CN105713676B - Gasification process and device containing burnt solid particle - Google Patents
Gasification process and device containing burnt solid particle Download PDFInfo
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- CN105713676B CN105713676B CN201410725880.9A CN201410725880A CN105713676B CN 105713676 B CN105713676 B CN 105713676B CN 201410725880 A CN201410725880 A CN 201410725880A CN 105713676 B CN105713676 B CN 105713676B
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Abstract
The present invention relates to a kind of gasification process and device containing burnt solid particle; continuous gasification is realized using the fluidized-bed reactor of two-stage series connection; comprising steps of to be gasified continuously enters in first fluidized bed reactor containing burnt solid particle, first order gasification reaction occurs at a temperature of 800-900 DEG C with the first gasifying agent after mixing with the high-temperature solid particle being recycled back into；Solid particle and gas uplink containing unconverted coke enter in second fluidized bed reactor, and second level gasification reaction occurs at a temperature of 900-1000 DEG C for unconverted coke and the second gasifying agent；Part high-temperature solid particle in second fluidized bed reactor is returned in first fluidized bed reactor by outer circulation mode part, and part high-temperature solid particle is continuously removed second fluidized bed reactor, as the product for completing gasification.The present invention can reduce gasification reactor size, reduce investment, and the gas products for producing different calorific values meet the difference demand of refinery.
Description
Technical field
The present invention relates to petrochemical process, specifically the process of the production synthesis gas containing burnt solid particle continuous gasification
And realize the device of the production synthesis gas containing burnt solid particle continuous gasification.
Background technique
It the use of fluidized-bed reactor is a critically important direction, example in the catalytic cracking and thermal conversion processes of mink cell focus
Such as fluid catalytic cracking, fluid coking etc..During such, the solid particle of fluidisation, i.e. catalyst either heat carrier, anti-
Surface can generate carbon deposit in should carrying out, and the effect of solid particle may be influenced when carbon deposit is more, and needing to burn in coke removes.Contain
The combustive regeneration of burnt solid particle is not limited only to oil refining process, is easy to produce in the fluidized-bed reactor of carbon deposit and frequently involves this and ask
Topic.General solution is that solid particle is continuously delivered into another fluidized-bed reactor, introduces air or oxygenous
Body is burnt at 600-700 DEG C or so, and the solid particle for burning completion is continuously conveyed back in fluidized-bed reactor again.
Burning can complete in a fluidized-bed reactor, also have using two-section flowing bed.United States Patent (USP)
US3844973 discloses typical two sections of methods burnt, the burning tank to be generated that high gas velocity is initially entered containing burnt particle, burning tank
The dilute phase conveying pipe of undergauge is arranged in top, and gas-solid separation equipment is arranged in conveying pipe end, in the higher gas velocity of burning tank and separation
Under the action of equipment, the particle partially burnt in burning tank is entered in the close phase of second fluidized bed, referred to as two emulsion zones, is burnt
Burnt tank flue gas then enters in the dilute phase of second fluidized bed.Application No. is 9712179.5 Chinese invention patent applications to propose benefit
Two fluidized beds arranged with axial overlap are first up and then down to carry out two sections and burns.Above-mentioned patent and some improved air-burn process are all
It is the activity in order to preferably restore catalyst, improves regeneration effect.
When coke content is higher in solid particle, the heat for burning generation has been more than to take thermic load to increase needed for system,
Coke, which can be used for gasifying, at this time produces synthesis gas, meets the needs of refinery's fuel gas and hydrogen.Flexicoking technology is exactly to flow
On the basis of changing coking, the step of increasing green coke direct gasification.Gasification and burning process have certain similitude, but need
It wants higher temperature and uses vapor as gasifying agent, condition is more harsh.
United States Patent (USP) US3759676 discloses the gasification reaction process of flexicoking technology.Gasifying section has used similar
The fast fluidized bed of burning tank, coke granule to be gasified is from burning pot bottom and top diluted phase transport section while entering, upper section
Into heater in former fluid coking is played the role of, complete gasification coke be up to top settling section, settling section and quickly
Fluidized bed separates, and the unvaporized coke in settling section bottom can be used as coke product factory, partially returns in coking reactor
It is reacted as heat carrier.Although in the technology gasifying fluidized bed be provided with two layers, upper layer really as discharge solid particle used in,
It is substantially single bed gasification.Patent such as US3752658 in terms of other flexicokings etc. is single bed gasification.United States Patent (USP)
US3661543 improves flexicoking technology, and by two fluidized bed placed coaxials of heater and gasifier, the above is heating
Device, here are gasifiers, and particle to be gasified is introduced into heater, are fallen under gravity into gasifier, and gasification reaction occurs,
It is substantially still single bed gasification.NPRA meeting (1982) discloses a kind of double gas circuit flexicoking methods, and this method will gasify
It is divided into two sections, one section is gasified using air/water steam, and two sections use pure oxygen/steam gasification, and two stage gasification uses two simultaneously
The bed fluidized bed of column exchanges solid particle by particle delivery pipe.Traditional flexicoking uses air gasification, the combustion of generation
Gas calorific value is low, and utilization rate is not high.And use pure oxygen gasification problematic, heat supply work is also played since gasification is not only production gas
With pure oxygen is obviously uneconomical for combustion heat supplying.It is divided into two sections, one section of air is mainly used for heat supply and adds production fuel gas with low heat value,
Two sections of synthesis gas that can produce high heating value, economy are more preferable.But double gas circuit gasifications are used, in addition coking reactor and heating
Device, shares 4 fluidized beds for having particle to convey between each other arranged side by side, and operation is excessively complicated.
Application No. is in 03157570.6,200710178843.0,200910244214.2,201210169277.8 etc.
State's patent application discloses the technology of heavy oil thermo-contact cracking and gasification coupling, and it is gentle that these technologies focus on Fluid thermal cracking
The coupling of change process, coupling and thermally equilibrated problem including reaction are all made of simple single bed gasification in terms of gasification.
Solid thermal carriers thermally contact the coke of cracking generation with oil product, and there are two stages, first in gasification reaction to be
The gasification of the higher activated charcoal of hydrogen content, the stage gasification rate is fast, and second is the higher coke of remaining degree of graphitization
Gasification, the gasification difficulty of these coke is higher, is gasified totally and takes a long time and higher temperature.It is general in above-mentioned technology
All over using single bed gasification, gasification needs biggish gasification reactor and a large amount of outlets of coke under lower severity, compared with
Gasifying under high severity then, more stringent requirements are proposed and higher energy consumption to equipment requirement.Therefore, anti-according to coke gasification
It answers rule to rationally design gasification reaction process, bigger raising is had for the economy of this kind of technologies.
Summary of the invention
The technical problem to be solved by the invention is to provide a kind of gasification process containing burnt solid particle, this method can be mentioned
The intensity of gasification and raising heating efficiency of high coke.
In order to achieve the above object, the gasification process of the invention containing burnt solid particle, using the fluidized bed of two-stage series connection
Reactor realizes continuous gasification, includes the following steps:
To be gasified continuously enters in first fluidized bed reactor containing burnt solid particle, with the high-temp solid being recycled back into
First order gasification reaction occurs after particle mixing at a temperature of T1 with the first gasifying agent, T1 is 800-900 DEG C；
Solid particle and gas uplink containing unconverted coke enter in second fluidized bed reactor, unconverted coke with
Second level gasification reaction occurs at a temperature of T2 for the second gasifying agent, and T2 is 900-1000 DEG C；
Part high-temperature solid particle in second fluidized bed reactor returns to first class by outer circulation mode part
The temperature of solid particle in first fluidized bed reactor is promoted in bed reactor, part high-temperature solid particle is continuously removed second
Fluidized-bed reactor, as the product for completing gasification.
The method provided according to the present invention realizes the gasification reaction of coke, first class using two-stage fluidized bed reactor
Partial heat comes from second fluidized bed reactor in bed reactor, so as to obtain being higher than conventional gas in first order gasification reaction
The high heating value synthesis gas of change process.More, (heavy oil is raw for the feature that method provided by the invention is reacted based on heavy oil green coke continuous gasification
There are two stages in burnt continuous gasification reaction, first is the gasification of the higher activated charcoal of hydrogen content, the stage gasification rate
Fastly, second be the higher coke of remaining degree of graphitization gasification, the gasification difficulty of these coke is higher, and be gasified totally needs
Longer time and higher temperature), keep the temperature of the second level gasification reaction 100-200 higher than the temperature of first order gasification reaction
DEG C, so that first order gasification reaction can complete the gasification of high activity coke, second level gasification reaction can be completed to remain difficult gasification coke
The gasification of charcoal.
The above-mentioned gasification process containing burnt solid particle, wherein first gasifying agent includes oxygen and vapor, and institute
State the 2-20% that oxygen volume accounts for the first gasifying agent total volume.Second gasifying agent includes oxygen and vapor, and the oxygen
Air volume accounts for the 12-35% of the second gasifying agent total volume.That is, the first gasifying agent can use lower oxygen content.
Second gasifying agent is needed compared to the higher oxygen content of the first gasifying agent, with higher temperature and faster reaction rate by coke
Conversion, in this way, the second level gasification reaction under higher oxygen concentration can quickly convert coke, reduces gasified reverse
The equipment size of device is answered, equipment investment expense can be reduced.
The above-mentioned gasification process containing burnt solid particle, wherein first gasifying agent or/and second gasifying agent are
The mixed gas of air and vapor reduces operating cost to save the dosage of pure oxygen.
The above-mentioned gasification process containing burnt solid particle, wherein the second level gasification reaction after first order gasification reaction
It before, further include that the solid particle containing unconverted coke that will be entered in second fluidized bed reactor and gas carry out gas-solid point
From the solid particle step to obtain first order gas products He isolate, in this way, the solid particle isolated and the second fluidisation
Solid particle mixing in bed reactor, relays the raw second level gasification reaction of supervention in second fluidized bed reactor, generates the
Secondary gas product.First order gas products are the gas of high effectively Gas content, can be used as hydrogen manufacturing or high heating value combustion gas；Second
Grade gas products can be used as fuel gas with low heat value.
The above-mentioned device containing burnt solid particle gasification process is able to achieve the present invention further provides a kind of, comprising:
First fluidized bed reactor has material inlet and the first gasification agent inlet on the first fluidized bed reactor；
Second fluidized bed reactor, positioned at the top of the first fluidized bed reactor, the second fluidized bed reactor
It is upper that there are the second gasification agent inlet, gas products outlet and regenerated solids particle discharge ports；
Outer circulating tube, one end are connected to the first fluidized bed reactor, and it is anti-that the other end is connected to the second fluidized bed
Device is answered, by the part high-temperature solid particle in the second fluidized bed reactor by outer circulation mode back to described first-class
In fluidized bed reactor；And
Dilute phase conveying pipe, one end are connected to the first fluidized bed reactor, and the other end is connected to the second fluidized bed
Reactor, by the first fluidized bed reactor gas and solid particle by diluted phase transport mode go upward to described second
In fluidized-bed reactor；
Wherein, the first vulcanization bed reactor is upstriker fluidized-bed reactor, and the second fluidized bed reactor is
Bed fluidized-bed reactor, and the second fluidized bed reactor and the first fluidized bed reactor pass through the outer circulating tube
And the dilute phase conveying pipe is connected in series.
The above-mentioned gasification installation containing burnt solid particle, wherein the dilute phase conveying pipe is placed in the second fluidized bed
The inside of reactor.
The above-mentioned gasification installation containing burnt solid particle, wherein the top of the dilute phase conveying pipe has multiple openings, institute
It states multiple openings and is directly connected to the second fluidized bed inside reactor, there are multiple whirlwind in the second fluidized bed reactor
Separator, the multiple cyclone separator are respectively provided with separated gas outlet, the separated gas outlet and the gas products
Outlet is connected.
The above-mentioned gasification installation containing burnt solid particle, wherein the top of the dilute phase conveying pipe has multiple openings, institute
Stating has multiple cyclone separators in second fluidized bed reactor, the multiple cyclone separator is respectively provided with separation gas and goes out
Mouthful, multiple opening connections corresponding with the part cyclone separator in multiple cyclone separators, the cyclone separator with open communication
Separated gas outlet connect with the external world, the separated gas outlet of remaining cyclone separator and the gas products, which export, to be connected.
The above-mentioned gasification installation containing burnt solid particle, wherein the first fluidized bed inside reactor arranged beneath has
Gas distributor, the gas distributor are connect with first gasification agent inlet.
The above-mentioned gasification installation containing burnt solid particle, wherein the second fluidized bed inside reactor arranged beneath has
Gas distributor, the gas distributor are connect with second gasification agent inlet.
Gasification installation containing burnt solid particle of the invention is able to satisfy the requirement of continuous gasification, and can improve the gas of coke
Change intensity and improves heating efficiency.
Below in conjunction with the drawings and specific embodiments, the present invention will be described in detail, but not as a limitation of the invention.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the gasification installation containing burnt solid particle of the first embodiment of the present invention；
Fig. 2 is the structural schematic diagram of the gasification installation containing burnt solid particle of the second embodiment of the present invention.
Wherein, appended drawing reference
10-first fluidized bed reactors
11-material inlets
20-second fluidized bed reactors
The outlet of 21-gas products
22-regenerated solids particle discharge ports
30-outer circulating tubes
40-dilute phase pipes
41-openings
50-cyclone separators
51,52-separated gas outlet
61,62-gas distributor
70-material input pipes
80-regenerated solids particle discharge pipes
Specific embodiment
Technical solution of the present invention is described in detail in the following with reference to the drawings and specific embodiments, to be further understood that
The purpose of the present invention, scheme and effect, but it is not intended as the limitation of scope of the appended claims of the present invention.
In conjunction with refering to fig. 1, the gasification installation containing burnt solid particle of one embodiment of the invention, including the first fluidized bed react
Device 10, second fluidized bed reactor 20, outer circulating tube 30 and dilute phase conveying pipe 40, second fluidized bed reactor 20 with it is first-class
Fluidized bed reactor 10 is connected in series by outer circulating tube 30 and dilute phase conveying pipe 40.
First fluidized bed reactor 10 is upstriker fluidized-bed reactor, has material inlet 11 and the first gasifying agent thereon
Entrance (not shown), material inlet 11 are connected to material input pipe 70.And 10 lower inside cloth of first fluidized bed reactor
It is equipped with gas distributor 61, gas distributor 61 is connect with the first gasification agent inlet.
Second fluidized bed reactor 20 is located at the top of first fluidized bed reactor 10, and second fluidized bed reactor 20 is bed
Laminar flow fluidized bed reactor has the second gasification agent inlet (not shown), gas products outlet 21 and regenerated solids thereon
Grain outlet 22, regenerated solids particle discharge ports 22 are connected to regenerated solids particle discharge pipe 80.Second fluidized bed reactor 20
Lower inside is disposed with gas distributor 62, and gas distributor 62 is connect with the second gasification agent inlet.
30 one end of outer circulating tube is connected to first fluidized bed reactor 10, and the other end is connected to second fluidized bed reactor
20, by by the part high-temperature solid particle in second fluidized bed reactor 20 by outer circulation in a manner of back to the first fluidized bed it is anti-
It answers in device 10.
40 one end of dilute phase conveying pipe is connected to first fluidized bed reactor 10, and the other end is connected to second fluidized bed reactor
20, by first fluidized bed reactor 10 gas and solid particle by diluted phase transport mode go upward to second fluidized bed react
In device 20, preferably, dilute phase conveying pipe 40 can be integrally formed with first fluidized bed reactor 10, that is, dilute phase conveying pipe 40 is the
A part of fluidized-bed reactor 10 is so that first fluidized bed reactor 10 is upstriker fluidized-bed reactor, dilute phase conveying pipe
40 are placed in the inside of second fluidized bed reactor 20, and specifically, dilute phase conveying pipe 40 is directly from second fluidized bed reactor 20
Bottom be inserted into the inside of second fluidized bed reactor 20.Also, the top of dilute phase conveying pipe 40 has multiple openings 41, should
Multiple openings 41 are directly connected to inside second fluidized bed reactor 20, have multiple cyclonic separations in second fluidized bed reactor 20
Device 50, multiple cyclone separators 50 are respectively provided with separated gas outlet 51, and separated gas outlet 51 exports 21 phases with gas products
Even.
When gasification, continuously entered from material input pipe 70 into first fluidized bed reactor 10 containing burnt solid particle, second
Part high-temperature solid particle continuously returns in first fluidized bed reactor 10 from outer circulating tube 30 in fluidized-bed reactor 20, the
One gasifying agent enters first fluidized bed reactor 10 through gas distributor 61 and first order gasification reaction occurs with containing burnt solid particle,
It adjusts the flow of solids circulation and the first gasifying agent in outer circulating tube 30 and controls 800-900 DEG C of reaction temperature, it is not complete
Second fluidized bed reactor is entered by dilute phase conveying pipe 40 at the gas of reaction and containing burnt solid particle and gasification product
20, the second gasifying agent enters second fluidized bed reactor 20 through gas distributor 62 and sends out with what is be not gasified totally containing burnt solid particle
Raw second level gasification reaction, adjusting the flow of the second gasifying agent and controlling reaction temperature is 900-1000 DEG C.Second fluidized bed is anti-
Gas products and solid particle in device 20 are answered to realize gas solid separation in cyclone separator 50, gas (the as gas isolated
Change product) it is used as gasification product through separated gas outlet 51 and the discharge of gas products export 21, solid particle part is from outer circulation
Pipe 30 is recycled in first fluidized bed reactor 10, is partially continuously discharged through regenerated solids particle discharge pipe 80, as except defocused
Regenerated solids particle.
Accordingly, the gasification process of the invention containing burnt solid particle is real using the fluidized-bed reactor of two-stage series connection
Existing continuous gasification, includes the following steps:
To be gasified continuously enters in first fluidized bed reactor containing burnt solid particle, with the high-temp solid being recycled back into
First order gasification reaction occurs after particle mixing at a temperature of T1 with the first gasifying agent, T1 is 800-900 DEG C；
Solid particle and gas uplink containing unconverted coke enter in second fluidized bed reactor, unconverted coke with
Second level gasification reaction occurs at a temperature of T2 for the second gasifying agent, and T2 is 900-1000 DEG C；
Part high-temperature solid particle in second fluidized bed reactor returns to first class by outer circulation mode part
The temperature of solid particle in first fluidized bed reactor is promoted in bed reactor, part high-temperature solid particle is continuously removed second
Fluidized-bed reactor, as the product for completing gasification.
Gasification process according to the present invention containing burnt solid particle, due to consolidating the high temperature in second fluidized bed reactor 20
Body is returned in first fluidized bed reactor 10 by outer circulation mode part, provides heat for first fluidized bed reactor 10.
Therefore, in first fluidized bed reactor 10 in first gasifying agent can use lower oxygen content, provided by the invention first
Gasifying agent is preferably vapor and oxygen mixture, and oxygen volume accounts for the 2-20% of the first gasifying agent total volume.Second fluidisation
Second gasifying agent needs higher oxygen content in bed reactor 20, is turned coke with higher temperature and faster reaction rate
Change, preferred second gasifying agent is vapor and oxygen mixture, and wherein oxygen volume accounts for the 12- of the second gasifying agent total volume
35%, in this way, the second level gasification reaction under higher oxygen concentration can quickly convert coke, to reduce gasified reverse
The equipment size of device is answered, to reduce equipment investment expense.
Gasification process according to the present invention containing burnt solid particle, since the second level is gasified in second fluidized bed reactor 20
The product of reaction is fuel gas with low heat value, can save pure oxygen using the mixed gas of air and vapor as the second gasifying agent
Dosage, reduce operating cost.It is of course also possible to use the mixed gas of air and vapor is as the first gasifying agent, with same
Sample reaches the dosage for saving pure oxygen, reduces the purpose of operating cost.
Referring to Fig.2, the structural schematic diagram of the gasification installation containing burnt solid particle of the second embodiment of the present invention, this implementation
The structure of the gasification installation of example is roughly the same with the structure of the gasification installation of first embodiment, the difference is that: diluted phase transport
The top of pipe 40 has multiple openings 41, has multiple cyclone separators 50, multiple whirlwind point in second fluidized bed reactor 20
It is (another with separated gas outlet 51 on such as a portion cyclone separator 50 that separated gas outlet is respectively provided with from device 50
There is separated gas outlet 52 on part cyclone separator 50), multiple openings 41 and the part whirlwind in multiple cyclone separators
Separator (such as the cyclone separator with separated gas outlet 52) corresponding connection, point for the cyclone separator being connected to opening 41
It is connect from gas vent 52 with the external world, the separated gas outlet 51 of remaining cyclone separator is connected with the outlet of gas products 21.This
Sample, gas products and partial gasification after first order gasification reaction first pass through part cyclone separator (tool containing burnt solid particle
Have the cyclone separator of separated gas outlet 52) realize gas solid separation, the gas isolated is from the cyclone separator top exit
(separated gas outlet 52), which is drawn, is used as first order gas products, and the solid particle isolated enters back into second fluidized bed reactor
Second level gasification reaction occurs in 20, later again through the part cyclone separator (whirlwind with separated gas outlet 51
Separator) gas solid separation, the gas isolated is through separated gas outlet 51 and the discharge of gas products export 21 as second level gas
Body product.The first order gas products are high heat value gas products, which is low-BTU gas product.
When carrying out the gasification containing burnt solid particle using the gasification installation of second embodiment, has and use first embodiment
Gasification installation carry out the roughly the same step of gasification containing burnt solid particle, the difference is that second implementing according to the present invention
When the gasification installation of example carries out the gasification containing burnt solid particle, before second level gasification reaction after first order gasification reaction,
Further include the solid particle containing unconverted coke that will be entered in second fluidized bed reactor and gas carry out gas solid separation with
The solid particle step for obtaining first order gas products and isolating, that is to say, that in second fluidized bed reactor 20 in the future
It is separated from the solid particle and gas of first fluidized bed reactor 10, gas is directly off second fluidized bed reactor 20 as the
Level-one gas products, the solid particle isolated are mixed with the solid particle in second fluidized bed reactor 20, in the second fluidisation
Bed reactor 20 relays the raw second level gasification reaction of supervention, obtains second level gas products.First order gas products can be used as making
Hydrogen or high heating value combustion gas, second level gas products can be used as fuel gas with low heat value.
Using the gasification process proposed by the present invention containing burnt solid particle, its advantage is that:
(1) segmented gasification of coke is realized according to coke gasification rule, and is optimized between two stage gasification
Heating efficiency is used for first order gasification by the heat that the second level is gasified, and can obtain being higher than conventional gas in the first order
The high heating value synthesis gas of change process.
(2) oxygen content that can improve gasifying agent in the second level is gasified using the method for two-stage gasification, promotes gasification
Temperature improves gasification reaction intensity, reduces the equipment size of gasification reactor, investment reduction.
(3) two-stage, which gasifies, is suitble to refinery to the different demands of combustion gas, not only can provide fuel gas with low heat value, but also can provide and be used for
The high heating value synthesis gas of chemical process.
(4) the gas-solid cyclic process of device is burnt similar to two sections of existing catalytic cracking unit, the conveying of particle, stream
Amount control has had accumulated a large amount of experiences in terms of engineering technology, and relevant device and accessory are highly developed, are conducive to the work of the technology
Journey and commercial operation.
Introduction is compared to the prior art and the present invention below in conjunction with multiple practical application examples.
Prior art application examples
Using conventional single fluidized bed gasification method, by the sieve and silica-sesquioxide particle (30-100 μm of partial size) containing burnt 2wt%
From the fluidized bed that top is introduced continuously into diameter 150mm high 1800mm, go out to be partially completed the solid of reaction from side line overflow
Grain.Fluidized-bed bottom is passed through oxygen/water vapor volume than the mixed gas for 1:6, and burning/gasification reaction self-heating is flat under normal pressure
Weighing apparatus measures the composition of gas products, the coke content of measurement discharge particle to 850 DEG C.Available gas H in gas products2Volume
Content 32%, CO volume content 39%, methane and ethane are less than 1%, available gas total 72%.Calculated coke consumption speed
Rate: particle mean residence time 7min, coke conversion about 50%, particle mean residence time 55min, coke conversion is about
95%.
Application examples 1 of the present invention
Using two-stage gasification process proposed by the present invention, by sieve and silica-sesquioxide particle (the partial size 30-100 μ containing burnt 2wt%
M) from the first fluidized bed reactor 10 that side is introduced continuously into the high 600mm of diameter 150mm main paragraph, first fluidized bed reaction
10 bottom of device is passed through the gasifying agent of oxygen/water vapor volume ratio 1:19, and the top of first fluidized bed reactor 10 is defeated by dilute phase
Pipe 30 is sent to be transported to gas-solid together in the second fluidized bed reactor 20 of the high 1200mm of diameter 150mm main paragraph, the second
20 bottom of fluidized bed reactor is passed through the gasifying agent of oxygen/water vapor volume ratio 1:4.Control gasification agent flux and second fluidized bed are anti-
Device 20 is answered to return to the grain flux (specific control belongs to the prior art, does not repeat herein) of first fluidized bed reactor 10,
The temperature of autothermal equilibrium is 850 DEG C in first fluidized bed reactor 10, and the autothermal equilibrium temperature of second fluidized bed reactor 20 is
935℃.10 exit gas of sampled measurements first fluidized bed reactor and 20 exit gas of second fluidized bed reactor composition, first
H in 10 gas products of fluidized-bed reactor2Volume content 35%, CO volume content 46%, methane volumetric content 3%, effective gas
Body content 84%, H in 20 gas products of second fluidized bed reactor2Content 31%, CO content 38%, methane content 2%, effectively
Gas content 71%.With the comparative illustration of prior art application examples, due to introducing second in first fluidized bed reactor 10
High-temperature solid particle in fluidized-bed reactor 20 can reach 850 DEG C of gasification temperature under less oxygen input condition,
Obtained effective Gas content is 12 percentage points higher than comparative example, and second fluidized bed reactor 20 needs more due to outputing heat
High oxygen inputs, and effectively Gas content significantly reduces in gasification product gas, due to mixed with the gas of first fluidized bed reactor 10
Conjunction can not measure specific value, but effective Gas content of the gas products after mixing is suitable with comparative example.In the present embodiment, meter
The sum of the mean residence time of the solid particle of calculating in two fluidized beds be 30min, be discharged particle in coke substantially completely
Conversion is less than measurement range.
Application examples 2 of the present invention
Using two-stage gasification process proposed by the present invention, by sieve and silica-sesquioxide particle (the partial size 30-100 μ containing burnt 2wt%
M) from the first fluidized bed reactor 10 that side is introduced continuously into the high 600mm of diameter 150mm main paragraph, first fluidized bed reaction
10 bottom of device is passed through the gasifying agent of oxygen/water vapor volume ratio 1:24, and the top of first fluidized bed reactor 10 will by rotation point
Gas solid separation, in the second fluidized bed reactor 20 of Solid Conveying and Melting to the high 1200mm of diameter 150mm main paragraph, the second fluidized bed
20 bottom of reactor is passed through the gasifying agent of air/water vapor volume ratio 2:1.Control gasification agent flux and second fluidized bed reactor
20 return to the grain flux of first fluidized bed reactor 10, and the temperature of autothermal equilibrium is 870 DEG C in first fluidized bed reactor 10,
The autothermal equilibrium temperature of second fluidized bed reactor 20 is 900 DEG C.10 exit gas of sampled measurements first fluidized bed reactor and
20 exit gas of second fluidized bed reactor forms, H in 10 gas products of first fluidized bed reactor2Volume content 36%, CO
Volume content 46%, methane volumetric content 3%, available gas content 85%, H in 20 gas products of second fluidized bed reactor2
Content 17%, CO content 9%, available gas content 26%.The product gas of first fluidized bed reactor 10 can be used for hydrogen manufacturing or
Other chemical processes, 20 product gas of second fluidized bed reactor contain a large amount of nitrogen, and calorific value is lower, can be used for boiler combustion.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe
It knows those skilled in the art and makes various corresponding changes and modifications, but these corresponding changes and change in accordance with the present invention
Shape all should fall within the scope of protection of the appended claims of the present invention.
Claims (8)
1. a kind of gasification process containing burnt solid particle, which is characterized in that realized and connected using the fluidized-bed reactor of two-stage series connection
Continuous gasification, includes the following steps:
To be gasified continuously enters in first fluidized bed reactor containing burnt solid particle, with the high-temperature solid particle being recycled back into
First order gasification reaction occurs after mixing at a temperature of T1 with the first gasifying agent, T1 is 800-900 DEG C, and the first fluidized bed is anti-
Answering device is upstriker fluidized-bed reactor, and first gasifying agent includes oxygen and vapor, and the oxygen volume accounts for first
The 2-20% of gasifying agent total volume；
Solid particle and gas uplink containing unconverted coke enter in second fluidized bed reactor, unconverted coke and second
Second level gasification reaction occurs at a temperature of T2 for gasifying agent, and T2 is 900-1000 DEG C, and the second fluidized bed reactor is bed
Fluidized-bed reactor, second gasifying agent includes oxygen and vapor, and the oxygen volume accounts for the second gasifying agent total volume
12-35%；
Part high-temperature solid particle in second fluidized bed reactor is anti-back to the first fluidized bed by outer circulation mode part
The temperature that solid particle in first fluidized bed reactor is promoted in device is answered, part high-temperature solid particle is continuously removed the second fluidisation
Bed reactor, as the product for completing gasification.
2. the gasification process according to claim 1 containing burnt solid particle, which is characterized in that first order gasification reaction it
It further include the solid particle containing unconverted coke that will be entered in second fluidized bed reactor afterwards before the gasification reaction of the second level
And gas carries out solid particle step of the gas solid separation to obtain first order gas products He isolate.
3. a kind of gasification installation containing burnt solid particle characterized by comprising
First fluidized bed reactor has material inlet and the first gasification agent inlet on the first fluidized bed reactor；
Second fluidized bed reactor has on the second fluidized bed reactor positioned at the top of the first fluidized bed reactor
There are the second gasification agent inlet, gas products outlet and regenerated solids particle discharge ports；
Outer circulating tube, one end are connected to the first fluidized bed reactor, and the other end is connected to the second fluidized bed reactor,
Part high-temperature solid particle in the second fluidized bed reactor is returned into the first fluidized bed by outer circulation mode
In reactor；And
Dilute phase conveying pipe, one end are connected to the first fluidized bed reactor, and the other end is connected to the second fluidized bed reaction
Device, by the first fluidized bed reactor gas and solid particle by diluted phase transport mode go upward to it is described second fluidisation
In bed reactor；
Wherein, the first fluidized bed reactor is upstriker fluidized-bed reactor, and the second fluidized bed reactor is bed
Fluidized-bed reactor, and the second fluidized bed reactor and the first fluidized bed reactor pass through the outer circulating tube and institute
State dilute phase conveying pipe series connection.
4. the gasification installation according to claim 3 containing burnt solid particle, which is characterized in that the dilute phase conveying pipe accommodating
In the inside of the second fluidized bed reactor.
5. the gasification installation according to claim 4 containing burnt solid particle, which is characterized in that the top of the dilute phase conveying pipe
Portion has multiple openings, and the multiple opening is directly connected to the second fluidized bed inside reactor, and the second fluidized bed is anti-
Answering has multiple cyclone separators in device, the multiple cyclone separator is respectively provided with separated gas outlet, the separation gas
Outlet is connected with gas products outlet.
6. the gasification installation according to claim 4 containing burnt solid particle, which is characterized in that the top of the dilute phase conveying pipe
Portion has multiple openings, has multiple cyclone separators, the multiple cyclone separator point in the second fluidized bed reactor
Not Ju You separated gas outlet, it is multiple opening it is corresponding with the part cyclone separator in multiple cyclone separators be connected to, with opening
The separated gas outlet of the cyclone separator of connection is connect with the external world, the separated gas outlet of remaining cyclone separator and the gas
Body products export is connected.
7. the gasification installation according to claim 3 containing burnt solid particle, which is characterized in that the first fluidized bed reaction
Device lower inside is disposed with gas distributor, and the gas distributor is connect with first gasification agent inlet.
8. the gasification installation according to claim 3 containing burnt solid particle, which is characterized in that the second fluidized bed reaction
Device lower inside is disposed with gas distributor, and the gas distributor is connect with second gasification agent inlet.
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| CN113801701B (en) * | 2021-09-06 | 2022-05-20 | 华中科技大学 | Gasification reactor suitable for wide-screening raw materials |
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