CN202849349U - Dry pulverized coal graded compression gasification device - Google Patents
Dry pulverized coal graded compression gasification device Download PDFInfo
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- CN202849349U CN202849349U CN 201220259973 CN201220259973U CN202849349U CN 202849349 U CN202849349 U CN 202849349U CN 201220259973 CN201220259973 CN 201220259973 CN 201220259973 U CN201220259973 U CN 201220259973U CN 202849349 U CN202849349 U CN 202849349U
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Abstract
The utility model discloses a dry pulverized coal graded compression gasification device. A first burner chamber with an overhead process burner inside is arranged on the top of the device, a second burner chamber with a lateral process burner inside is arranged on the lateral side of the upper part of the device along the peripheral direction, and a discharge port is formed at the bottom of the device; and the upper end of a synthetic gas cooling chamber is provided with a plurality of shock gas inlets, an inner cylinder membrane type water cooling wall, an outer cylinder membrane type water cooling wall and a screen type water cooling wall. According to the dry pulverized coal graded compression gasification device, the service life of the lining of the furnace body can be prolonged, and the actual operation flexibility can be enhanced.
Description
Technical field
The utility model relates to a kind of gasification reactor apparatus, particularly relates to a kind of dry pulverized coal classification pressurized gasification reaction unit.
Background technology
Coal Gasification Technology is the basis of the process industrials such as development coal-based chemicals, coal-based liquid fuel, combined cycle generation, hydrogen manufacturing, is gordian technique and the leading technology of these industries.
Existing can be with carbonaceous fuel gasifyings such as coal, Jiao, in the technology that adopts air flow bed to gasify, representational dry coal powder gasification technology mainly contains: many burners opposed type dry coal dust gasification furnace, the Shell gasifier of the exploitation of the units such as China East China University of Science, and the double-section dry coal powder gasifying furnace of GSP vapourizing furnace and Inst. of Pyrology, State Electric power Corp..
Single stove processing power of single fire mouth overhead type dry coal dust gasification furnace of the prior art is less, such as the GSP vapourizing furnace.Because the turbulence intensity of top jet is higher, exist partial material short circuit and formation than the phenomenon of large stream recirculating zone, and adopt the top enter material way, burning, gasification reaction concentrate on the top area of gasification reactor chamber.Usually this regional temperature is higher, and stove inner top furnace wall material is owing to bearing washing away of backflow material under the high temperature, and its work-ing life is shorter, affects long-term operation.Yet many burners opposed type dry coal dust gasification furnace of East China University of Science is owing to adopting the collision type charging, and still there is larger threat in the upwards impinging flame that bump produces to furnace wall, the top material of vapourizing furnace.Shell gasifier and double-section dry coal powder gasifying furnace all adopt coal gas and molten state slag to be countercurrent flow, and its subject matter is that the molten state slag is discharged vapourizing furnace downwards by gravity under the reverse holder power effect of air-flow, very easily the frozen plug cinder notch.
There are two subject matters at present dry coal dust gasification furnace operation: the one, and temperature control problem in the vapourizing furnace; The 2nd, the cooling of gasification product and high temperature purification process.
Because the response behaviour in can't the manual control vapourizing furnace, so that temperature distribution and air-flow condition in the stove are unreasonable.And under the historical background of energy-conserving and environment-protective, adopt the water washing process for cooling to process the gasification product with high-order sensible heat, there is the low problem of efficiency of energy utilization.Therefore, domestic and international many researchists attempt developing the synthetic gas heat recovery technology that is applicable to the coal gasification course generation, adopt the radiation waste pot to add the technique of bottom water Quench such as US Patent No. 20080041572, energy recovery part gasification product sensible heat, but radiation section directly adopts screen formula water wall in the radiation waste pot, the stifled slag of screen formula water wall slagging scorification very easily occurs, affect its long-term operation, follow the bottom water Quench, complex process, the usage on black water amount is also larger.
The typical process flow that Xie Er gasifies adopts in top of gasification furnace exit low temperature synthetic gas Quench, again through after the membrane wall heat transfer cooling, enters the useless pot of synthetic gas conduit inflow convection current and carries out further cooling process.Because synthetic gas is carried a large amount of flying dusts secretly and is entered syngas cooler, easily form dust stratification at its water wall, affect heat-transfer effect, and it has adopted two heat-exchange equipments, syngas cooler huge structure, manufacturing cost are high, manufacturing cycle is long, and the I﹠M difficulty is larger, and has the problems such as floor space is large.
Therefore, developing the extensive high-efficiency gasification technology that temperature can be regulated and control flexibly, the gasification product sensible heat is utilized effectively in a kind of stove, is one of gordian technique approach that improves coal in China gasification technology reliability.
The utility model content
The technical problems to be solved in the utility model is can't regulate and control flexibly in order to overcome in the prior art in the vapourizing furnace temperature, and the defective that is not utilized effectively of gasification product sensible heat, and a kind of dry pulverized coal classification pressurized gasification reaction unit is provided.
The utility model solves above-mentioned technical problem by following technical proposals: a kind of dry pulverized coal classification pressurized gasification reaction unit, it comprises a furnace shell, from top to bottom coaxial arrangement has a gasification reactor chamber, a synthetic gas cooling room and a bottom slag bath in described furnace shell, and its characteristics are:
The top of described gasification reactor chamber is provided with first a burner chamber that is built-in with an overhead process burner, the upper side of described gasification reactor chamber is provided with one deck the second burner chamber in the circumferential direction of the circle, and at the indoor layout one side process burner of each described second burner, bottom at described gasification reactor chamber also is provided with cinder notch, be communicated with described synthetic gas cooling room by described lower cinder notch, the inwall of described gasification reactor chamber adopts membrane wall.
The upper end of described synthetic gas cooling room is provided with several Quench gas entrances, be provided with an inner core membrane wall in the described synthetic gas cooling room, one urceolus membrane wall also is set between described synthetic gas cooling room and described furnace shell, and a screen formula water wall is set between described inner core membrane wall and described urceolus membrane wall.
Be equipped with corresponding water wall header on described membrane wall, described inner core pattern water wall, described urceolus pattern water wall and the described screen formula water wall.
Wherein, the long service life of membrane wall, serviceability is high.The indoor part spiral coil cooling tube that arranges of described the first burner can play the effect of protection overhead process burner.
Preferably, the water wall form that described lower cinder notch adopts coil tube type water wall and shell and tube water wall to combine, described the first burner chamber opening and straight section on the described gasification reactor chamber partly adopt the shell and tube water wall.
Herein; the described first burner chamber opening on gasification reactor chamber top and straight section partly adopt the cooling of shell and tube water wall to be conducive to protect top of gasification furnace furnace wall material; lower cinder notch adopts coil tube type and the combination of shell and tube water wall to be beneficial to processing and to realize slag tap; and both interludes also adopt the shell and tube water wall, and it is conducive to slag and flows downward.
In addition, arranging of several Quench gas entrances can make slag namely be solidified by Quench at synthetic gas cooling room head inlet zone effectively.
Preferably, described coil tube type water wall, described shell and tube water wall and described membrane wall are that cantilevered or lateral support formula are installed in the described gasification reactor apparatus.
Preferably, described the first burner chamber, described gasification reactor chamber and described synthetic gas cooling room are coaxial setting, and the vertical range of described the second burner chamber and described the first burner chamber lower edge is the 10%-30% of the straight section Partial Height of described gasification reactor chamber.
This structure can satisfy the needs of temperature distribution in the stove effectively, too toply will make the furnace roof overtemperature, will make too on the lower the residence time of material in stove too short.
Preferably, described side process burner is deflection radially, and radially skew direction is consistent with angle excursion, and described angle excursion is 4 °-6 °.
Described process burner adopts the same level face to be evenly arranged, and radially has identical drift angle, utilizes radially the circle of contact to arrange and can avoid clashing into the up and down percussion flow thigh of generation, realizes rational flow field.The whirlpool that is formed by circle of contact jet can entrainment the top area material effectively, thereby the second gasification reaction occurs, and the residence time of material in stove is greatly improved.Make so the indoor temperature distribution of gasification reaction more reasonably also improve simultaneously efficiency of carbon conversion and cold gas efficiency.
Preferably, at least a portion of described the first burner chamber is provided with spiral coil cooling tube and a fire-resistant packing layer.
Preferably, the opening of described the first burner chamber is truncated cone-shaped or dome-shaped.
Preferably, it is indoor that described process burner adopts mechanical system to be installed on described the second burner, and plane, described process burner place is vertical with the wall of described gasification reactor chamber.
Preferably, described mechanical system is welding or flange connection.
Wherein, described gasification reactor chamber and described synthetic gas cooling room be vertical and coaxial being connected in the furnace shell from top to bottom, herein for the ease of making and installing, described gasification reactor chamber and described synthetic gas cooling room can be divided into two parts in furnace shell, can connect by flange in the middle of during installation, this flange connection is convenient to assembly and disassembly more.
Preferably, the height of the straight section of described gasification reactor chamber part is 3 with the diameter ratio: 1-8: 1.This structure can guarantee rational flow field effect, and helping simultaneously to keep the superfacial velocity of raw gas in gasification reactor chamber is 0.5m/s-2.5m/s.So-called superfacial velocity is exactly the ratio of volume and sectional area, by the control superfacial velocity material is kept the rational residence time in stove.
Preferably, the indoor described film-type water-cooling wall surface of described gasification reaction is equipped with a high-temperature flame-proof layer.
Preferably, the material of described high-temperature flame-proof layer comprises SiC and/or Al
2O
3, the thickness of described high-temperature flame-proof layer is 2mm-30mm.
In addition, described high-temperature refractory also can be selected SiC and/or Al
2O
3Deng matrix material, thereby play the effect of protection water wall tube wall material.
Preferably, the bottom of described synthetic gas cooling room is provided with a slag-drip opening that is communicated with described bottom slag bath, and the side that is positioned at the described furnace shell in the described synthetic gas cooling room outside is provided with a syngas outlet.
Described syngas outlet can be used for discharging synthetic gas, and its diameter value should make the apparent velocity of synthetic gas remain on 15m/s-30m/s.
Preferably, the number of described screen formula water wall is 4-40, and is evenly arranged along the central axis of described synthetic gas cooling room is coaxial.
Preferably, the number of described screen formula water wall is 10-20, and the height of described screen formula water wall is that the medullary ray of described syngas outlet is to the 50%-100% of the vertical range of the bottom of described inner core membrane wall.
Arrange that screen formula water wall will increase the water wall heat interchanging area, highly arrange and can design according to actual cooling requirement herein.Screen formula water wall width according to the synthetic gas cooling room inside and outside with between the annular space spatial design, its number can require control according to process for cooling.
Preferably, coil tube type water wall or shell and tube water wall are adopted in upper reducing place of described synthetic gas cooling room.
Preferably, the angle of inclination of the lower cinder notch of described gasification reactor chamber is 25 °-60 °.What gasification reactor chamber described herein adopted is the slag tap mode, and it is 8m/s-15m/s that described lower cinder notch interior diameter should keep the superfacial velocity at synthetic gas cinder notch place under gasification reactor chamber.
In gasification reactor chamber provided by the utility model, except coil tube type water wall and method that the shell and tube water wall combines were adopted in described lower cinder notch zone, the shell and tube water wall was all adopted in other zones (comprising the straight section of described gasification reactor chamber cylindrical shell and the reducing section of described lower cinder notch etc.).And the shell and tube water wall can adopt top cantilevered or lateral support formula, and the lateral support unit is arranged on up and down two parts of described the second burner chamber, arranges along even circumferential.
Preferably, the described Quench gas that is positioned at the ingress of described synthetic gas cooling room enters the opening's edge annulus and is evenly arranged, and the direction of described Quench gas entrance and the axis angle of described gasification reactor apparatus are 5 °-60 °, and the number of described Quench gas entrance is 4-80.
Wherein, Quench gas can adopt water vapor, CO
2, N
2, the dustless gas such as the low temperature clean synthetic gas of pump around circuit or its mixture.
As mentioned above, whole dry pulverized coal classification pressurized gasification reaction unit is divided into the gasification reactor chamber on top and the synthetic gas cooling room of bottom.The high-temperature gasification product that produces after the gasification is cooled off and rough purification in described synthetic gas cooling room, membrane wall and screen formula water wall that its heat is synthesized in the gas cooling room again absorb for generation of water vapor, reclaimed like this and be equivalent to the heat of raw coal net calorific value more than 10%, can make overall thermal coal gas efficient reach approximately 95%, improve 4-5 percentage point than the chilling process efficiency of energy utilization of identical gasifying process.
The method that the synthetic gas cooling room of gasification installation that the utility model provides adopts gas Quench, radiation heat transfer formula membrane wall and convective heat exchange formula screen formula water wall to combine is with radiation waste pot commonly used in the engineering reality and the useless pot of convection current organic combination.When the high-order sensible heat that makes gasification product obtains efficient recovery, greatly reduced heat-exchange equipment size and floor space, saved investment, adopt the gas chilling technology to strengthen operation controllability and the reliability of whole synthesis gas process.Substantially occur without chemical reaction in the syngas cooler, synthetic gas cooling and slag process of setting are realized by Physical temperature-lowering.During operation, high-temperature synthesis gas is being carried slag secretly and is being entered syngas cooler along lower cinder notch, and at inlet zone by low temperature Quench gas Quench, slag is frozen into rapidly the grey solid impurity particle of Watch glass attitude, flow downward with synthetic gas, the heat of synthetic gas is further taken away by the water in the inner core water wall tube by the mode of radiative transfer, lime-ash is finally thoroughly solidified falls into slag bath, synthetic gas is met to turn back behind the slag bath liquid level and is entered annular space between syngas cooler inner core water wall and urceolus water wall, and shielded the formula water wall in the mode of transmission of heat by convection and further lower the temperature, finally flow out from gasification installation housing side exit.
In the utility model, but above-mentioned optimum condition arbitrary combination on the basis that meets this area general knowledge namely gets each preferred embodiment of the utility model.
Positive progressive effect of the present utility model is: the utility model dry pulverized coal classification pressurized gasification reaction unit and gasification process thereof have adopted the classification gasification technology, make top of gasification furnace need not bear strongly washing away of high temperature gas flow, prolong the work-ing life of furnace lining, but and can make vapourizing furnace inner compartment temperature Effective Regulation by the classification gasification technology, strengthened actually operating elasticity.
Description of drawings
Fig. 1 is the structural representation of the utility model dry pulverized coal classification pressurized gasification reaction unit.
Fig. 2 is the structural representation of synthetic gas cooling room in the utility model dry pulverized coal classification pressurized gasification reaction unit.
Fig. 3 is the schema of the gasification process of the utility model dry pulverized coal classification pressurized gasification reaction unit.
Fig. 4 when adopting respectively single fire mouth overhead type gasification reactor apparatus and the utility model dry pulverized coal classification pressurized gasification reaction unit, the indoor axis temperature distribution contrast of corresponding gasification reaction schematic diagram.
Embodiment
Provide the utility model preferred embodiment below in conjunction with accompanying drawing, to describe the technical solution of the utility model in detail.
Shown in Fig. 1-2, the utility model dry pulverized coal classification pressurized gasification reaction unit, it is set to a upright round tube type in the present embodiment, and it comprises a furnace shell 1, and from top to bottom coaxial arrangement has a gasification reactor chamber 2, a synthetic gas cooling room 3 and a bottom slag bath 5 in furnace shell 1.
The top of gasification reactor chamber 2 is provided with one first burner chamber 11, and at the first burner chamber 11 interior overhead process burners 111 that arrange.Simultaneously, be provided with in the circumferential direction of the circle one deck the second burner chamber 21 in the upper side of gasification reactor chamber 2, and at each the second burner chamber 21 interior layout one side process burner 211.One deck the second burner chamber 21 comprises that several are evenly distributed on the second burner chamber 21 of gasification reactor chamber 2 sides, so that side process burner 211 is arranged symmetrically with.Wherein overhead process burner 111 and side process burner 211 adopt respectively mechanical system to be installed in the first burner chamber 11 and the second burner chamber 21, for example welding or adopt flange 4 to connect, and the wall with gasification reactor chamber 2 is vertical respectively on the plane at overhead process burner 111 and side process burner 211 places.Also be provided with cinder notch 23 in the bottom of gasification reactor chamber 2, be communicated with synthetic gas cooling room 3 by lower cinder notch 23, and the inwall of gasification reactor chamber 2 adopts membrane wall.Herein, lower cinder notch 23 is preferably cinder notch under the taper, and its angle of inclination is preferably 25 °-60 °.Especially, the water wall form that lower cinder notch 23 adopts coil tube type water wall and shell and tube water wall 222 to combine, and the first burner chamber 11 openings on the gasification reactor chamber 2 adopt shell and tube water wall 112, and straight section partly adopts shell and tube water wall 22.
In addition, side process burner 211 adopts the little circle of contact to arrange, has avoided the generation of impinging flame.Flame directly touches wall in the time of simultaneously also can preventing from adopting the wide-angle circle of contact.Owing to adopting the steam coal of top burner pan feeding than controlled design, can effectively carry out parameter adjustment according to running statuses such as the indoor temperature fluctuations of gasification reaction in real time, promoted the overall operation reliability and stability.
Usually, the working pressure in the gasification reactor chamber 2 is set as 1.5MPa ~ 8MPa, and the membrane wall of gasification reactor chamber 2 only can bear than small pressure difference.Therefore the cavity 12 that consists of between membrane wall and the furnace shell 1 in the gasification reactor chamber 2 needs to adopt rare gas element to fill (such as N
2, Ar etc.), make the pressure in the cavity 12 little greater than the pressure in the gasification reactor chamber 2, can prevent that like this synthetic gas from scurrying into cavity 12, also play heat insulation and effect anti-leak protection housing metal simultaneously.
The upper end of synthetic gas cooling room 3 is provided with several Quench gas entrances 36, in synthetic gas cooling room 3, be provided with an inner core membrane wall 32, one urceolus membrane wall 33 also is set between synthetic gas cooling room 3 and furnace shell 1, and a screen formula water wall 34 is set between inner core membrane wall 32 and urceolus membrane wall 33.In addition, be equipped with corresponding water wall header 35 at described membrane wall, inner core pattern water wall 32, urceolus pattern water wall 33 and screen formula water wall 34.In addition, be provided with a slag-drip opening 51 that is communicated with bottom slag bath 5 in the bottom of synthetic gas cooling room 3, the side that is positioned at the furnace shell 1 in synthetic gas cooling room 3 outsides is provided with a syngas outlet 31.
Wherein, the number of screen formula water wall 34 is 4-40, and is evenly arranged along the central axis of synthetic gas cooling room 3 is coaxial.More preferably 10-20 of the number of screen formula water wall 34, the height of screen formula water wall 34 are that the medullary ray of syngas outlet is to the 50%-100% of the vertical range of the bottom of described inner core membrane wall.For convenient install, inspection and maintenance, on the furnace shell of integrated gasification reaction unit, one or more manholes can also be set, for example can near the middle and upper part of synthetic gas cooling room 3 or middle and lower part, the manhole (not shown) be set.
In addition, the Quench gas entrance 36 that is positioned at the ingress of synthetic gas cooling room 3 is evenly arranged along annulus, and the axis angle of the direction of Quench gas entrance 36 and gasification reactor apparatus 2 is 5 °-60 °, and the number of Quench gas entrance is preferably 4-80.
Preferably, coil tube type water wall or shell and tube water wall 37 are adopted in upper reducing place of synthetic gas cooling room 3.Above-mentioned described coil tube type water wall, described shell and tube water wall and described membrane wall all can adopt cantilevered or lateral support formula to be installed in the described gasification reactor apparatus.
Further, the first burner chamber 11, gasification reactor chamber 2 and synthetic gas cooling room 3 are coaxial setting, and the vertical range of the second burner chamber 21 and the first burner chamber 11 lower edges is the 10%-30% of the straight section Partial Height of gasification reactor chamber 2.Side process burner 211 is deflection radially, and radially skew direction is consistent with angle excursion, and described angle excursion is 4 °-6 °.
Preferably, at least a portion of the first burner chamber 11 is provided with spiral coil cooling tube and a fire-resistant packing layer.The opening of the first burner chamber 11 is truncated cone-shaped or dome-shaped.
Further, the height of the straight section of gasification reactor chamber 2 part is 3 with the diameter ratio: 1-8: 1.Described film-type water-cooling wall surface in the gasification reactor chamber 2 is equipped with a high-temperature flame-proof layer.The material of described high-temperature flame-proof layer comprises SiC and/or Al
2O
3, the thickness of described high-temperature flame-proof layer is 2-30mm.
As shown in Figure 3, the utility model also provides a kind of gasification process that adopts aforesaid dry pulverized coal classification pressurized gasification reaction unit, and it specifically may further comprise the steps:
Step 100 passes into oxygen, gas or liquid fuel at the top of described gasification reactor apparatus, and described gasification reactor apparatus is carried out thermal pretreatment.
Step 101 sprays into a gasification reactor chamber with vaporising fuel, water vapour and oxygen by an overhead process burner, carries out incomplete gasification reaction.Wherein, described incomplete gasification reaction forms a cold zone, and described cold zone is 1000 ℃-1250 ℃ the non-slag of low temperature or half slag zone.
Step 102 passes into oxygen or oxygen rich gas and water vapour in the process burner of described side, with the reaction that is gasified totally through the logistics behind the described incomplete gasification reaction.Wherein, in required described oxygen or the described oxygen rich gas oxygen content more than or equal to 21%.
Wherein, form a high-temperature zone after above-mentioned be gasified totally reaction and the reaction of above-mentioned second gasification, described high-temperature zone is 1300 ℃-1600 ℃ full-fusing zone.
Step 106 is discharged described synthetic gas cooling room with synthetic gas, and lime-ash enters described bottom slag bath.
Can mainly finish following gasification by above-mentioned gasification process: dry pulverized coal, water vapor are sent into respectively the overhead process burner 111 of gasification reactor chamber 2 according to the steam coal ratio of setting.Oxygen or oxygen-rich air are sent into by the side process burner 211 of gasification reactor chamber 2, in gasification reactor chamber 2 interior generating gasification reactions, form thus 1000 ~ 1250 ℃ the non-slag of low temperature or half slag zone at the headspace of gasification reactor chamber 2.The coal dust devolatilization that sprays into from overhead process burner 111, and entrainment downwards behind the partial gasification under the effect of air-flow and enter the second gasification reaction zone, mix with the material rotational flows such as carbonic acid gas, water vapor and partial oxidation that produce after 211 partial combustions of side process burner and to carry out the second gasification reaction, form 1300 ℃ ~ 1600 ℃ of high-temperature zones.Middle thermal-flame district even surpass 2000 ℃, this moment, lime-ash was in complete molten state in this zone, and wall forms stable fluidised bed slag, and the molten state lime-ash flows downward with synthetic gas along wall.Gasification product enters synthetic gas cooling room 3 by lower cinder notch 23, and after the head of synthetic gas cooling room 3 was by Quench gas Quench, syngas outlet flowed out from the side after inner core membrane wall 32, urceolus membrane wall 33 and 34 heat exchange of screen formula water wall.And grey solid impurity particle flows downward after inlet zone is solidified by Quench, the solid ash solid impurity particle that most grey solid impurity particles are hunted down and solidify to form vitreous state when contact slag bath liquid level, and from slag-drip opening 51 discharges.
Fig. 4 is when adopting respectively single fire mouth overhead type gasification and gasification process described in the utility model, and the contrast of gasification reaction chamber axis temperature distribution is illustrated.As seen from Figure 4, under identical dry pulverized coal treatment capacity condition, the gasification reactor chamber top area temperature (shown in curve A among Fig. 4) of single fire mouth overhead type gasification obviously heats up very fast, and temperature is higher.And when adopting gasification installation provided by the utility model to carry out gasification reaction (shown in curve B among Fig. 4), the indoor high-temperature zone of gasification reaction moves down, away from headspace, the high-temperature zone just appears on process burner plane, side, realized the transformation of non-slag-slag process.Can effectively reach like this protection membrane wall of " with the slag anti-slag ", the overall operation efficiency of gasification installation and reliability are improved.
Above-mentioned dry coal powder gasification method is that dry pulverized coal is sent into respectively the side process burner by pressurization Dense Phase Pneumatic Conveying mode, and delivery medium can be CO
2, N
2Deng gas.Required oxygen or oxygen rich gas (O gasify
2〉=21%) all sends into by described side process burner, the required water vapor that gasifies is sent into by described side process burner, and recently realizes temperature distribution in gasification reaction mode control in the vapourizing furnace and the definite stove by the steam coal of regulating described overhead process burner pan feeding.In this gasification, steam plays preferably temperature adjusting effect.
Gasification process described in the utility model adopts sends into a small amount of oxygen in the overhead process burner, make vaporising fuel be in incomplete gasification reaction, and then charging in the process burner of side, so that be in oxygen condition through the logistics behind the described incomplete gasification reaction, be that side burner pan feeding oxygen coal is than required far above gasification, therefore the reaction of generating unit divided combustion.And the coal dust that the overhead process burner sprays into is after heat absorption and devolatilization occur in the gasification reactor chamber top, remaining material is mainly carbon black and semicoke particle, down flow process meets with the reaction product that the side burner sprays into and mixes, again generating gasification reaction, thus reach the effect that the gasification reactor chamber top area is lowered the temperature.Can be called the indoor temperature of chemical method regulation and control gasification reaction from principle.
Therefore, the utility model utilizes the classification gasification method that devolatilization, burning and the gasification of the indoor generation of gasification reaction are decomposed.In the gasification reactor chamber top area coal dust devolatilization process occurs mainly, be mainly combustion processes in process burner planar central zone, side, other zones are mainly the gasification reaction process.Set up the indoor differing temps district of gasification reaction by oxygen and water vapor distribution that the adjusting gasification reaction is indoor, optimized reaction conditions.Because gasification reactor chamber top area temperature is lower, the wall lime-ash is in non-melting or semi-melting state, below, described the second burner chamber wall lime-ash then is molten state, realized the indoor non-slag of gasification reaction-slag subregion, the slag discharge gasification reactor chamber that finally will gasify and produce in the slag tap mode.
The below is specifically described the utility model with a concrete example:
The dry pulverized coal classification pressurized gasification reaction unit of one cover day 3000 tons of coals of processing, the interior diameter of gasification reactor chamber housing is 4200mm.Overhead process burner of top layout at gasification reactor chamber sprays into 20% coal dust, 20% water vapor by the overhead burner.Its side is evenly arranged four side process burners of one deck, and process burner plane, side is vertical with the gasification reaction chamber axis, and radially angle excursion is 4.8 °, sprays into altogether 80% coal dust, 80% water vapor and 100% oxygen by four side process burners.It is basically identical that the raw coal of above-mentioned overhead process burner and side process burner is processed load.
The inner core water wall diameter of synthetic gas cooling room is set to 4500mm, highly is 25000mm, and urceolus water wall diameter is set to 6800mm, highly is 32000mm, and screen formula water wall height is 15000mm, and width is 800mm, along 16 of middle annular space circumference uniform distributions.
Can be obtained the analytical data (as shown in table 2) of coal analysis (as shown in table 1) and gasification reactor apparatus outlet synthetic gas by above-mentioned gasification reactor apparatus:
Table 1 coal analysis table
Other main operational conditions:
Service temperature: 1673K;
Working pressure: 4.0MPa;
Coal dust delivery of carrier gas medium: nitrogen;
Oxygen coal ratio: 0.48kg/kg;
Steam coal ratio: 0.3kg/kg;
Steam-in temperature: 623K;
Oxygen intake temperature: 298K;
Oxygen purity: 99.6%.
Gasification reactor apparatus outlet synthetic gas analytical data is:
Table 2 gasification installation outlet gas composition (Vol%) and lower cinder notch place temperature (K) data
| H 2 | CO | CO 2 | H 2O | CH 4 | H 2S | COS | N 2 | T |
| 29.95 | 59.67 | 2.28 | 3.87 | 0.31 | 0.50 | 0.01 | 3.41 | 1732 |
Gasification reactor apparatus outlet synthetic gas temperature: 612K;
Efficiency of carbon conversion: 99.2%;
Active constituent content (H in the coal gas
2+ CO): 92.3% (butt);
Gasification installation outlet synthetic gas flow: 225414Nm
3/ h;
Overall thermal coal gas efficient: 94.8%.
The high-temperature water temperature that enters synthetic gas cooling room membrane wall and screen formula water wall is 312 ℃, pressure 112MPa, and steam output is about 260t/h.Synthetic gas cooling room head Quench gas adopts low temperature synthetic gas circulation re-injection mode, and circulation ratio is about 20% of total synthesis gas yield.
The specific performance parameter of synthetic gas cooling room is as follows:
Heat lost by radiation:＜0.4%;
Available rate:〉95%;
Working pressure (tube side): 11.2atm;
Working pressure (shell side): 35atm.
In sum, the method that the synthetic gas cooling room of the utility model dry pulverized coal classification pressurized gasification reaction unit adopts gas Quench, radiation heat transfer formula membrane wall and convective heat exchange formula screen formula water wall to combine, with radiation waste pot commonly used in the engineering reality and the useless pot of convection current organic combination, when the high-order sensible heat that makes gasification product obtains efficient recovery, heat-exchange equipment size and floor space have greatly been reduced, save investment, adopted the gas chilling technology to strengthen operation controllability and the reliability of whole synthesis gas process.
In addition, substantially occur without chemical reaction in the synthetic gas cooling room, synthetic gas cooling and slag process of setting are realized by Physical temperature-lowering.During operation, high-temperature synthesis gas is being carried slag secretly and is being entered syngas cooler along lower cinder notch, and at inlet zone by low temperature Quench gas Quench, slag is frozen into rapidly the grey solid impurity particle of Watch glass attitude, flows downward with synthetic gas.Then, the heat of synthetic gas is further taken away by the water in the inner core water wall tube by the mode of radiative transfer, lime-ash is finally thoroughly solidified falls into slag bath, synthetic gas is met to turn back behind the slag bath liquid level and is entered annular space between syngas cooler inner core water wall and urceolus water wall, and shielded the formula water wall in the mode of transmission of heat by convection and further lower the temperature, finally flow out from gasification installation housing side exit.
The utility model has been introduced the theory of classification gasification dexterously, effectively solved the problem of the indoor regional area of gasification reaction furnace wall overtemperature, so that the high-temperature zone of top fuel gasification flame is away from the top wall of gasification reactor chamber, prolonged the work-ing life of gasification reactor chamber internal protecting wall material, is improved the work-ing life of overhead process burner.Also form thus non-slag-slag gasification, can realize smoothly the theory of " with the slag anti-slag ", effectively reduced the high temperature logistics to the oxidation corrosion of wall lining material, improved its work-ing life.And by the classification gasification technology whole efficiency of carbon conversion and the cold gas efficiency of gasification installation also are improved.
In addition, the utility model has also adopted the method for gas chilling technology, radiative transfer and transmission of heat by convection combination, the gasification product that will have high-order sensible heat in effective space cools off and rough purification, has reached the effect of synthetic gas waste heat recovery and rough purification.At synthetic gas cooling room inlet zone Quench gas is set, molten state lime-ash particle surface will be solidified rapidly, greatly reduce grey solid impurity particle touches the wall deposition in the process of flowing downward probability, namely greatly reduce the possibility of the stifled slag of water wall slagging scorification, improved the overall operation reliability of device, and make the device structure design more reliable through gathering, greatly reduced total floor space of device.
Although more than described embodiment of the present utility model, it will be understood by those of skill in the art that these only illustrate, protection domain of the present utility model is limited by appended claims.Those skilled in the art can make various changes or modifications to these embodiments under the prerequisite that does not deviate from principle of the present utility model and essence, but these changes and modification all fall into protection domain of the present utility model.
Claims (18)
1. dry pulverized coal classification pressurized gasification reaction unit, it comprises a furnace shell, from top to bottom coaxial arrangement has a gasification reactor chamber, a synthetic gas cooling room and a bottom slag bath in described furnace shell, it is characterized in that:
The top of described gasification reactor chamber is provided with first a burner chamber that is built-in with an overhead process burner, the upper side of described gasification reactor chamber is provided with one deck the second burner chamber in the circumferential direction of the circle, and at the indoor layout one side process burner of each described second burner, bottom at described gasification reactor chamber also is provided with cinder notch, be communicated with described synthetic gas cooling room by described lower cinder notch, the inwall of described gasification reactor chamber adopts membrane wall;
The upper end of described synthetic gas cooling room is provided with several Quench gas entrances, be provided with an inner core membrane wall in the described synthetic gas cooling room, one urceolus membrane wall also is set between described synthetic gas cooling room and described furnace shell, and a screen formula water wall is set between described inner core membrane wall and described urceolus membrane wall;
Be equipped with corresponding water wall header on described membrane wall, described inner core pattern water wall, described urceolus pattern water wall and the described screen formula water wall.
2. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1, it is characterized in that, the water wall form that described lower cinder notch adopts coil tube type water wall and shell and tube water wall to combine, described the first burner chamber opening and straight section on the described gasification reactor chamber partly adopt the shell and tube water wall.
3. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 2 is characterized in that, described coil tube type water wall, described shell and tube water wall and described membrane wall are that cantilevered or lateral support formula are installed in the described gasification reactor apparatus.
4. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1, it is characterized in that, described the first burner chamber, described gasification reactor chamber and described synthetic gas cooling room are coaxial setting, and the vertical range of described the second burner chamber and described the first burner chamber lower edge is the 10%-30% of the straight section Partial Height of described gasification reactor chamber.
5. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1 is characterized in that, described side process burner is deflection radially, and radially skew direction is consistent with angle excursion, and described angle excursion is 4 °-6 °.
6. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1 is characterized in that, at least a portion of described the first burner chamber is provided with spiral coil cooling tube and a fire-resistant packing layer.
7. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 6 is characterized in that, the opening of described the first burner chamber is truncated cone-shaped or dome-shaped.
8. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1 is characterized in that, it is indoor that described process burner adopts mechanical system to be installed on described the second burner, and plane, described process burner place is vertical with the wall of described gasification reactor chamber.
9. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 8 is characterized in that, described mechanical system is welding or flange connection.
10. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1 is characterized in that, the height of the straight section part of described gasification reactor chamber is 3:1-8:1 with the diameter ratio.
11. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1 is characterized in that, the indoor described film-type water-cooling wall surface of described gasification reaction is equipped with a high-temperature flame-proof layer.
12. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 11 is characterized in that the thickness of described high-temperature flame-proof layer is 2-30mm.
13. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 11, it is characterized in that, the bottom of described synthetic gas cooling room is provided with a slag-drip opening that is communicated with described bottom slag bath, and the side that is positioned at the described furnace shell in the described synthetic gas cooling room outside is provided with a syngas outlet.
14. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 13 is characterized in that, the number of described screen formula water wall is 4-40, and is evenly arranged along the central axis of described synthetic gas cooling room is coaxial.
15. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 14, it is characterized in that, the number of described screen formula water wall is 10-20, and the height of described screen formula water wall is that the medullary ray of described syngas outlet is to the 50%-100% of the vertical range of the bottom of described inner core membrane wall.
16. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 14 is characterized in that, coil tube type water wall or shell and tube water wall are adopted in upper reducing place of described synthetic gas cooling room.
17. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1 is characterized in that, the angle of inclination of the lower cinder notch of described gasification reactor chamber is 25 °-60 °.
18. dry pulverized coal classification pressurized gasification reaction unit as claimed in claim 1, it is characterized in that, the described Quench gas that is positioned at the ingress of described synthetic gas cooling room enters the opening's edge annulus and is evenly arranged, the direction of described Quench gas entrance and the axis angle of described gasification reactor apparatus are 5 °-60 °, and the number of described Quench gas entrance is 4-80.
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| CN 201220259973 CN202849349U (en) | 2012-06-04 | 2012-06-04 | Dry pulverized coal graded compression gasification device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220259973 CN202849349U (en) | 2012-06-04 | 2012-06-04 | Dry pulverized coal graded compression gasification device |
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| CN202849349U true CN202849349U (en) | 2013-04-03 |
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Cited By (8)
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| CN103173247A (en) * | 2013-04-12 | 2013-06-26 | 邰学林 | Compound type furnace body of slag coal gasification furnace |
| CN103351890A (en) * | 2013-07-19 | 2013-10-16 | 华东理工大学 | Washing cooling tube with flaring structure |
| CN104927924A (en) * | 2015-06-12 | 2015-09-23 | 西安元创化工科技股份有限公司 | Protrusion type partition reactor |
| CN104946311A (en) * | 2015-05-28 | 2015-09-30 | 中国寰球工程公司 | Semi-syngas cooler lower-chilling type powder coal gasification furnace |
| CN107216918A (en) * | 2017-04-01 | 2017-09-29 | 安徽科达洁能股份有限公司 | Gas generator |
| IT201600124642A1 (en) * | 2016-12-09 | 2018-06-09 | Site S P A Con Socio Unico | PLANT FOR THE TRANSFORMATION OF AN ORGANIC-BASED MATERIAL IN SYNTHESIS GAS |
| CN109504444A (en) * | 2018-11-19 | 2019-03-22 | 清华大学山西清洁能源研究院 | Oxygen classification gasifying furnace with radiation waste pot |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103173247A (en) * | 2013-04-12 | 2013-06-26 | 邰学林 | Compound type furnace body of slag coal gasification furnace |
| CN103351890A (en) * | 2013-07-19 | 2013-10-16 | 华东理工大学 | Washing cooling tube with flaring structure |
| CN103351890B (en) * | 2013-07-19 | 2015-04-22 | 华东理工大学 | Washing cooling tube with flaring structure |
| CN104946311A (en) * | 2015-05-28 | 2015-09-30 | 中国寰球工程公司 | Semi-syngas cooler lower-chilling type powder coal gasification furnace |
| CN104946311B (en) * | 2015-05-28 | 2018-03-16 | 中国寰球工程公司 | Chilling-type powder coal gasification furnace under a kind of half useless pot |
| CN104927924A (en) * | 2015-06-12 | 2015-09-23 | 西安元创化工科技股份有限公司 | Protrusion type partition reactor |
| IT201600124642A1 (en) * | 2016-12-09 | 2018-06-09 | Site S P A Con Socio Unico | PLANT FOR THE TRANSFORMATION OF AN ORGANIC-BASED MATERIAL IN SYNTHESIS GAS |
| WO2018104907A1 (en) * | 2016-12-09 | 2018-06-14 | Site S.P.A. Con Socio Unico | System for transforming an organic material into syngas |
| CN107216918A (en) * | 2017-04-01 | 2017-09-29 | 安徽科达洁能股份有限公司 | Gas generator |
| CN107216918B (en) * | 2017-04-01 | 2023-08-22 | 安徽科达洁能股份有限公司 | Gas producer |
| CN109504444A (en) * | 2018-11-19 | 2019-03-22 | 清华大学山西清洁能源研究院 | Oxygen classification gasifying furnace with radiation waste pot |
| RU2737833C1 (en) * | 2020-07-06 | 2020-12-03 | Игорь Владимирович Тихомиров | Autonomous electric generation method and device - small solid fuel power plant for its implementation |
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