CN105713675A - Coke-containing solid particle two-stage gasification method and device - Google Patents
Coke-containing solid particle two-stage gasification method and device Download PDFInfo
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- CN105713675A CN105713675A CN201410725834.9A CN201410725834A CN105713675A CN 105713675 A CN105713675 A CN 105713675A CN 201410725834 A CN201410725834 A CN 201410725834A CN 105713675 A CN105713675 A CN 105713675A
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Abstract
The invention relates to a coke-containing solid particle two-stage gasification method and device. The method utilizes two-stage tandem fluidized bed reactors to realize continuous gasification and comprises 1, a first-stage gasification reaction at a temperature of 800-900 DEG C, 2, gas-solid separation of a first synthetic gas product and first solid particles, 3, downward feeding of the separated first solid particle into a second fluidized bed reactor through an outer circulation method and then a second-stage gasification reaction at a temperature of 900-1000DEG C, 3, gas-solid separation of a second synthetic gas product and second solid particles, 4, discharging of a part of the second synthetic gas product into the environment and simultaneous introduction of a part of the second synthetic gas product into a first fluidized bed reactor, or discharging of all the second synthetic gas product into the environment, and continuous discharging of the separated second solid particles out of the second fluidized bed reactor. The coke-containing solid particle two-stage gasification method reduces a gasification reactor size, reduces an investment and can produce gas products with different calorific values so that refinery difference demands are satisfied.
Description
Technical field
The present invention relates to petrochemical process, specifically produce the process of synthesis gas containing burnt solid particle continuous gasification and realize producing containing burnt solid particle continuous gasification the device of synthesis gas.
Background technology
In the catalytic cracking of mink cell focus and thermal conversion processes, use fluidized-bed reactor is a critically important direction, for instance fluid catalytic cracking, fluid coking etc..In this class process, the solid particle of fluidisation, i.e. catalyst or heat carrier, in reaction carries out, surface can produce carbon deposit, is likely to affect the effect of solid particle when carbon deposit is more, it is necessary to coke burning is removed.Combustive regeneration containing burnt solid particle is not limited only to oil refining process, it is easy to produce also to frequently involve this problem in the fluidized-bed reactor of carbon deposit.General solution is that solid particle delivers into another fluidized-bed reactor continuously, introduces air or oxygen-containing gas burns at about 600-700 DEG C, and the solid particle burnt is carried continuously and returned in fluidized-bed reactor.
Burn and can complete in a fluidized-bed reactor, also have and use two-section flowing bed.US Patent No. 3844973 discloses two sections of air-burn process of typical case, the to be generated burning tank initially entering high gas velocity containing burnt granule, burning tank top arranges the dilute phase conveying pipe of undergauge, conveying pipe end arranges gas-solid separation equipment, under the fast effect with separation equipment of the gas that burning tank is higher, in burning tank, part burnt particles enters in second close phase of fluid bed, is called that two emulsion zones, burning tank flue gas then enter in second fluid bed dilute phase.Application number be 97121795 Chinese invention patent application propose that two fluid beds utilizing axial overlap to arrange are first up and then down to carry out two sections and burn.The air-burn process of above-mentioned patent and some improvement is provided to better recover catalyst activity, improves regeneration effect.
When in solid particle, coke content is higher, burning needed for the heat of generation exceeded system, heat-obtaining load increases, and now coke can be used for gasification and produces synthesis gas, meets the demand of refinery's fuel gas and hydrogen.Flexicoking technology is exactly on the basis of fluid coking, adds green coke direct gasification step.Gasification and burning process have certain similarity, but need higher temperature and use steam as gasifying agent, and condition is more harsh.
US Patent No. 3759676 discloses the gasification reaction process of flexicoking technology.Gasifying section employs the fast fluidized bed of similar burning tank, coke granule to be gasified simultaneously enters with top diluted phase transport section bottom burning tank, epimere enters and plays the effect of heater in former fluid coking, the coke completing gasification is up to top settling section, settling section and fast fluidized bed separate, the coke not gasified bottom settling section can dispatch from the factory as coke product, is partly returned in coking reactor and reacts as heat carrier.Although gasifying fluidized bed is provided with two-layer in this technology, upper strata, really as discharging used by solid particle, is substantially single bed gasification.The patent of other flexicoking aspect such as US3752658 etc. is single bed gasification.Flexicoking technology is improved by US Patent No. 3661543, and by heater and two fluid bed placed coaxial of gasifier, the above is heater, gasifier is presented herein below, treating that gasification granule is introduced into heater, fall under gravity in gasifier, generating gasification is reacted.Substantially it is still single bed gasification.NPRA meeting (1982) discloses a kind of double; two gas circuit flexicoking method, gasification is divided into two sections by the method, one section adopts the gasification of air/water steam, two-stage nitration adopts pure oxygen/steam gasification, two stage gasification have employed two bed fluid beds arranged side by side, carries pipe exchange solid particle by granule.Traditional flexicoking adopts air gasification, and the fuel gases calorific value of generation is low, and utilization rate is not high.And adopt pure oxygen gasification problematic, and also to play for heat effect owing to aerogenesis is not only in gasification, pure oxygen is obviously uneconomical for combustion heat supplying.Being divided into two sections, one section of air is mainly used in heat supply and adds production fuel gas with low heat value, and two-stage nitration can produce the synthesis gas of high heating value, and economy is better.But adopting double; two gas circuit gasification, add coking reactor and heater, have 4 arranged side by side fluid beds having granule to carry each other, operation is excessively complicated.
Application number is 03157570.6,200710178843.0,200910244214.2,201210169277.8 Chinese invention patent application disclose heavy oil thermal contact cracking and the technology of gasification coupling, these technology focus on the coupling of Fluid thermal cracking and gasification, including coupling and the thermally equilibrated problem of reaction, in gasification, all adopt simple single bed gasification.
Hot solids at high temperature generating gasification can react two stages of existence containing burnt problem with steam, oxygen-containing gas, first is the gasification of the activated charcoal that hydrogen content is higher, this stage gasification rate is fast, second is the gasification of the coke that the degree of graphitization remained is higher, the gasification difficulty of these coke is higher, and be gasified totally needs longer time and higher temperature.Commonly used single bed gasification in above-mentioned technology, needs bigger gasification reactor and coke outer row in a large number in relatively low severity gasified, and relatively equipment requirements is then had higher requirement by high severity gasified, and higher energy consumption.Therefore, according to coke gasification rule appropriate design gasification reaction process, the economy for this class technology has bigger raising.
Summary of the invention
The technical problem to be solved is to provide a kind of bed fluid bed continuous gasification regeneration method containing coke solids granule, and the method can improve the intensity of gasification of coke and improve heating efficiency, and makes to realize regeneration containing coke granule.
In order to achieve the above object, the two-stage gasification process containing burnt solid particle provided by the invention, adopt the fluidized-bed reactor of two-stage series connection to realize continuous gasification, comprise the steps:
To be gasified continuously enters in first class bed bioreactor containing burnt solid particle, with the first gasifying agent, first order gasification reaction occurs at T1 temperature, and T1 is 800-900 DEG C；
The gas products of first order gasification reaction gained and the solid particle of unconverted coke are carried out gas solid separation and obtains the first solid particle of the first synthesis gas product and separation；
The first solid particle separated comes downwards in second fluidized bed reactor by outer circulation mode, with the second gasifying agent, second level gasification reaction occurs at T2 temperature, and T2 is 900-1000 DEG C；
The gas products of second level gasification reaction gained and the solid particle of unconverted coke are carried out gas solid separation and obtains the second solid particle of the second synthesis gas product and separation；
While second synthesis gas product leads to the external world, part introduces to first class bed bioreactor, or all leads to the external world, and the second solid particle separated is continuously removed second fluidized bed reactor.
According to method provided by the invention, two-stage fluidized bed reactor is adopted to realize the gasification reaction of coke, two-stage gasification can be realized, in first class bed bioreactor, part heat is from second fluidized bed reactor, such that it is able to obtain being higher than the high heating value synthesis gas of traditional gasification process at first order gasification reaction.More, (in the reaction of heavy oil green coke continuous gasification, there are two stages in the feature that method provided by the invention is reacted based on heavy oil green coke continuous gasification, first is the gasification of the activated charcoal that hydrogen content is higher, this stage gasification rate is fast, second is the gasification of the coke that the degree of graphitization remained is higher, the gasification difficulty of these coke is higher, be gasified totally needs longer time and higher temperature), the temperature making second level gasification reaction is higher than the temperature of the first order gasification reaction 100-200 DEG C, thus first order gasified reverse should be able to complete the gasification of high activity coke, second level gasified reverse should be able to complete to remain the gasification of difficult gas coke.
The above-mentioned two-stage gasification process containing burnt solid particle; wherein, the second solid particle further comprising the steps of: the separation by being continuously removed second fluidized bed reactor is promoted by outer circulation mode and is mixed in first class bed bioreactor containing burnt solid particle with to gasify.
According to method provided by the invention, prioritization scheme is proposed the Btu utilization mode of two-step fluidized bed reactor.It is re-introduced in first class bed bioreactor by the high-temperature gas in second fluidized bed reactor preheating treating gasification solid particle；Can also rising in first class bed bioreactor by high-temp solid in second fluidized bed reactor by outer conveying, improve first fluidized bed reactor temperature, lift gas used can adopt the mixing gas of steam or steam and oxygen.
The above-mentioned two-stage gasification process containing burnt solid particle, wherein, further comprises the steps of: the second solid particle of the separation being continuously removed second fluidized bed reactor as the product completing gasification.
The above-mentioned two-stage gasification process containing burnt solid particle, wherein, described first gasifying agent includes oxygen and steam, and described oxygen volume accounts for the 2-20% of the first gasifying agent volume total amount.Described second gasifying agent includes oxygen and steam, and described oxygen volume accounts for the 12-35% of the second gasifying agent volume total amount.So, first gasifying agent and the second gasifying agent include oxygen and steam, two-stage gasification reaction is made to include steam gasification and oxygen combustion two parts, wherein steam gasification produces synthesis gas product, oxygen combustion provides institute's calorific requirement, thus can improving gasification heating efficiency and improving the productivity of available gas in synthesis gas.Described available gas is H well-known in the art2, the combustible gas component such as CO and hydro carbons.Owing to entering the to be gasified higher containing burnt granule hydrogen content of first class bed bioreactor, it is possible to gasify at lower temperature, therefore, the first gasifying agent in first class bed bioreactor can adopt relatively low oxygen content.The second gasifying agent in second fluidized bed reactor needs higher oxygen content, with higher temperature and faster reaction rate by coke convert, coke can quickly be converted by the second level gasification reaction under higher oxygen concentration, reduce the equipment size of gasification reactor, equipment investment expense can be reduced.
The above-mentioned two-stage gasification process containing burnt solid particle, wherein, described second gasifying agent is the mixing gas of air and steam.So, when the gas products of second level gasification reaction does not enter first class bed bioreactor, the second gasifying agent can select more cheap air and steam to be mixed to get, and generating gasification product is the synthesis gas that available gas concentration is little, for use as fuel gas with low heat value.And first class bed bioreactor can obtain the gas of high effectively Gas content, for use as hydrogen manufacturing or high heating value combustion gas.
The present invention further provides a kind of two-stage gasification installation containing burnt solid particle, including:
First class bed bioreactor, described first class bed bioreactor has material inlet, gasification agent inlet and gas products outlet, and has the first gas solid separation system in described first class bed bioreactor；
Second fluidized bed reactor, is positioned at the lower section of described first class bed bioreactor, described second fluidized bed reactor has gasification agent inlet and solid particle outlet, and has the second gas solid separation system in described second fluidized bed reactor；And
Outer circulating tube, one end is connected to described first class bed bioreactor, and the other end is connected to described second fluidized bed reactor, is come downwards in described second fluidized bed reactor by outer circulation mode by the high-temperature solid particle in described first class bed bioreactor；
Inner circulating tube, one end is connected in described first class bed bioreactor, and the other end is connected to described second gas solid separation system, is gone upward in described first class bed bioreactor by inner loop mode by the gas products in described second fluidized bed reactor；
Wherein, described first vulcanization bed reactor and described second fluidized bed reactor are all bed fluidized-bed reactor, and described second fluidized bed reactor is connected in series by described outer circulating tube and described inner circulating tube with described first vulcanization bed reactor.
The above-mentioned two-stage gasification installation containing burnt solid particle, wherein, described first class bed bioreactor and described second fluidized bed reactor arranged in co-axial alignment.
The above-mentioned two-stage gasification installation containing burnt solid particle, wherein, described first class bed bioreactor shifts to install with described second fluidized bed reactor height.
The above-mentioned two-stage gasification installation containing burnt solid particle; wherein; also include riser; one end is connected to described first class bed bioreactor; the other end is connected to described second fluidized bed reactor, by outer circulation mode, the high-temperature solid particle in described second fluidized bed reactor is promoted to described first class bed bioreactor and is mixed containing burnt solid particle with to gasify.
The two-stage gasification installation containing burnt solid particle of the present invention, can meet the requirement of continuous gasification, and can improve the intensity of gasification of coke and improve heating efficiency.
Describe the present invention below in conjunction with the drawings and specific embodiments, but not as a limitation of the invention.
Accompanying drawing explanation
Fig. 1 is the structural representation of the two-stage gasification installation containing burnt solid particle of the first embodiment of the present invention；
Fig. 2 is the structural representation of the two-stage gasification installation containing burnt solid particle of the second embodiment of the present invention.
Wherein, accompanying drawing labelling
10 first class bed bioreactors
11 material inlets
12 gas products outlets
20 second fluidized bed reactors
21 regenerated solids particle discharge ports
22 regenerated solids granules promote mouth
30 outer circulating tubes
40 inner circulating tubes
51,52 cyclone separator
511,521 separated gas outlet
61,62 gas distributor
70 material input pipes
80 regenerated solids granule discharge pipes
90 synthesis gas gas distributors
100 risers
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, technical solution of the present invention is described in detail, to be further understood that the purpose of the present invention, scheme and effect, but is not intended as the restriction of claims protection domain of the present invention.
In conjunction with consulting Fig. 1, the two-stage gasification installation containing burnt solid particle of one embodiment of the invention, including first class bed bioreactor 10, second fluidized bed reactor 20, outer circulating tube 30 and inner circulating tube 40, second fluidized bed reactor 20 is connected in series by outer circulating tube 30 and inner circulating tube 40 with first class bed bioreactor 10.
First class bed bioreactor 10 is bed fluidized-bed reactor, and it has material inlet the 11, first gasification agent inlet (not shown) and gas products outlet 12, and material inlet 11 connects with material input pipe 70.And first class bed bioreactor 10 lower inside is provided with gas distributor 61, gas distributor 61 is connected with the first gasification agent inlet.First class bed bioreactor 10 is internal, gas distributor 61 is provided above synthesis gas gas distributor 90.Having the first gas solid separation system 51 in first class bed bioreactor 10, the first gas solid separation system 51 herein is preferably cyclone separator, and this cyclone separator 51 has separated gas outlet 511, and this separated gas outlet 511 exports 12 with gas products and connects.
Second fluidized bed reactor 20 is positioned at the lower section of first class bed bioreactor 10, second fluidized bed reactor 20 is bed fluidized-bed reactor, having the second gasification agent inlet (not shown) and regenerated solids particle discharge ports 21 on it, regenerated solids particle discharge ports 21 connects with regenerated solids granule discharge pipe 80.Second fluidized bed reactor 20 lower inside is provided with gas distributor 62, and gas distributor 62 is connected with the second gasification agent inlet.Having the second gas solid separation system 52 in second fluidized bed reactor 20, the second gas solid separation system 52 herein is preferably also cyclone separator, and this cyclone separator 52 has separated gas outlet 521.
Outer circulating tube 30 one end is connected to first class bed bioreactor 10, and the other end is connected to second fluidized bed reactor 20, to be come downwards in second fluidized bed reactor 20 by outer circulation mode by the high-temperature solid particle in first class bed bioreactor 10.
Inner circulating tube 40 one end is connected in first class bed bioreactor 10, and the other end is connected to the second gas solid separation system 52, is gone upward in first class bed bioreactor 10 by inner loop mode by the gas products in second fluidized bed reactor 20.It is preferred that one end of inner circulating tube 40 connects with separated gas outlet 521, the other end is connected to a synthesis gas gas distributor 90 being arranged in first class bed bioreactor 10.
During gasification, continuously enter first class bed bioreactor 10 containing burnt solid particle from material input pipe 70, contact through the thermal evaporation product of synthesis gas gas distributor 90 with from second fluidized bed reactor 20, absorb a part of heat energy；First gasifying agent enters bottom first class bed bioreactor 10 and containing burnt solid particle generation first order gasification reaction through gas distributor 61, by known method, the first gasifying agent flow and the oxygen concentration control reaction temperature that regulate gas flow and gas distributor 61 in synthesis gas gas distributor 90 are 800～900 DEG C；The gas products of first class bed bioreactor 10 and solid particle realize gas solid separation in cyclone separator 51, isolated gas is the first synthesis gas product, solid particle part is transported to second fluidized bed reactor 20 from outer circulating tube 30, proceeds second level gasification reaction with the second gasifying agent entered through gas distributor 62 bottom second fluidized bed reactor 20；Containing higher concentration oxygen in second gasifying agent, with coke generation combustion reaction, by known method, the flow and the oxygen concentration control reaction temperature that regulate the second gasifying agent are 900～1000 DEG C.Gas products and solid particle in second fluidized bed reactor 20 realize gas solid separation in cyclone separator 52, isolated gas can partly pass through separated gas outlet 521, inner circulating tube 40, synthesis gas gas distributor 90 enter first class bed bioreactor 10, can also partly or entirely draw as the second synthesis gas product, solid particle is discharged continuously through regenerated solids granule discharge pipe 80, as the regenerated solids granule after decoking.
It is preferred that material input pipe 70 and/or regenerated solids granule discharge pipe 80 are provided with the guiding valve preventing granule from flowing backwards.
Accordingly, the two-stage gasification process containing burnt solid particle of the present invention, it is that the fluidized-bed reactor adopting two-stage series connection realizes continuous gasification, comprises the steps:
To be gasified continuously enters in first class bed bioreactor containing burnt solid particle, with the first gasifying agent (when the situation having gasification reaction isolated gas in the second level to return, contact including the second synthesis gas returned with second fluidized bed reactor, absorb a part of heat energy step) at T1 temperature, there is first order gasification reaction, T1 is 800-900 DEG C；
The gas products of first order gasification reaction gained and the solid particle of unconverted coke are carried out gas solid separation and obtains the first solid particle of the first synthesis gas product and separation；
The first solid particle separated comes downwards in second fluidized bed reactor by outer circulation mode, with the second gasifying agent, second level gasification reaction occurs at T2 temperature, and T2 is 900-1000 DEG C；
The gas products of second level gasification reaction gained and the solid particle of unconverted coke are carried out gas solid separation and obtains the second solid particle of the second synthesis gas product and separation；
While second synthesis gas product leads to the external world, part introduces to first class bed bioreactor, or all leads to the external world, and the second solid particle separated is continuously removed second fluidized bed reactor；
Using the second solid particle of the separation being continuously removed second fluidized bed reactor as the product completing gasification.
The gasification process containing burnt solid particle according to the present invention, owing to having following situation: the second synthesis gas product section introduced to first class bed bioreactor 10, provide heat for first class bed bioreactor 10.Therefore, can adopting relatively low oxygen content in first class bed bioreactor 10 in the first gasifying agent, the first gasifying agent provided by the invention is preferably oxygen and steam mixture, and oxygen volume accounts for the 2-20% of the first gasifying agent cumulative volume.In second fluidized bed reactor 20, the second gasifying agent needs higher oxygen content, with higher temperature and faster reaction rate by coke convert, preferred second gasifying agent is oxygen and steam mixture, wherein oxygen volume accounts for the 12-35% of the second gasifying agent cumulative volume, so, coke can quickly be converted by the second level gasification reaction under higher oxygen concentration, to reduce the equipment size of gasification reactor, thus reducing equipment investment expense.
The gasification process containing burnt solid particle according to the present invention, when the gas products of second level gasification reaction does not enter first class bed bioreactor 10, the gasifying agent (i.e. the second gasifying agent) of second fluidized bed reactor 20 can select more cheap air and steam to be mixed to get, generating gasification product is the synthesis gas that available gas concentration is little, can be used as fuel gas with low heat value；First class bed bioreactor can obtain the gas of high effectively Gas content, can be used as hydrogen manufacturing or high heating value combustion gas.
Consult Fig. 2, the structural representation of the two-stage gasification installation containing burnt solid particle of the second embodiment of the present invention, the structure of the two-stage gasification installation of the present embodiment is roughly the same with the structure of the two-stage gasification installation of first embodiment, it is different in that: second fluidized bed reactor 20 has regenerated solids granule and promotes mouth 22, one riser 100 one end is connected to first class bed bioreactor 10 (being connected to material input pipe 70 specifically), the other end is connected to second fluidized bed reactor 20 (promoting mouth 22 specifically by a connecting tube with regenerated solids granule to connect), mixed containing burnt solid particle with to gasify so that the high-temperature solid particle in second fluidized bed reactor 20 is promoted to first class bed bioreactor 10 by outer circulation mode, during lifting, lift gas need to be passed in riser 100, lift gas used can adopt the mixing gas of steam or steam and oxygen.
When the two-stage gasification installation adopting the second embodiment carries out the two-stage gasification containing burnt solid particle, the gasification installation having and adopt first embodiment carries out the step that the gasification containing burnt solid particle is roughly the same, institute the difference is that, the processing mode of the second solid particle is different, the present embodiment is promoted being continuously removed the second solid particle of the separation of second fluidized bed reactor by outer circulation mode and is mixed in first class bed bioreactor with to gasify containing burnt solid particle, so by solid particle conveying, a part of heat can be brought in first class bed bioreactor 10.
Adopting the first synthesis gas product that the two-stage gasification installation of the present invention prepares is high heat value gas product, and the second synthesis gas product is low-BTU gas product.
It should be noted that, although Fig. 1, Fig. 2 illustrate only the example of first class bed bioreactor and second fluidized bed reactor arranged in co-axial alignment, but in actual use, local is not in this, and height is arranged side by side etc. well known in the art meets pressure balanced fluid bed train all in the scope of the present invention.
Adopting the gasification renovation process containing burnt solid particle that the present invention proposes, its advantage is:
(1) segmented gasification of coke is achieved according to coke gasification rule, and optimize the heating efficiency between two stage gasification, by the heat that the gasification of the part second level produces is used for first order gasification, it is possible to obtain being higher than the high heating value synthesis gas of traditional gasification process in the first order.
(2) method adopting two-stage gasification can improve the oxygen content of gasifying agent in gasifying in the second level, promotes gasification temperature, improves gasification reaction intensity, reduce the equipment size of gasification reactor, investment reduction.
(3) two-stage gasification is suitable for the refinery's different demands to combustion gas, both can provide fuel gas with low heat value, and can provide again the high heating value synthesis gas for chemical process.
(4) the gas-solid course of conveying of device burns similar to the regenerator of existing catalytic cracking unit, the conveying of granule, flow-control have accumulated a large amount of experience in engineering, relevant device and accessory are highly developed, are conducive to through engineering approaches and the commercial operation of this technology.
Below in conjunction with multiple practical application examples, prior art and the present invention are compared introduction.
Prior art application examples
Adopt conventional single fluidized bed gasification method, the sieve and silica-sesquioxide granule (particle diameter 30-100 μm) containing burnt 2wt% is introduced continuously into the fluid bed of diameter 150mm height 1800mm from top, goes out to be partially completed the solid particle of reaction from side line overflow.Fluidized-bed bottom passes into oxygen/water vapor volume than the mixing gas for 1:6, and burning/gasification reaction autothermal equilibrium is to 850 DEG C at ambient pressure, measures the composition of gas products, measures the coke content discharging granule.Available gas H in gas products2Volume content 32%, CO volume content 39%, methane and ethane are less than 1%, and available gas amounts to 72%.The coke consumption speed calculated: granule mean residence time 7min, coke converts about 50%, granule mean residence time 55min, coke conversion about 95%.
Application examples 1 of the present invention
Adopt the two-stage gasification process that the present invention proposes, sieve and silica-sesquioxide granule (particle diameter 30-100 μm) containing burnt 2wt% is introduced continuously into the first class bed bioreactor 10 of diameter 180mm main paragraph height 800mm from sidepiece, the oxygen/water vapor volume gasifying agent than 1:19 is passed into bottom first class bed bioreactor 10, position, middle and lower part is that second fluidized bed reactor 20 introduces gasification product by synthesis gas gas distributor 90, and the first synthesis gas product that first order gasification obtains is extracted out from reactor bottom after cyclone separator 51.Solid particle in first class bed bioreactor 10 is transported to the middle and lower part of the second fluidized bed reactor 20 of diameter 150mm main paragraph height 600mm by outer circulating tube 30 from bottom, and this reactor bottom passes into the oxygen/water vapor volume gasifying agent than 1:4.Controlling tow channel gas agent flow and first fluidized bed reactor granules reserve, so that the temperature of first class bed bioreactor autothermal equilibrium is 850 DEG C, the autothermal equilibrium temperature of second fluidized bed reactor is 935 DEG C.Sampled measurements first fluidized bed reactor outlet gas forms, H in gas products2Volume content 34%, CO volume content 41%, methane volumetric content 2%, available gas content 77%.With the comparative illustration of prior art application examples, there are two stages in the gasification for coke, adopts two-stage gasification schemes, and the effective Gas content obtained is higher 5 percentage points than comparative example.In the present embodiment, the solid particle calculated mean residence time sum in two fluid beds is 35min, discharges coke in granule and substantially completely converts, less than the scope of measurement.
Application examples 2 of the present invention
Adopt the two-stage gasification process that the present invention proposes; it is introduced continuously into the first class bed bioreactor 10 of diameter 180mm main paragraph height 800mm from sidepiece after sieve and silica-sesquioxide granule (particle diameter 30-100 μm) containing burnt 2wt% is mixed with the solid particle after the gasification regeneration promoted from second fluidized bed reactor 20; passing into the oxygen/water vapor volume gasifying agent than 1:24 bottom first class bed bioreactor 10, the first synthesis gas product that first order gasification obtains is extracted out from reactor bottom after cyclone separator 51.Solid particle in first class bed bioreactor 10 is transported to the middle and lower part of the second fluidized bed reactor 20 of diameter 150mm main paragraph height 600mm by outer circulating tube 30 from bottom, the gasification gas of this reactor is directly led out as gasification product (i.e. the second synthesis gas product) by pipeline, and this reactor bottom passes into steam/volume of air gasifying agent than 2:1.Controlling tow channel gas agent flow, promote amount and first fluidized bed reactor granules reserve, so that the temperature of first class bed bioreactor autothermal equilibrium is 870 DEG C, the autothermal equilibrium temperature of second fluidized bed reactor is 910 DEG C.Sampled measurements first fluidized bed reactor outlet gas and second fluidized bed reactor exit gas composition, H in first fluidized bed gas reactor product2Volume content 37%, CO volume content 45%, methane volumetric content 2.5%, available gas content 84.5%, H in second fluidized bed reactor gas products2Content 12%, CO content 9%, available gas content 21%.The gas product of first class bed bioreactor can be used for hydrogen manufacturing or other chemical process, and second fluidized bed reactor gas product contains a large amount of nitrogen, and calorific value is relatively low, can be used for boiler combustion.
Certainly; the present invention also can have other various embodiments; when without departing substantially from present invention spirit and essence thereof; those of ordinary skill in the art are when can make various corresponding change and deformation according to the present invention, but these change accordingly and deformation all should belong to the scope of the claims appended by the present invention.
Claims (10)
1. the two-stage gasification process containing burnt solid particle, it is characterised in that adopt the fluidized-bed reactor of two-stage series connection to realize continuous gasification, comprise the steps:
To be gasified continuously enters in first class bed bioreactor containing burnt solid particle, with the first gasifying agent, first order gasification reaction occurs at T1 temperature, and T1 is 800-900 DEG C；
The gas products of first order gasification reaction gained and the solid particle of unconverted coke are carried out gas solid separation and obtains the first solid particle of the first synthesis gas product and separation；
The first solid particle separated comes downwards in second fluidized bed reactor by outer circulation mode, with the second gasifying agent, second level gasification reaction occurs at T2 temperature, and T2 is 900-1000 DEG C；
The gas products of second level gasification reaction gained and the solid particle of unconverted coke are carried out gas solid separation and obtains the second solid particle of the second synthesis gas product and separation；
While second synthesis gas product leads to the external world, part introduces to first class bed bioreactor, or all leads to the external world, and the second solid particle separated is continuously removed second fluidized bed reactor.
2. the two-stage gasification process containing burnt solid particle according to claim 1, it is characterised in that further comprise the steps of:
The second solid particle being continuously removed the separation of second fluidized bed reactor is promoted by outer circulation mode and is mixed in first class bed bioreactor containing burnt solid particle with to gasify.
3. the two-stage gasification process containing burnt solid particle according to claim 1, it is characterised in that further comprise the steps of:
Using the second solid particle of the separation being continuously removed second fluidized bed reactor as the product completing gasification.
4. the two-stage gasification process containing burnt solid particle according to Claims 2 or 3, it is characterised in that described first gasifying agent includes oxygen and steam, and described oxygen volume accounts for the 2-20% of the first gasifying agent volume total amount.
5. the two-stage gasification process containing burnt solid particle according to Claims 2 or 3, it is characterised in that described second gasifying agent includes oxygen and steam, and described oxygen volume accounts for the 12-35% of the second gasifying agent volume total amount.
6. the two-stage gasification process containing burnt solid particle according to Claims 2 or 3, it is characterised in that described second gasifying agent is the mixing gas of air and steam.
7. the two-stage gasification installation containing burnt solid particle, it is characterised in that including:
First class bed bioreactor, described first class bed bioreactor has material inlet, gasification agent inlet and gas products outlet, and has the first gas solid separation system in described first class bed bioreactor；
Second fluidized bed reactor, is positioned at the lower section of described first class bed bioreactor, described second fluidized bed reactor has gasification agent inlet and solid particle outlet, and has the second gas solid separation system in described second fluidized bed reactor；And
Outer circulating tube, one end is connected to described first class bed bioreactor, and the other end is connected to described second fluidized bed reactor, is come downwards in described second fluidized bed reactor by outer circulation mode by the high-temperature solid particle in described first class bed bioreactor；
Inner circulating tube, one end is connected in described first class bed bioreactor, and the other end is connected to described second gas solid separation system, is gone upward in described first class bed bioreactor by inner loop mode by the gas products in described second fluidized bed reactor；
Wherein, described first vulcanization bed reactor and described second fluidized bed reactor are all bed fluidized-bed reactor, and described second fluidized bed reactor is connected in series by described outer circulating tube and described inner circulating tube with described first vulcanization bed reactor.
8. the two-stage gasification installation containing burnt solid particle according to claim 7, it is characterised in that described first class bed bioreactor and described second fluidized bed reactor arranged in co-axial alignment.
9. the two-stage gasification installation containing burnt solid particle according to claim 7, it is characterised in that described first class bed bioreactor shifts to install with described second fluidized bed reactor height.
10. the two-stage gasification installation containing burnt solid particle according to claim 8 or claim 9; it is characterized in that; also include riser; one end is connected to described first class bed bioreactor; the other end is connected to described second fluidized bed reactor, by outer circulation mode, the high-temperature solid particle in described second fluidized bed reactor is promoted to described first class bed bioreactor and is mixed containing burnt solid particle with to gasify.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108102720A (en) * | 2017-11-01 | 2018-06-01 | 中国石油大学(华东) | Fine coal composite fluidization bed classification gasification device |
| CN110553249A (en) * | 2019-09-02 | 2019-12-10 | 中国科学院工程热物理研究所 | Rotary preheating device and method for solid fuel |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108102720A (en) * | 2017-11-01 | 2018-06-01 | 中国石油大学(华东) | Fine coal composite fluidization bed classification gasification device |
| CN110553249A (en) * | 2019-09-02 | 2019-12-10 | 中国科学院工程热物理研究所 | Rotary preheating device and method for solid fuel |
| CN110553249B (en) * | 2019-09-02 | 2021-12-24 | 中国科学院工程热物理研究所 | Rotary preheating device and method for solid fuel |
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