactor, promptly only inject high-temperature steam by pipeline 7.Be closed from the steam of pipeline 9 and the hot mixture of air.Another kind of and preferred method is that two reactors are all moved, but only injects high-temperature steam from pipeline 9.In this case, gac directly is gathered into dried forms.Be surprised to find that second method can access higher-quality gac coke.Believe that this is because the high-temperature steam that injects by pipeline 9 makes the hole of gac open at second reactor 4.Therefore, the gac in wideer hole in can obtaining compared to existing technology by method of the present invention.Described size (aperture) can be controlled by the vapor temperature in the reactor 4.Usually, more pyritous steam increases the hole count of gac.

Therefore, the present invention can realize dual production (gas and gac) by a kind of and identical charging 1.The required ratio of product can decide according to price of the type that can get charging, product or the like.

In addition, the present invention can be used for handling carbonaceous material and the fine particle and/or the liquid feeding of coarse particles (diameter is greater than 0.5cm).

Fig. 3 has shown the sectional view of gasifier 21, and it has shown tangent line liquid/fine particle charging injection.Two injection lance 19 (19a and 19b) are shown as and are connected to reactor 4.Can in reactor 4, inject the liquid residue of collecting behind little baking oven (micro-oven) pyrolytic process of liquid feeding such as Automotive Shredder Residue (ASR), and thin or atomizing charging.The charging of injection tangentially enter in the reactor 4 and with high temperature air/vapor mixing from grid 5.Tangential injection can increase the residence time of liquid and/or thin charging.Carry mobile gas secretly by top fixed bed grid 8, before leaving gasifier, enter reactor 3 subsequently at outlet pipe 12.Injection port 19 should be positioned at the bottom of reactor 4 sieges, to increase the residence time.Usually, for the small evaporator device, the position of this injection port is inclined wall 17 top 10cm.

The described residence time can be controlled the angle of gasifier by injection rate and injection lance.

In preferred embodiment, gasifier wall is made of two-layer: outer steel shell, preferred 5.0mm is thick, and the inner fiber ceramic thermal barrier layer, preferred resistant to elevated temperatures high

quality pottery.Wall

13 and 14 used potteries can promptly tolerate the highest 1400 ℃ temperature preferably with the highest 1400 ℃ temperature operation.The material that is fit to can be by Al ₂O ₃45%, SiO ₂36%, Fe ₂O ₃, 0.9% and CaO 16% form.The pottery that is used for 15,16 and 17 wall preferably can move under 1400-1500 ℃ higher temperature.The working temperature that the maximum of this wall material allows is 1600 ℃.The material that is fit to can have following composition: Al ₂O ₃61%, SiO ₂26%, Fe ₂O ₃0.5%, CaO 2.6%, ZrO22.95% and BaO 3.3%.Stupalith is supported by box hat.

In preferred embodiment, use fire-resistant (refractive) vitrified pipe as grid 8 and 5.The composition of these vitrified pipes can be for example 97%ZrO ₂With 3% MgO.

Via the high-temperature steam of pipeline 9 chargings, optional mixture, enter the throat 18 that is positioned at grid 5 belows with air or oxygen.This hot mixture of air and steam can remain on molten state with the ash content in the throat 18, and this ash content is finally fallen into bottom 6, and can take out off and on.

Embodiment 1:

Under the room temperature (15 ℃), be fed in first reactor via inlet 2 by the wood substance grain 1 of gravity with the 97kg/h of the about 8mm of diameter.The character of wood substance grain is as shown in table 1.

The component of the used charging of table 1 and ultimate analysis

Proximate analysis
			Wood substance grain (WP)
Total moisture (SS187170)	8％
		Ash oontent (SS-187171)	0.5-0.6% (doing)
LHV(SS-ISO562)	(17.76MJ/kg when receiving)
		Volatile matter (SS-ISO)	84% (doing)
Density	630-650kg/m ³
		Ultimate analysis (drying composition)
	Wood substance grain
		Sulphur (SS-187177)	S?0.01-0.02％
Carbon (Leco-600)	C?50％
		Hydrogen (Leco-600)	H?6.0-6.2％
Nitrogen (Leco-600)	N＜0.1％
		Oxygen (calculated value)	O?43-44％
Ash content melt temperature (oxidizing condition)
			Wood substance grain
Begin distortion, IT	1350-1400℃
		Softening, ST	1450-1500℃
Hemisphere, HT	1500℃
		Fluid temperature (F.T.), FT	1500-1550℃

Embodiment 2

Waste material derivatived fuel (RDF) with the 60kg/h of the about 8mm of diameter, by the granule type fuel made from other material such as fabric fibre, wood chip and plastics blended paper fiber as charging, and at room temperature (15 ℃) (promptly by action of gravity) is fed in first reactor 3 from top 1 by weight.RDF particulate character is as shown in table 2.

The component and the ultimate analysis of the used RDF charging of table 2

Proximate analysis
			Waste material derivatived fuel (RDF)
Total moisture (SS187170)	2.9％
		Ash oontent (SS-187171)	6.0% (doing)
LHV(SS-ISO562)	(26.704MJ/kg when receiving)
		Volatile matter (SS-ISO)	84.4% (doing)
Density	472kg/m ³
		Ultimate analysis (drying composition)
	RDF
		Sulphur (SS-187177)	S?0.09％
Carbon (Leco-600)	C?63.3％
		Hydrogen (Leco-600)	H?8.9％
Nitrogen (Leco-600)	N?0.3％
		Oxygen (calculated value)	O?20.95％
Ash content melt temperature (oxidizing condition)
			RDF
Begin distortion, IT	1210℃
		Softening, ST	1220℃
Hemisphere, HT	1230℃
		Fluid temperature (F.T.), FT	1240℃

Claims

1. be used for being produced by thick carbon-containing feeding the two stage gasification device (21) of synthetic gas and optional gac, this gasifier comprises:

-be equipped with the inlet (2) that is used for thick carbon-containing feeding (1) and be used for steam first the inlet (7) first reactor (3); And

-be equipped with and be used for steam, optional with air or oxygen, second reactor (4) of second inlet (9);

-and the outlet (12) that is used for synthetic gas;

Wherein said first and second reactors are had the crevice (20) of the cross section that reduces and are separated, this crevice is used to limit the circulation of unreacted solid carbonaceous substance from first reactor to second reactor, wherein said first reactor can move under at least 600 ℃ temperature, and wherein said second reactor can move under higher temperature, it is characterized in that, described second reactor (4) is the bottom reactor, described first reactor (3) is a upper reactor, be equipped with grid (8) in the bottom of first reactor, inlet (7) is set to close on the bottom of described first reactor, thereby the pre-hot steam of temperature at least 700 ℃ can be fed to described first reactor from grid (8) below via inlet (7), described second reactor is equipped with the inlet (19) that is used for thin solid carbon charging and/or liquid carbon-containing charging, inlet (9) is set to close on the bottom of described second reactor, thereby can be at least 700 ℃ pre-hot steam with temperature, optional preheated air or oxygen with uniform temp, be fed to described second reactor from the below via inlet (9), and be equipped with second crevice (18) with the cross section that reduces in the bottom of described second reactor (4).

2. two stage gasification device according to claim 1, wherein one or more, and preferably all described inlets (7,9,19) all have circular in the corresponding section (20,18,16) of described gasifier of cross section tangentially enter in the described gasifier.

3. two stage gasification device according to claim 1 and 2, wherein said inlet (19) comprise the inlet (19a, 19b) that at least two apart maximum distances of the circumference along described circular cross section distribute.

4. using to have two reactors, is respectively first and second reactors, the two stage gasification device thick carbon-containing feeding that gasifies, to produce synthetic gas and optional process of active carbon, comprise the steps:

(a) thick carbon-containing feeding is fed in first section reactor of gasifier;

(b) under at least 600 ℃ reactor service temperature, make steam in first section reactor of described thick carbon-containing feeding contact, realizing the gasification of described carbon-containing feeding,

It is characterized in that, feeding oxygen in described first section reactor not, and only feeding temperature be at least 700 ℃ pre-hot steam, and optional in any solid of step (b) gained and/or the second section reactor that the liquid carbon-containing material moves under the temperature at least 700 ℃ contacted, with the pre-hot steam of air or oxygen to obtain the arbitrary combination of following product: gac; CO; CO ₂, and the combustion heat.

5. method according to claim 4 comprises another step (d), wherein thin solid carbon of feeding or liquid carbon-containing charging in second section reactor of gasifier simultaneously.

6. according to claim 4 or 5 described methods, wherein in step (c), the steam that enters second section reactor is preheated to 700-1600 ℃ temperature, and preferred 800-1200 ℃.

7. each described method among the claim 4-6 is wherein selected the steam/air used in the step (c) or the ratio of steam/oxygen gas, thereby internal-combustion is minimized, and the yield of maximization CO and/or gac.

8. according to each described method among the claim 4-7, wherein use the oxygen replaces air.

9. according to each described method among the claim 4-6, wherein not to described gasifier supply air or oxygen.