CN203144353U - Jet pipe and fluidized bed reactor with jet pipe - Google Patents
Jet pipe and fluidized bed reactor with jet pipe Download PDFInfo
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- CN203144353U CN203144353U CN 201320045965 CN201320045965U CN203144353U CN 203144353 U CN203144353 U CN 203144353U CN 201320045965 CN201320045965 CN 201320045965 CN 201320045965 U CN201320045965 U CN 201320045965U CN 203144353 U CN203144353 U CN 203144353U
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Abstract
The utility model relates to a jet pipe and a fluidized bed reactor with the jet pipe. A plurality of jet pipes with dispersed bed layers are used for feeding oxygen. The jet pipes are in sleeve structures. A mixed gas of oxygen and overheat steam is fed in a central pipe. Hot steam flows in an annular space. The ratio of oxygen to overheat steam is adjusted to control the oxygen concentration in a certain range. Strong exothermic reaction is mainly generated in combustion of oxygen and carbon material in a jet region. Heat released is used in gasification reaction in a reactor. Overheat steam fed to the annular space can strengthen inner circulation of carbon material particles and performs heat exchange with high-temperature gas in a central pipe area, and also can provide heat for gasification and heat absorption reaction in the annular space. Local high temperature areas are avoided through fast heat exchange and heat absorption reaction, and the probability of scorification in the jet pipe area is reduced.
Description
Technical field
The utility model relates to the catalytic coal gasifaction technical field, relates in particular to a kind of jet pipe and has the fluidized-bed reactor of this jet pipe.The utility model is not only applicable to catalytic coal gasifaction technology, is equally applicable to logical oxygen metallization processes and coal and the common gasifying process of biomass of low ash smelting point, clinker(ing) coal.
Background technology
Increasingly stringent along with rapid economic development and environmental regulations, in the following more than ten years, China will be explosive growth to the demand of this clean energy of Sweet natural gas, though and gas production has and increases far below demand, imbalance between supply and demand becomes increasingly conspicuous, and the supply breach strengthens year by year.Characteristics in view of China's Energy resources situation " rich coal, few oil, deficency "; long term maintenance can not change in a short time based on the energy consumption structure of coal; development trend according to development of clean coal trend and world's low-carbon economy; coal is changed into top quality fuel-Sweet natural gas in the fossil energy, is to be fit to China's national situation, to dissolve energy dilemma and to guarantee a shortcut of energy security.
Common Coal Gasification Technology, namely coal at high temperature with oxygen (or air) and/or water vapor (H
2O) vaporized chemical of Zu Chenging carries out gasification reaction, generates to contain a small amount of methane (CH
4) synthetic gas (mainly being hydrogen, carbon monoxide and carbonic acid gas), carry out hydrosphere transformation and methanation operation afterwards, adopt two-step approach to prepare methane.This Coal Gasification Technology have the required temperature height of gasification reaction, energy consumption big, to the equipment requirements height, and need three reaction units, technology than shortcomings such as complexity.
The catalytic coal gasifaction technology is the clean efficient a kind of important way utilized of coal.Adopt the catalytic coal gasifaction technology, coal under relatively low temperature with water vapor (H
2O), hydrogen (H
2), the vaporized chemical formed of carbon monoxide (CO) carries out gasification reaction under the katalysis of catalyzer, generate the methane (CH of high density
4).The catalytic coal gasifaction technology is compared with other Coal Gasification Technology, has advantages such as the required temperature of methane content height, gasification reaction is low.
Existing catalysis gasification technique all adopts outer heat-supplying mode, U.S. EXXON, GPE company disclose this catalytic gasification technology, see patent US4318712, US2009246120A1, US2009165376A1, all need with a large amount of superheated vapours and cyclic part product gas carbon monoxide, hydrogen enters the heat release of vapourizing furnace generation methanation reaction that institute of system heat requirement is provided, adopting low temperature separation process, product gas partial oxidation or setting up combustion oxygen vapourizing furnace provides superheated vapour and CO, H
2, the energy consumption of technology is all bigger, the facility investment height, and the technical process complexity, steam superheating system and heat exchange system load are higher, to sum up cause the technology macroeconomic not good, and total efficiency is lower.
The mode that the small-scale development adopts outer heat supply to satisfy the required heat of gasification still can, and the mode that industrialization adopts outer heat supply to satisfy the required heat of gasification is invested huge, and be difficult on the engineering realize, need to adopt fire coal to provide institute's heat requirement from heat-supplying mode for the catalytic gasification reaction, keep furnace temperature in the certain reaction temperature, need not to append other equipment, technical process is simple, and Technological Economy is preferable.But the adding catalyst combustion reaction of catalyzer improves carbonaceous material burning thermal discharge, and the base metal catalysts of Tian Jiaing may form the low temperature fused matter with the coal mineral under certain process conditions, reaction atmosphere simultaneously, reduces the ash fusion point of coal; And catalysis gasification technique requires long gas-solid duration of contact, bed is higher relatively, full bed zone evenly flash heat transfer is difficult relatively, local temperature is too high in the bed causes the coal ash particle slagging scorification that bonds mutually, cause fluidized state bad, deslagging difficulty even defluidizationization etc. when serious cause reactor to be difficult to the continous-stable operation.
Fluidized-bed reactor is because its gas-solid mixes fully and advantage such as transfer efficiency height and be widely used in the gasification field.Industrialized U-gas vapourizing furnace, KRW and ash melt poly-vapourizing furnace and all adopt single efflux nozzle at present, i.e. one-jet fluidized-bed, and the gas-solid contact efficiency is low, easily forms the localized hyperthermia district and causes slagging scorification.
CN 1974733A discloses a kind of coal and the multi-jet composite fluidized bed gasification installation of biomass.Though it can provide higher gas-solid contact efficiency with respect to the one-jet fluidized-bed, but for higher jet fluidized-bed of bed, because of solid particulate back-mixing less turbulence more slow, a plurality of efflux nozzles are distributed in the localized hyperthermia that forms on the same horizontal plane and are difficult to be passed to fast full bed, also are easier to slagging scorification.
Present existing one-jet fluidized-bed and how jet fluidized-bed gasification installation, all exist the gas-solid contact efficiency low, easily form the problem that the localized hyperthermia district causes slagging scorification, especially for higher jet fluidized-bed of bed, because of solid particulate back-mixing less turbulence more slow, a plurality of efflux nozzles are distributed in the localized hyperthermia that forms on the same horizontal plane and are difficult to be passed to fast full bed, also are easier to slagging scorification.
The utility model content
The purpose of this utility model is at the existing jet fluidized-bed deficiency that is applied to the gasification field, proposes a kind of jet pipe and has the fluidized-bed reactor of this jet pipe.
The utility model adopts and disperses oxygen supply that reaction institute heat requirement is provided, oxygen enters reactor by a plurality of jet pipes of bed, guarantees that oxygen evenly distributes, by regulating water vapour, oxygen blending ratio control oxygen concn in certain limit, avoid occurring bed localized hyperthermia district, reduce the slagging scorification probability.
For reaching this purpose, the utility model by the following technical solutions:
One of the purpose of this utility model is to provide a kind of jet pipe, and described jet pipe is telescoping, comprises pipe core and around the outer tube of pipe core; Form annular space between described pipe core and the outer tube.
Jet pipe described in the utility model is formed by pipe core and outer tube suit, during application, the gas mixture of aerating oxygen and superheated vapour in pipe core, described oxygen and the thermopositive reaction of carbonaceous material generation catalyticcombustion, for the gasification reaction in the fluidized-bed reactor provides heat, realize coal-fired from heat supply; Because high calorie causes particles of carbonaceous material fusion slagging scorification easily, therefore in annular space, feed superheated vapour, strengthened the less turbulence in the pipe core zone of jet pipe, thereby strengthened the heat exchange degree of pipe core zone high-temperature medium, superheated vapour in the while annular space carries out thermal exchange with the gas mixture from pipe core, the timely heat that the pipe core exit region generation catalyticcombustion thermopositive reaction of jet pipe is produced in time changes away evacuation, reduces fluerics slagging scorification risk; Simultaneously, the superheated vapour in the annular space can accelerate C and H after heat exchange improves temperature
2The speed of the thermo-negative reaction of O is further led away heat, reduces fluerics slagging scorification risk more.
Described jet pipe is formed by connecting by horizontal section and vertical section; Preferably, the exit end of described outer tube is the ejector nozzle shape.The exit end of outer tube is designed to the ejector nozzle shape, can more effectively strengthens the interior medium of annular space with the heat exchange of fluerics high-temperature gas, strengthen the particles of carbonaceous material internal recycle, avoid the appearance in localized hyperthermia district, solve the slagging scorification problem better.
Two of the purpose of this utility model is to provide a kind of how jet fluidized-bed reactor, and described reactor adopts at least one aforesaid jet pipe as the bed distribution device.Above-mentioned jet pipe as the bed distribution device, not only can be realized coal-fired confession heat in the fluidized-bed reactor, and can be avoided the slagging scorification problem.
Bed distribution device described in the utility model is made of a plurality of jet pipes.The distribution form of described a plurality of jet pipe in fluidized-bed there is no particular form, and those skilled in the art can carry out equidistantly or the non-equidistance distribution according to practical situation.Same horizontal plane gas feeds a mouthful number and can be one or radially a plurality of, also axial distribution device can be set in bed, guarantees that whole bed oxygen is uniformly dispersed to get final product.For example can adopt following two kinds of forms that jet pipe is arranged:
(1) the two or more jet pipes of symmetrical distribution on the interior same horizontal plane of described reactor, the while arranges the jet pipe of multilayer symmetry arrangement vertically; Be that described bed distribution device is made up of a plurality of jet pipes that multilayer is symmetrically distributed vertically.
(2) a plurality of jet pipes are distributed in the reactor vertically with asymmetrical form, and namely described bed distribution device is made up of a plurality of jet pipes of asymmetric distribution vertically.
The concrete structure of reactor described in the utility model is as follows: described reactor comprises:
Reactor body, its inner chamber that forms;
The conical distribution plate is positioned at described reactor body bottom, and forms air chamber between the wall of reactor body bottom;
Feeding line runs through being arranged at reactor body top, with described chamber in fluid communication, enters in the described chamber for the material carbon material;
The vaporized chemical pipeline runs through being arranged at the reactor body bottom, is opened on air chamber, enters in the described chamber by the conical distribution plate for vaporized chemical;
The bed distribution device runs through the sidewall that is arranged at reactor body, with described chamber in fluid communication;
The discharging pipeline runs through being arranged at the reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product.
Reactor body described in the utility model has bearing capacity, can tolerate and keep the temperature and pressure in respective inner space, is made by pressure-resistant material.Described feeding line and vaporized chemical pipeline are used for described material is introduced the inside reactor chamber under certain pressure, mix laggard promoting the circulation of qi reaction.The gaseous product that described discharging pipeline is used for behind the gasification reaction is discharged reactor.Those skilled in the art can determine the number that above-mentioned respective lines is required according to practical condition, with better realization function separately, realize the purpose of this utility model.
In the utility model, the vaporized chemical pipeline is arranged at the bottom of reactor body, and the gas-solid two-phase is in the indoor abundant contact of reactor cavity, is beneficial to reach fluidized state.In addition, vaporized chemical is simultaneously as fluidizing medium, and gasification temperature is even in the reactor.Vaporized chemical is evenly distributed through the conical distribution plate by air chamber after entering from the vaporized chemical pipeline, enter again reactor cavity indoor with carbonaceous material carry out gasification reaction, can make to be reflected in the whole chamber and carry out simultaneously, raw material is taken full advantage of.
Reactor described in the utility model also comprises the deslagging pipeline, runs through described reactor body and conical distribution plate, is opened on described chamber, discharges reactor for the remaining semicoke after the gasification.In the utility model, carbonaceous material and vaporized chemical reactor cavity is indoor react after, gaseous product is discharged reactor from the discharging pipeline, the semicoke product that the gasification back produces is discharged reactor from the deslagging pipeline.
A kind of method of utilizing aforesaid fluidized-bed reactor to carry out catalytic coal gasifaction:
It is indoor to make carbonaceous material and vaporized chemical enter reactor cavity, vaporized chemical and the reaction of carbonaceous material generating gasification;
It is indoor to make carbonaceous material and vaporized chemical enter reactor cavity, vaporized chemical and the reaction of carbonaceous material generating gasification;
To the gas mixture as aerating oxygen and superheated vapour in the pipe core of the jet pipe of bed distribution device; Described oxygen and the thermopositive reaction of carbonaceous material generation catalyticcombustion are for gasification reaction provides heat;
In annular space, feed superheated vapour; Evacuate with the heat that the catalyticcombustion thermopositive reaction is produced;
The gaseous product that gasification reaction generates is discharged reactor from the discharging pipeline; Remaining semicoke is discharged reactor through the deslagging pipeline.
Catalytic coal gasifaction method described in the utility model is specific as follows:
The carbonaceous material of impregnated catalyst enters chamber of the reactor through feeding line, and vaporized chemical enters chamber of the reactor by air chamber through the vaporized chemical pipeline behind conical distribution plate gas distribution, and vaporized chemical and material carbon material be the generating gasification reaction under the effect of catalyzer;
As the pipe core aerating oxygen of the jet pipe of bed distribution device and the gas mixture of superheated vapour, feed superheated vapour in the annular space; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion are for gasification reaction provides heat; Superheated vapour in the annular space is strengthened jet pipe turbulence heat exchange, and the high-temperature gas with the pipe core zone carries out thermal exchange simultaneously, avoids the appearance in localized hyperthermia district;
The gaseous product that generates behind the gasification reaction is discharged reactor from the discharging pipeline, and remaining semicoke is discharged reactor through the deslagging pipeline.
Vaporized chemical described in the utility model is superheated vapour, or O
2, CO or H
2In a kind of or at least two kinds of mixed gass with superheated vapour.Typical but non-limiting example comprises superheated vapour, superheated vapour and O
2Combination, the combination of superheated vapour and CO, superheated vapour and H
2Combination, superheated vapour, CO and H
2Combination, superheated vapour, O
2, CO and H
2Combination etc., all can be used for implementing the utility model.
Preferably, the oxygen concentration in the described vaporized chemical is 0～20mol%, 0.2～18.9mol% for example, 3～16mol%, 5.5～14.6mol%, 7～12mol%, 9mol% etc., more preferably 0～10mol%.
Preferably, the steam that described superheated vapour is produced by boiler and gaseous product carry out thermal exchange and obtain, and temperature is 300～500 ℃ after the heat exchange; Preferably, the water carbon mol ratio of described vaporized chemical and carbonaceous material is 0.5～3:1,0.52～2.95:1 for example, 0.7～2.45:1,1.1～2.06:1,1.5～2:1,1.8:1 etc., preferred 1～2:1.
In the gas mixture that described pipe core feeds, oxygen concentration is by regulating the amount control of superheated vapour.Oxygen concentration≤30mol%, 0.1～29.6mol% for example, 0.75～26mol%, 1.2～24.3mol%, 4～21.7mol%, 8.6～18mol%, 10～16mol%, 13.4mol% etc., more preferably 5～20mol%.In the utility model, only need control steam and oxygen proportion to regulate oxygen concentration, lose the decision of enthusiasm condition as for logical how much oxygen of needs and water vapour by fluidized-bed, lose the hot more oxygen ability additional heat that needs to burn more, then need to feed more oxygen, some more jet pipes are set, but the water vapour of the vaporized chemical that the overall steam vapour amount that feeds feeds with respect to the vaporized chemical pipeline seldom.
Preferably, the superheat steam temperature that feeds in the described annular space is 300～500 ℃, for example 300.2～486 ℃, and 316～470 ℃, 330～453 ℃, 356～435 ℃, 370～413 ℃, 386 ℃ etc.
Preferably, the service temperature of gasification reaction is 600～800 ℃, for example 600.3～789.6 ℃, and 625～770 ℃, 645～748 ℃, 680～720 ℃, 695～703 ℃ etc., further preferred 750 ℃.Working pressure is 0～5MPa, 0.1～4.99MPa for example, 0.2～4.5MPa, 0.5～3.5MPa etc., further preferred 0.3～4MPa.
The composition of described gaseous product is CH
4, CO, H
2, CO
2, a spot of H
2S and NH
3And part entrained fines.Feed vaporized chemical in the deslagging pipeline, control bed drain purge by control tolerance size.
Under certain temperature, pressure condition, carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng and the part entrained fines discharge through the discharging pipeline from reactor top outlet.Principal reaction is as follows in the fluidized-bed reactor:
2C+2H
2O→2H
2+2CO （1）
CO+H
2O→CO
2+H
2 （2）
3H
2+CO→CH
4+H
2O （3）
C+2H
2→CH
4 （4）
2C+O
2→2CO （5）
C+O
2→CO
2 （6）
Remaining semicoke after the gasification is discharged reactor through the deslagging pipeline, feeds vaporized chemicals such as superheated vapour, carbon monoxide, hydrogen in the deslagging pipeline, and controls bed drain purge by the amount of control vaporized chemical.
Compare with the prior art scheme, the utlity model has following beneficial effect:
A plurality of jet pipes that the utility model adopts bed to disperse advance oxygen, and the jet pipe structure is telescoping, and the gas mixture of the logical oxygen of pipe core and superheated vapour by hot steam, is regulated oxygen and superheated vapour proportioning control oxygen concn in certain limit in the annular space; Described oxygen and carbonaceous material be the main burning strong exothermal reaction that takes place in the fluerics, and the heat of release provides heat for the gasification reaction in the reactor; The superheated vapour that feeds in the annular space, can strengthen the internal recycle of particles of carbonaceous material, and carry out thermal exchange with the high-temperature gas in pipe core zone, provide heat for gasification thermo-negative reaction in the annular space simultaneously, through heat exchange and gasification thermo-negative reaction are avoided the appearance in localized hyperthermia district, the generation probability of reduction jet pipe zone slagging scorification fast.
The fire coal that the utility model adopts for the catalytic gasification reaction provides institute's heat requirement, need not to append other equipment from heat-supplying mode, and technical process is simple, and Technological Economy is preferable, and single stove is realized the coupling of heat material, and total efficiency is higher; And the technology that the utility model provides realizes easily that on engineering industrialization is amplified simple, and prospect is huge.
Description of drawings
Fig. 1 is a kind of structural representation of how jet fluidized-bed reactor described in the utility model;
Fig. 2 is the another kind of structural representation of how jet fluidized-bed reactor described in the utility model;
Fig. 3 is a kind of structural representation of jet pipe described in the utility model;
Fig. 4 is the another kind of structural representation of jet pipe described in the utility model.
Wherein, Fig. 1 is that with the difference of Fig. 2 the arrangement form of a plurality of jet pipes is different; The difference of Fig. 3 and Fig. 4 is that the outer tube exit end shape of jet pipe is different.
Among the figure: the 1-pipe core; The 2-outer tube; The 3-annular space; 41-bed distribution device; 42-conical distribution plate; The 43-feeding line; The 44-air chamber; 45-deslagging pipeline; 46-vaporized chemical pipeline; 47-discharging pipeline.
Below the utility model is further described.But following example only is simple and easy example of the present utility model, does not represent or limit rights protection scope of the present utility model, and protection domain of the present utility model is as the criterion with claims.
Embodiment
For the utility model is described better, be convenient to understand the technical solution of the utility model, typical but non-limiting embodiment of the present utility model is as follows:
As depicted in figs. 1 and 2, a kind of how jet fluidized-bed reactor, described reactor comprises:
Reactor body, its inner chamber that forms;
Feeding line 43 runs through being arranged at reactor body top, with described chamber in fluid communication, enters in the described chamber for the material carbon material;
Discharging pipeline 47 runs through being arranged at the reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product;
Described bed distribution device 41 is made of a plurality of jet pipes; Described a plurality of jet pipe is equidistant or unequal-interval distribution in reactor.
Among Fig. 1, two or more jet pipes that are symmetrically distributed on the same horizontal plane in the described reactor, the while arranges a plurality of jet pipes of multilayer symmetry arrangement vertically, and among Fig. 2, a plurality of jet pipes are distributed in the reactor vertically with asymmetrical form.
As shown in Figure 3 and Figure 4, described jet pipe is telescoping, comprises pipe core 1 and around the outer tube 2 of pipe core 1; Form annular space 3 between described pipe core 1 and the outer tube 2.Described jet pipe is formed by connecting by horizontal section and vertical section.Among Fig. 3, the exit end of described outer tube 2 is the straight tube shape.Among Fig. 4, the exit end of described outer tube 2 is the ejector nozzle shape.
A kind of method of utilizing how jet fluidized-bed reactor to carry out catalytic coal gasifaction, the carbonaceous material of impregnated catalyst is entered chamber of the reactor through feeding line 43, vaporized chemical enters chamber of the reactor by air chamber 44 through vaporized chemical pipeline 46 behind conical distribution plate 42 even gas distributions, vaporized chemical and carbonaceous material be the generating gasification reaction under the effect of catalyzer; Described vaporized chemical is superheated vapour and O
2Mixed gas, oxygen concentration wherein is 5mol%, the water carbon mol ratio of vaporized chemical and carbonaceous material is 3.
As pipe core 1 aerating oxygen of the jet pipe of bed distribution device 41 and the gas mixture of superheated vapour, feed superheated vapour in the annular space 3; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion are for gasification reaction provides heat; Superheated vapour in the annular space 3 is strengthened jet pipe turbulence heat exchange, and the high-temperature gas with pipe core 1 zone carries out thermal exchange simultaneously, avoids the appearance in localized hyperthermia district.
Two jet pipes of symmetrical distribution on the same horizontal plane in the described reactor, the while arranges the jet pipe of three layers of symmetry arrangement vertically, and oxygen can enter reactor by bed distribution device 41 from a plurality of positions of bed, guarantees that whole bed oxygen is uniformly dispersed.Oxygen concentration is by the control of steam regulation amount, and oxygen concentration is 25mol%, and the oxygen total flux is regulated according to the equipment for gasification temperature requirement, and for catalytic gasification provides required heat, the red-tape operati temperature is at 750 ℃, and working pressure is at 2.5MPa.
Carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng and the part entrained fines discharge through discharging pipeline 47 from reactor top outlet.Remaining semicoke after the gasification is discharged reactor through deslagging pipeline 45, and deslagging pipeline 45 can feed vaporized chemical, controls bed drain purge by control tolerance size.
The steam that boiler produces and discharging pipeline expellant gas product carry out using as the superheated vapour in the present embodiment after the thermal exchange in heat-exchange equipment, and temperature is 400 ℃ after the heat exchange.
A kind of method of utilizing how jet fluidized-bed reactor to carry out catalytic coal gasifaction, the carbonaceous material of impregnated catalyst is entered chamber of the reactor through feeding line 43, vaporized chemical enters chamber of the reactor by air chamber 44 through vaporized chemical pipeline 46 behind conical distribution plate 42 gas distributions, vaporized chemical and carbonaceous material be the generating gasification reaction under the effect of catalyzer; Described vaporized chemical is superheated vapour;
As pipe core 1 aerating oxygen of the jet pipe of bed distribution device 41 and the gas mixture of superheated vapour, feed superheated vapour in the annular space 3; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion are for gasification reaction provides heat; Superheated vapour in the annular space 3 is strengthened jet pipe turbulence heat exchange, and the high-temperature gas with pipe core 1 zone carries out thermal exchange simultaneously, avoids the appearance in localized hyperthermia district;
Three jet pipes are distributed in the reactor vertically with asymmetrical form in the described reactor, and oxygen can enter reactor by bed distribution device 41 from a plurality of positions of bed, guarantees that whole bed oxygen is uniformly dispersed.Oxygen concentration is by the control of steam regulation amount, and oxygen concentration is 20mol%, and the oxygen total flux is regulated according to the equipment for gasification temperature requirement, and for catalytic gasification provides required heat, the red-tape operati temperature is at 700 ℃, and working pressure is at 3.5MPa.
Carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng and the part entrained fines discharge through discharging pipeline 47 from reactor top outlet.Remaining semicoke after the gasification is discharged reactor through deslagging pipeline 45, and deslagging pipeline 45 can lead to vaporized chemical, controls bed drain purge by control tolerance size.
The steam that boiler produces and discharging pipeline expellant gas product carry out in heat-exchange equipment that the superheated vapour as present embodiment uses after the thermal exchange, and temperature is 450 ℃ after the heat exchange, and controlling water carbon mol ratio is 2.5.
Embodiment 4
A kind of method of utilizing how jet fluidized-bed reactor to carry out catalytic coal gasifaction, the carbonaceous material of impregnated catalyst is entered chamber of the reactor through feeding line 43, vaporized chemical enters chamber of the reactor by air chamber 44 through vaporized chemical pipeline 46 behind conical distribution plate 42 gas distributions, vaporized chemical and carbonaceous material be the generating gasification reaction under the effect of catalyzer; Described vaporized chemical is superheated vapour, CO, H
2Mixed gas, CO wherein, H
2Mol ratio is 1:3, and both account for the 30mol% of vaporized chemical total amount;
As pipe core 1 aerating oxygen of the jet pipe of bed distribution device 41 and the gas mixture of superheated vapour, feed superheated vapour in the annular space 3; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion are for gasification reaction provides heat; Superheated vapour in the annular space 3 is strengthened jet pipe turbulence heat exchange, simultaneously with pipe core 1 in high-temperature gas carry out thermal exchange, avoid the appearance in localized hyperthermia district;
Two jet pipes of symmetrical distribution on the same horizontal plane in the described reactor, the while arranges the jet pipe of three layers of symmetry arrangement vertically, and oxygen can enter reactor by bed distribution device 41 from a plurality of positions of bed, guarantees that whole bed oxygen is uniformly dispersed.Oxygen concentration is by the control of steam regulation amount, and oxygen concentration is 15mol%, and the oxygen total flux is regulated according to the equipment for gasification temperature requirement, and for catalytic gasification provides required heat, the red-tape operati temperature is at 700 ℃, and working pressure is at 3.5MPa.
Carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng and the part entrained fines discharge through discharging pipeline 47 from reactor top outlet.Remaining semicoke after the gasification is discharged reactor through deslagging pipeline 45, and the deslagging pipeline can lead to vaporized chemical, controls bed drain purge by control tolerance size.
The steam that boiler produces and discharging pipeline expellant gas product carry out in heat-exchange equipment that the superheated vapour as present embodiment uses after the thermal exchange, and temperature is 500 ℃ after the heat exchange, and controlling water carbon mol ratio is 2.
Applicant's statement, the utility model illustrates detailed construction feature of the present utility model and catalysis gasification method by above-described embodiment, but the utility model is not limited to above-mentioned detailed construction feature and catalysis gasification method, does not mean that namely the utility model must rely on above-mentioned detailed construction feature and catalysis gasification method could be implemented.The person of ordinary skill in the field should understand; to any improvement of the present utility model; to the increase of the equivalence replacement of the selected parts of the utility model and accessory, the selection of concrete mode etc., all drop within protection domain of the present utility model and the open scope.
The test raw material that the utility model adopts is not for connecting ditch bituminous coal (particle diameter is 20～80 orders), and its technical analysis and ultimate analysis are shown in Table 1:
Table 1 does not connect technical analysis and the ultimate analysis of ditch bituminous coal
In fluidized bed reaction, adopt conventional single hole road jet pipe and present embodiment jet pipe to compare respectively, concrete processing condition and result are as shown in table 2:
Table 2 contrast processing condition and result
Claims (8)
1. a jet pipe is characterized in that, described jet pipe is telescoping, comprises pipe core (1) and around the outer tube (2) of pipe core (1); Form annular space (3) between described pipe core (1) and the outer tube (2).
2. jet pipe as claimed in claim 1 is characterized in that, described jet pipe is formed by connecting by horizontal section and vertical section.
3. jet pipe as claimed in claim 2, the exit end of described outer tube (2) is the ejector nozzle shape.
4. a how jet fluidized-bed reactor that has as jet pipe as described in one of claim 1-3 is characterized in that described reactor adopts at least one jet pipe as bed distribution device (41).
5. reactor as claimed in claim 4 is characterized in that, described bed distribution device (41) is made of a plurality of jet pipes; Described a plurality of jet pipe is in reactor equidistantly or non-equidistance distributes.
6. reactor as claimed in claim 5 is characterized in that, described bed distribution device (41) is made up of a plurality of jet pipes that multilayer is symmetrically distributed vertically;
Or described bed distribution device (41) is made up of a plurality of jet pipes of asymmetric distribution vertically.
7. reactor as claimed in claim 4 is characterized in that, described reactor comprises:
Reactor body, its inner chamber that forms;
Conical distribution plate (42) is positioned at described reactor body bottom, and forms air chamber (44) between the wall of reactor body bottom;
Feeding line (43) runs through being arranged at reactor body top, with described chamber in fluid communication, enters in the described chamber for raw material;
Vaporized chemical pipeline (46) runs through being arranged at the reactor body bottom, is opened on air chamber (44), enters in the described chamber by conical distribution plate (42) for vaporized chemical;
Bed distribution device (41) runs through the sidewall that is arranged at reactor body, with described chamber in fluid communication;
Discharging pipeline (47) runs through being arranged at the reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product.
8. reactor as claimed in claim 7 is characterized in that, described reactor also comprises deslagging pipeline (45), runs through described reactor body and conical distribution plate (42), is opened on described chamber, discharges reactor for the remaining semicoke after the gasification.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320045965 CN203144353U (en) | 2013-01-28 | 2013-01-28 | Jet pipe and fluidized bed reactor with jet pipe |
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|---|---|---|---|
| CN 201320045965 CN203144353U (en) | 2013-01-28 | 2013-01-28 | Jet pipe and fluidized bed reactor with jet pipe |
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| CN203144353U true CN203144353U (en) | 2013-08-21 |
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ID=48971896
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|---|---|---|---|
| CN 201320045965 Expired - Lifetime CN203144353U (en) | 2013-01-28 | 2013-01-28 | Jet pipe and fluidized bed reactor with jet pipe |
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| Country | Link |
|---|---|
| CN (1) | CN203144353U (en) |
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2013
- 2013-01-28 CN CN 201320045965 patent/CN203144353U/en not_active Expired - Lifetime
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130821 |