CN110205164B - Circulating fluidized bed gasification device and circulating fluidized bed gasification method - Google Patents
Circulating fluidized bed gasification device and circulating fluidized bed gasification method Download PDFInfo
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- CN110205164B CN110205164B CN201910499983.0A CN201910499983A CN110205164B CN 110205164 B CN110205164 B CN 110205164B CN 201910499983 A CN201910499983 A CN 201910499983A CN 110205164 B CN110205164 B CN 110205164B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- Oil, Petroleum & Natural Gas (AREA)
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Abstract
A gasification device of a circulating fluidized bed comprises a gasification furnace, a gas-solid separator and a material returning device, wherein the gasification furnace is communicated with the gas-solid separator, the gas-solid separator is communicated with the material returning device, the material returning device is communicated with the gasification furnace, a gasification agent inlet, a feeding port, a material returning port and a gasification product outlet are arranged on the gasification furnace, the gasification agent inlet comprises a primary gasification agent inlet and a secondary gasification agent inlet, the primary gasification agent inlet is located at a first position, and the secondary gasification agent inlet is located at a second position different from the first position. The invention also provides a gasification method of the circulating fluidized bed. According to the circulating fluidized bed gasification device and the circulating fluidized bed gasification method, the problem of coking at the bottom of the hearth can be reduced.
Description
Technical Field
The invention relates to the technical field of fuel gasification, in particular to a circulating fluidized bed gasification device and a circulating fluidized bed gasification method, and particularly relates to a circulating fluidized bed oxygen-enriched gasification device and a circulating fluidized bed oxygen-enriched gasification method.
Background
Coal gasification is one of the important ways for clean utilization of coal, and is mainly used for converting coal into CO and H2And CH4The gaseous clean energy is widely applied to the fields of metallurgy, synthesis and the like or used for combined cycle power generation, fuel gas and the like.
Coal gasification technologies can be mainly divided into fixed bed gasification, fluidized bed gasification and entrained flow gasification according to the moving state of solids in the system. The fluidized bed has the advantages of low raw material cost, less environmental pollution, high gasification efficiency and the like, and the circulating fluidized bed is widely applied due to the advantages of mild reaction conditions, high circulation rate, uniform temperature distribution of a hearth, sufficient gas-solid contact, wide particle size range required by raw materials and the like.
According to the type of gasification agent, the circulating fluidized bed gasification technology can be divided into air gasification, oxygen-enriched gasification, pure oxygen gasification and the like, wherein the oxygen-enriched gasification is widely applied to the fields of coal-to-high-heat-value industrial gas, synthesis gas production and the like. In the conventional circulating fluidized bed oxygen-enriched gasification process, oxygen-enriched air as a gasifying agent enters a gasification system from an air distribution device at the bottom of a hearth of a gasification furnace, raw material pulverized coal is subjected to reactions such as combustion, gasification and the like under the action of the gasifying agent, generated coal gas and carbon-containing solid particles which are not completely reacted are discharged from the upper part of the hearth and enter a gas-solid separation device for gas-solid separation, wherein most of the carbon-containing solid particles are separated and returned to the gasification furnace by a material returning device, and the rest of the dust-containing coal gas enters a subsequent dust removal and cooling system.
In a conventional circulating fluidized bed gasification furnace, all gasification agents enter the gasification furnace from the bottom of a hearth and are influenced by gas-solid flow and reaction distribution characteristics in the furnace, the bottom of the gasification furnace is a high-temperature zone, and main solid materials are large-particle semi-coke with high ash content; along the height direction of the hearth, the temperature of the hearth is gradually reduced, and the main solid material at the middle upper part of the hearth is small-particle semicoke with low ash content. Reference is made to fig. 1 with respect to the relationship between the temperature in the conventional circulating fluidized bed furnace, the concentration of particulate ash and the height of the furnace. From the aspect of the operation stability of the gasification furnace, the bottom of the hearth is easy to coke due to the high temperature and high ash content state at the bottom of the hearth; in addition, due to the influence of the oxygen concentration on the combustion reaction rate, the oxygen-enriched gasifying agent is easier to cause local high-temperature coking at the bottom of the hearth. From the viewpoint of gasification performance optimization, the reduction of the temperature at the upper part of the hearth limits the small-particle semicoke with high carbon content and CO in gas phase2And the gasification reaction between the water vapor affects the improvement of the gasification index of the system.
In addition, in order to ensure larger circulating flux, the amount of the gasification agent introduced from the bottom of the hearth needs to meet the requirement of the fluidization speed at the bottom of the hearth, part of larger particles are carried to move to the upper part of the hearth, the retention time in an oxidation zone with sufficient gasification agent is short, and the reaction is insufficient. In addition, the position of a material return port in the conventional circulating fluidized bed gasification furnace is low, partial materials returned to the hearth can enter the lower part of the hearth and are discharged from a bottom slag discharge pipe along with solid particles with large particle size, the retention time is short, and the carbon content of the gasified bottom slag of the circulating fluidized bed is high.
In summary, the following technical defects mainly exist in the conventional oxygen-enriched gasification process of the circulating fluidized bed:
(1) the oxygen-carbon ratio at the bottom of the hearth is high, the heat release amount of combustion is large, the temperature is high, and the bottom of the hearth is a large-particle material with high ash content and is easy to coke at high temperature;
(2) along the height direction of the hearth, the temperature of the hearth is in a descending trend, although the carbon concentration of the upper area of the hearth is high, the temperature is low, so that the gasification reaction is limited, and the oxygen-enriched gasification efficiency of the circulating fluidized bed is influenced;
(3) the carbon content of the ash in the system is high, and the main reasons comprise: on one hand, the temperature distribution is not matched with the gasification reaction, the gasification efficiency is low, the solid particle reaction is incomplete, and the carbon content of the formed ash is high; on the other hand, the bottom of the hearth has high fluidization speed, the retention time of solid particles in an oxidation zone with sufficient oxidant is short, and the carbon content of ash is high due to insufficient reaction; in addition, the back mixing effect of the hearth particles returned by the material returning device to the lower part of the hearth causes that part of high-carbon-content solid particles are discharged together with the bottom slag, so that the carbon content of the gasified bottom slag is high.
Disclosure of Invention
The object of the present invention is to overcome at least partly the drawbacks of the prior art and to provide a new circulating fluidized bed gasification apparatus and a circulating fluidized bed gasification method.
The invention also aims to provide a circulating fluidized bed gasification device and a circulating fluidized bed gasification method, which can reduce the coking problem at the bottom of a hearth.
The invention also aims to provide a circulating fluidized bed gasification device and a circulating fluidized bed gasification method with high gasification efficiency and carbon conversion rate.
The invention also aims to provide a circulating fluidized bed gasification device and a circulating fluidized bed gasification method, wherein the carbon content of bottom slag is lower.
To achieve one of the above objects or purposes, the technical solution of the present invention is as follows:
a gasification device of a circulating fluidized bed comprises a gasification furnace, a gas-solid separator and a material returning device, wherein the gasification furnace is communicated with the gas-solid separator, the gas-solid separator is communicated with the material returning device, the material returning device is communicated with the gasification furnace, a gasification agent inlet, a feeding port, a material returning port and a gasification product outlet are arranged on the gasification furnace, the gasification agent inlet comprises a primary gasification agent inlet and a secondary gasification agent inlet, the primary gasification agent inlet is located at a first position, and the secondary gasification agent inlet is located at a second position different from the first position.
According to a preferred embodiment of the present invention, the primary gasifying agent inlet is located at the bottom of the gasification furnace, and the secondary gasifying agent inlet is located below the middle of the gasification furnace.
According to a preferred embodiment of the invention, the height of the hearth of the gasification furnace is H, and the height of the material returning opening from the bottom of the hearth is H0And 0.1H is not more than H0≤0.3H。
According to a preferred embodiment of the invention, the height of the secondary gasification agent inlet from the bottom of the hearth is h, and h is less than or equal to h0。
According to a preferred embodiment of the present invention, the gasifying agent inlet includes a plurality of secondary gasifying agent inlets, and the plurality of secondary gasifying agent inlets are distributed in the same layer or in multiple layers along the height direction of the gasification furnace.
According to a preferred embodiment of the present invention, projections of the secondary gasifying agent inlets of different layers on a cross section perpendicular to a height direction of the gasification furnace are offset from each other.
According to a preferred embodiment of the present invention, the gasification furnace comprises an oxidation zone, a transition zone and a reduction zone from bottom to top, the diameter of the transition zone and the diameter of the reduction zone are D, and the diameter of the oxidation zone is D1And D is less than or equal to D1。
According to a preferred embodiment of the present invention, the secondary gasification agent inlet is located in the transition zone of the gasifier.
According to a preferred embodiment of the present invention, the gasification furnace includes a throat having a diameter reduced with respect to a main body of the gasification furnace.
According to a preferred embodiment of the invention, the throat is located below the return orifice.
According to another aspect of the present invention, there is provided a circulating fluidized bed gasification method using the circulating fluidized bed gasification apparatus according to any one of the preceding embodiments, the circulating fluidized bed gasification method including:
(1) the fuel enters the gasification furnace from the feeding port, the circulating solid particles containing incompletely reacted carbon enter the gasification furnace from the return port, the primary gasification agent enters the gasification furnace from the primary gasification agent inlet, and the fuel, the return material and the primary gasification agent are subjected to a reaction mainly based on a combustion reaction and release heat;
(2) the secondary gasification agent enters the gasification furnace from the secondary gasification agent inlet, contacts with carbon particles, reacts and releases heat, and simultaneously combusts part of generated combustible gas to release heat;
(3) the gasification product carries the incompletely reacted carbon-containing materials to enter a gas-solid separator from a gasification product outlet;
(4) the circulating solid particles separated by the gas-solid separator are returned to the gasification furnace through a material returning device, and the gasification substances separated by the gas-solid separator are collected.
According to a preferred embodiment of the invention, the fluidization velocity at the bottom of the gasifier is controlled between 1.5m/s and 2.5 m/s.
According to a preferred embodiment of the present invention, the gasification furnace forms an oxidation zone, a transition zone and a reduction zone from bottom to top during operation, and the temperature of the oxidation zone is controlled to be not higher than 950 ℃.
According to a preferred embodiment of the invention, the reaction temperature of the gasifier is between 850 ℃ and 1200 ℃.
According to a preferred embodiment of the invention, the primary gasification agent is air or oxygen-enriched air with an oxygen-enriched concentration of less than 40%, or a mixture of air or oxygen-enriched air with an oxygen-enriched concentration of less than 40% and water vapor.
According to a preferred embodiment of the invention, the secondary gasification agent is oxygen-enriched air or oxygen with oxygen-enriched concentration > 50%, or a mixture of oxygen-enriched air or oxygen and water vapor with oxygen-enriched concentration > 50%.
According to a preferred embodiment of the invention, the proportion of the oxygen in the secondary gasification agent to the total oxygen of the gasification agent is 10% to 60%.
According to the circulating fluidized bed gasification device and the circulating fluidized bed gasification method, the gasification agent does not completely enter from the bottom of the hearth, so that a good partition of the atmosphere and the temperature of the gasification furnace is provided, the temperature of the lower oxidation zone is lower (not more than 950 ℃), and coking caused by over-temperature at the bottom is avoided; the introduction of the secondary gasification agent forms a local high-temperature area, the temperature of a hearth transition area and a reduction area is increased due to radiation and fluidization, heat is provided for the gasification reaction of the areas, the endothermic gasification reaction is promoted, and the gasification efficiency and the carbon conversion rate of the system are increased. FIG. 2 is a graph of the temperature T in the circulating fluidized bed gasification apparatus of the present invention as a function of the hearth height H, and it can be seen that the temperature T in the circulating fluidized bed gasification apparatus does not decrease with the hearth height H.
Meanwhile, the gasification device and the gasification method of the circulating fluidized bed realize reasonable distribution of solid particles in the gasification furnace: the lower fluidization speed of the oxidation zone ensures that the large-particle-size solid particles with high ash content have long retention time in the oxidation zone, can realize full reaction with the gasifying agent, and the small-particle-size solid particles circulate for many times in a circulating system consisting of a gasification furnace hearth, a gas-solid separator and a material returning device and react with the gasifying agent in a high-temperature area of the hearth. The particles with different particle diameters can fully contact and react with the gasifying agent in different areas, so that the gasification efficiency and the carbon conversion rate are improved, and the carbon content of ash and slag of the system is reduced.
The gasification device and the gasification method of the circulating fluidized bed are more suitable for oxygen-enriched gasification of the circulating fluidized bed.
Drawings
FIG. 1 is a graph showing the relationship between the temperature (T) in a conventional circulating fluidized bed furnace, the concentration (theta) of particulate ash and the height (H) of a hearth;
FIG. 2 is a temperature profile of a circulating fluidized bed gasification apparatus of the present invention;
FIG. 3 is a schematic view of a circulating fluidized bed gasification apparatus according to a first embodiment of the present invention;
FIG. 4 is a schematic view of a circulating fluidized bed gasification apparatus according to a second embodiment of the present invention; and
FIG. 5 is a schematic view of a circulating fluidized bed gasification apparatus according to a third embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present invention will hereinafter be described in detail with reference to the accompanying drawings, wherein like or similar reference numerals denote like or similar elements. Furthermore, in the following detailed description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the embodiments of the disclosure. It may be evident, however, that one or more embodiments may be practiced without these specific details. In other instances, well-known structures and devices are shown in schematic form in order to simplify the drawing.
According to the general concept of the present invention, there is provided a circulating fluidized bed gasification apparatus, comprising a gasification furnace, a gas-solid separator and a material returning device, wherein the gasification furnace is communicated with the gas-solid separator, the gas-solid separator is communicated with the material returning device, the material returning device is communicated with the gasification furnace, the gasification furnace is provided with a gasification agent inlet, a feeding port, a material returning port and a gasification product outlet, wherein the gasification agent inlet comprises a primary gasification agent inlet and a secondary gasification agent inlet, the primary gasification agent inlet is located at a first position, and the secondary gasification agent inlet is located at a second position different from the first position.
The gasification furnace comprises an oxidation zone, a transition zone and a reduction zone from bottom to top, wherein the oxidation zone, the transition zone and the reduction zone can have the same cross-sectional area or different cross-sectional areas, for example, the diameter of the transition zone and the diameter of the reduction zone are D, the diameter of the oxidation zone is D1And D is less than or equal to D1。
Specifically, the primary gasifying agent inlet is positioned at the bottom of the gasification furnace, and the secondary gasifying agent inlet is positioned below the middle part of the gasification furnace. Advantageously, said secondary gasification agent inlet is located in the transition zone of the gasifier. The gasifying agent enters the gasification furnace in two stages, and particularly, under the condition that the oxygen concentration of the one-stage gasifying agent is low (for example, air or oxygen-enriched air with the oxygen-enriched concentration less than 40%), compared with the condition that the oxygen-enriched gasifying agent is completely introduced from the bottom, the oxygen-carbon ratio in an oxidation zone is reduced, the heat release quantity is reduced, the temperature of the bottom of a hearth is effectively reduced, and coking caused by high temperature at the bottom of the hearth with higher ash concentration is avoided.
In addition, the secondary gasifying agent forms local high temperature after entering the hearth, and the heat is carried to the upper part of the hearth along with the materials and the fluidized air, so that the temperature of the middle upper part of the hearth is increased, heat is provided for the gasification reaction, the gasification reaction is promoted, and the gasification efficiency and the carbon conversion rate of the system are increased. Particularly, in the case where the oxygen concentration of the secondary gasifying agent is high, the effect is more remarkable.
Preferably, the height of a hearth of the gasification furnace is H, and the height of the material returning opening from the bottom of the hearth is H0And 0.1H is not more than H0Less than or equal to 0.3H. The height of the material returning port is limited, and the problem that the carbon content of the gasified bottom slag of the circulating fluidized bed is high due to too low position of the material returning port is avoided.
Furthermore, the height of the secondary gasification agent inlet from the bottom of the hearth is h, and h is not less than h0. When the secondary gasification agent is introduced below the material returning opening, the carbon-containing solid material returned to the hearth is carried upwards, so that the concentration of the carbon-containing solid particles in the transition region and the reduction region is improved, and the gasification efficiency and the carbon conversion rate of the system are further improved.
The gasifying agent inlet may include a plurality of secondary gasifying agent inlets, and the plurality of secondary gasifying agent inlets may be distributed in the same layer or in multiple layers along the height direction of the gasification furnace. Projections of the secondary gasifying agent inlets of different layers on the section vertical to the height direction of the gasification furnace are staggered with each other. The staggered second-stage gasifying agent inlets are beneficial to the uniform distribution of the gasifying agent.
According to a preferred embodiment of the present invention, the gasification furnace includes a throat having a diameter reduced with respect to a main body of the gasification furnace. Advantageously, the throat is located below the return port. The throat opening is arranged below the material returning opening, so that the internal circulation of an oxidation area at the bottom of the hearth, a transition area at the middle upper part and a reduction area is enhanced, and more definite atmosphere, particle size and temperature division is realized: an oxidation zone with low fluidization speed and low temperature is arranged below the throat, and large-particle materials circulate for many times, so that the carbon content of the bottom slag is reduced; the arrangement of the throat further reduces the back mixing of the returned materials to the lower part of the hearth, improves the concentration of small-particle materials in a high-temperature circulation loop above the throat, promotes gasification reaction, improves gasification efficiency and reduces the carbon content of fly ash.
According to another aspect of the present invention, there is provided a circulating fluidized bed gasification method including:
(1) the fuel enters the gasification furnace from the feeding port, the circulating solid particles containing incompletely reacted carbon enter the gasification furnace from the return port, the primary gasification agent enters the gasification furnace from the primary gasification agent inlet, and the fuel, the return material and the primary gasification agent are subjected to a reaction mainly based on a combustion reaction and release heat;
(2) the secondary gasification agent enters the gasification furnace from the secondary gasification agent inlet, contacts with carbon particles, reacts and releases heat, and simultaneously combusts part of generated combustible gas to release heat;
(3) the gasification product carries the incompletely reacted carbon-containing materials to enter a gas-solid separator from a gasification product outlet;
(4) the circulating solid particles separated by the gas-solid separator are returned to the gasification furnace through a material returning device, and the gasification substances separated by the gas-solid separator are collected.
According to a preferred embodiment of the invention, the fluidization velocity at the bottom of the gasifier is controlled between 1.5m/s and 2.5 m/s. The fluidization velocity at the bottom of the gasifier is controlled so that the larger particles of the circulating material stay in the sufficient oxidation zone of the gasifying agent for a sufficient time to allow the reaction to be more complete.
The gasification furnace forms an oxidation zone, a transition zone and a reduction zone from bottom to top in the operation process, and the temperature of the oxidation zone is controlled to be not higher than 950 ℃. The reaction temperature of the gasification furnace is between 850 ℃ and 1200 ℃. The lower oxidation zone has lower temperature, thus avoiding coking at the bottom due to overtemperature.
Preferably, the primary gasification agent is air or oxygen-enriched air with oxygen-enriched concentration less than 40%, or a mixture of air or oxygen-enriched air with oxygen-enriched concentration less than 40% and water vapor, and the secondary gasification agent is oxygen-enriched air with oxygen-enriched concentration greater than 50%, or a mixture of oxygen-enriched air with oxygen-enriched concentration greater than 50% and water vapor. Advantageously, the proportion of the oxygen in the secondary gasification agent to the total oxygen of the gasification agent is between 10 and 60 percent.
According to the circulating fluidized bed gasification device and the circulating fluidized bed gasification method, the gasification agent does not completely enter from the bottom of the hearth, so that a good partition of the atmosphere and the temperature of the gasification furnace is provided, the temperature of the lower oxidation zone is lower (not more than 950 ℃), and coking caused by over-temperature at the bottom is avoided; the introduction of the secondary gasification agent forms a local high-temperature area, the temperature of a hearth transition area and a reduction area is increased due to radiation and fluidization, heat is provided for the gasification reaction of the areas, the endothermic gasification reaction is promoted, and the gasification efficiency and the carbon conversion rate of the system are increased. FIG. 2 is a graph of the temperature T in the circulating fluidized bed gasification apparatus of the present invention as a function of the hearth height H, and it can be seen that the temperature T in the circulating fluidized bed gasification apparatus does not decrease with the hearth height H.
Meanwhile, the gasification device and the gasification method of the circulating fluidized bed realize reasonable distribution of solid particles in the gasification furnace: the lower fluidization speed of the oxidation zone ensures that the large-particle-size solid particles with high ash content have long retention time in the oxidation zone, can realize full reaction with the gasifying agent, and the small-particle-size solid particles circulate for many times in a circulating system consisting of a gasification furnace hearth, a gas-solid separator and a material returning device and react with the gasifying agent in a high-temperature area of the hearth. The particles with different particle diameters can fully contact and react with the gasifying agent in different areas, so that the gasification efficiency and the carbon conversion rate are improved, and the carbon content of ash and slag of the system is reduced.
The gasification device and the gasification method of the circulating fluidized bed are more suitable for oxygen-enriched gasification of the circulating fluidized bed.
Example one
Fig. 3 is a schematic view of a circulating fluidized bed gasification apparatus according to a first embodiment of the present invention. The oxygen-enriched gasification device of the circulating fluidized bed comprises a gasification furnace 1, a gas-solid separator 2, a downcomer 3, a material returning device 4 and a material returning inclined pipe 5. The hearth is provided with a first-stage gasifying agent inlet a, a second-stage gasifying agent inlet (comprising a first second-stage gasifying agent inlet b1 and a second-stage gasifying agent inlet b2), a feeding port c, a return port d and a gasified product outlet e.
The gasification furnace 1 is divided into a plurality of sections from bottom to top, and sequentially comprises an oxidation zone 1-A, a transition zone 1-B and a reduction zone 1-C. The diameter of the transition zone and the reduction zone is D, the diameter of the oxidation zone is D1D and D1Determined by the fluidization velocity of the zone to which it corresponds, D and D1Can be combined withEtc., wherein the fluidization velocity in the oxidation zone is 2m/s and the fluidization velocity in the lower part of the transition zone is 3.5 m/s. The feeding port c is positioned in the transition zone 1-B, the return port d is positioned at the middle lower part of the transition zone 1-B and is spaced above the primary gasifying agent air distribution point by h0And h is00.15H. In this example, 2 secondary gasifying agent inlets are provided as b1And b2Which are positioned on the same horizontal plane of the hearth. The second-stage gasifying agent inlet is positioned at a position H above the air distribution point of the first-stage gasifying agent, and H is 0.2H. The direction of the secondary gasification agent inlet is vertical to the vertical center line of the hearth.
A first-stage gasifying agent inlet a is located at the bottom of a hearth, 0-6 mm pulverized coal enters the gasification furnace 1 from a feeding port c, large particles enter a lower oxidation zone 1-A, the large particles and the first-stage gasifying agent are subjected to a reaction mainly involving a combustion reaction and release heat, and small particles are carried to enter the middle upper part of the hearth. The primary gasification agent is a mixture of air and steam, and compared with the situation that the oxygen-enriched gasification agent is completely introduced from the bottom of the hearth, the oxygen-carbon ratio in the oxidation zone 1-A and the oxygen concentration in the oxygen-enriched air are reduced, the heat release quantity during combustion is reduced, the temperature of the oxidation zone 1-A is kept between 900 ℃ and 950 ℃, and the overtemperature coking at the bottom of the hearth is avoided.
The fluidizing air speed at the bottom of the hearth is kept at 2m/s, larger particle materials which are not carried to the upper part of the hearth flow in a bubbling state in the oxidation zone 1-A and react with the primary gasifying agent, the retention time of the particles is long, the full reaction of solid particles is promoted, and the carbon content of bottom slag is reduced.
The small-particle-size solid particles and heat move from bottom to top in the hearth, and in the process, the gasifying agent is gradually consumed and enters a reduction zone 1-C mainly based on gasification reaction after passing through a transition zone 1-B. The secondary gasifying agent is a mixture of oxygen and water vapor, enters the gasification furnace 1 from a secondary gasifying agent inlet of the transition zone, contacts with high-concentration carbon particles, performs a reaction mainly based on oxidation and releases heat, and burns part of generated combustible gas to form a local high-temperature area, so that the gasification reaction near the area is promoted. Meanwhile, heat at the local high temperature is carried to the upper part of the hearth under the action of heat radiation and fluidization, so that the temperature of the middle upper part of the hearth is increased. Since the gasification reaction is endothermic, the increase in temperature provides heat for the gasification reaction in the region above it, promoting the progress of the gasification reaction, thereby increasing the gasification efficiency and carbon conversion rate of the system.
The generated coal gas carries the carbon-containing materials which are not completely reacted to enter a gas-solid separator 2 from a gasification product outlet e, most particles are collected and return to a hearth through a downcomer 3, a material returning device 4 and a material returning inclined pipe 5 in sequence, the reaction is continuously and circularly participated, and a small part of the particles escape from the gas-solid separator 2 to enter a subsequent cooling and purifying system.
Wherein, the first-stage gasifying agent is a mixture of air and steam, the steam amount is adjusted according to the requirements of the fluidization speed and the temperature at the bottom of the hearth, and the second-stage gasifying agent is a mixture of oxygen and steam. The proportion of oxygen in the secondary gasification agent to the total oxygen of the system is 30%.
Example two
FIG. 4 is a schematic view of a circulating fluidized bed gasification apparatus according to a second embodiment of the present invention. The oxygen-enriched gasification device of the circulating fluidized bed comprises a gasification furnace 1, a gas-solid separator 2, a downcomer 3, a material returning device 4 and a material returning inclined pipe 5. The hearth is provided with a first-stage gasifying agent inlet a, a second-stage gasifying agent inlet (comprising a first second-stage gasifying agent inlet b1, a second-stage gasifying agent inlet b2, a third second-stage gasifying agent inlet b3 and a fourth second-stage gasifying agent inlet b4), a feeding port c, a return port d and a gasified product outlet e.
The gasification furnace 1 is divided into a plurality of sections from bottom to top, and sequentially comprises an oxidation zone 1-A, a transition zone 1-B and a reduction zone 1-C. The diameters of the transition region 1-B and the reduction region 1-C of the gasification furnace 1 are both D, and the diameter of the oxidation region 1-A is D1D and D1Determined by the fluidization velocity of the corresponding area, D is less than or equal to D1. Wherein the fluidization velocity of the oxidation zone is 1.5m/s, and the fluidization velocity of the lower part of the transition zone is 3.8 m/s. The feeding port c is positioned at the upper part of the oxidation area 1-A; the return port d is positioned at the middle lower part of the transition zone 1-B and is spaced above the air distribution point of the first-stage gasifying agent by h0And h is00.2H. In this example, 4 secondary gasifying agent inlets are provided as b1～b4Which are positioned on the same horizontal plane of the hearth and are uniformly arranged in a circumference way. The second-stage gasifying agent inlet is positioned at the position h above the air distribution point of the first-stage gasifying agent,and H is 0.18H. The direction of the secondary gasification agent inlet is vertical to the vertical center line of the hearth.
The first-stage gasifying agent inlet a is positioned at the bottom of the hearth, 0-6 mm pulverized coal enters the gasification furnace 1 from the feeding port c, and reacts with the first-stage gasifying agent in the oxidation zone 1-A mainly through a combustion reaction, and heat is released. The air quantity of the primary gasification agent is adjusted, the fluidization air speed at the bottom of the hearth is kept at 1.5m/s, large-particle materials which are not carried into the upper part of the hearth flow in a bubbling state in the oxidation zone 1-A and react with the primary gasification agent, the retention time of the particles is long, the full reaction of solid particles is promoted, and the carbon content of the discharged bottom slag is low. The steam quantity is adjusted, the temperature in the oxidation zone 1-A is kept to be not higher than 950 ℃, and coking of particles with high bottom ash concentration due to high temperature is avoided.
The small particle pulverized coal and the carbon-containing solid particles returned to the hearth from the material returning port d move in the hearth from bottom to top under the carrying of the gas-solid mixture, and in the process, the gasifying agent is gradually consumed and enters the reduction zone 1-C mainly for gasification reaction after passing through the transition zone 1-B. The secondary gasifying agent enters the gasification furnace 1 from the secondary gasifying agent inlet of the transition zone, contacts with high-concentration carbon particles, generates oxidation-based reaction and releases heat, and burns part of generated combustible gas to form a local high-temperature area, so that the gasification reaction near the area is promoted. Meanwhile, heat at the local high temperature is carried to the upper part of the hearth under the action of heat radiation and fluidization, so that the temperature of the middle upper part of the hearth is increased. Since the gasification reaction is endothermic, the increase in temperature provides heat for the gasification reaction in the region above it, promoting the progress of the gasification reaction, thereby increasing the gasification efficiency and carbon conversion rate of the system.
The generated coal gas carries the carbon-containing materials which are not completely reacted to enter a gas-solid separator 2 from a gasification product outlet e, most particles are collected and return to a hearth through a downcomer 3, a material returning device 4 and a material returning inclined pipe 5 in sequence, and a small part of the particles escape from the gas-solid separator 2 to enter a subsequent cooling and purifying system.
The carbon-containing solid particles returned to the gasification furnace 1 from the material returning port d continuously and circularly participate in the reaction, and as the secondary gasification agent inlet is arranged below the material returning port C, more returned materials are carried into the area above the material returning port C, so that the particle amount of the returned materials entering the bottom oxidation area 1-A in a back mixing manner is reduced, the concentration of the carbon-containing solid particles in the hearth transition area 1-B and the reduction area 1-C is improved, the gasification reaction is promoted, the retention time of the solid particles is prolonged, the carbon conversion rate is improved, and the carbon content of fly ash is reduced.
Wherein, the primary gasification agent is a mixture of air and oxygen, the oxygen-enriched concentration is 30 percent, and water vapor is introduced to adjust the temperature and the fluidization speed in the bottom oxidation zone 1-A; the secondary gasification agent is oxygen-enriched air with oxygen-enriched concentration of 60%, and water vapor is introduced to adjust the fluidization speed and temperature.
EXAMPLE III
FIG. 5 is a schematic view of a circulating fluidized bed gasification apparatus according to a third embodiment of the present invention. The oxygen-enriched gasification device of the circulating fluidized bed comprises a gasification furnace 1, a gas-solid separator 2, a downcomer 3, a material returning device 4 and a material returning inclined pipe 5. The hearth is provided with a first-stage gasifying agent inlet a, a second-stage gasifying agent inlet (comprising a first second-stage gasifying agent inlet b1, a second-stage gasifying agent inlet b2, a third second-stage gasifying agent inlet b3 and a fourth second-stage gasifying agent inlet b4), a feeding port c, a material returning port d, a gasified product outlet e and a throat f.
The gasification furnace 1 is divided into a plurality of sections from bottom to top, and sequentially comprises an oxidation zone 1-A, a transition zone 1-B and a reduction zone 1-C. The diameters of the transition region 1-B and the reduction region 1-C of the gasification furnace 1 are both D, and the diameter of the oxidation region 1-A is D1D and D1Determined by the fluidization velocity of the corresponding area, D is less than or equal to D1. Wherein the fluidization velocity of the oxidation zone is 2.0m/s, and the fluidization velocity of the lower part of the transition zone is 3.8 m/s. Diameter D of the minimum part of the throat f20.6D. The feeding port is positioned at the upper part of the oxidation area 1-A; the material returning port is positioned at the middle lower part of the transition zone 1-B and is spaced above the air distribution point of the first-stage gasifying agent by h0And h is00.18H. The throat opening is positioned at the lower part of the transition area 1-B and below the material returning opening. In this example, 4 secondary gasifying agent inlets are provided as b1～b4Which are positioned on the same horizontal plane of the hearth and are uniformly arranged in a circumference way. The second-stage gasifying agent inlet is positioned at a position H above the air distribution point of the first-stage gasifying agent, and H is 0.25H. The secondary gasifying agent enters the hearth through the vertical gasifying furnace 1.
The first-stage gasifying agent inlet a is positioned at the bottom of the hearth, 0-6 mm pulverized coal enters the gasification furnace 1 from the feeding port c, and reacts with the first-stage gasifying agent in the oxidation zone 1-A mainly through a combustion reaction, and heat is released. The air quantity of the primary gasification agent is adjusted, the fluidization air speed of the oxidation zone is kept at 2.0m/s, large-particle materials which are not carried into the upper part of the hearth flow in a bubbling state in the oxidation zone 1-A and react with the primary gasification agent, the retention time of the particles is long, the full reaction of solid particles is promoted, and the carbon content of the discharged bottom slag is low. The steam quantity is adjusted, the temperature in the oxidation zone 1-A is kept to be not higher than 950 ℃, and coking of particles with high bottom ash concentration due to high temperature is avoided.
The small particle pulverized coal and the carbon-containing solid particles returned to the hearth from the material returning port d move in the hearth from bottom to top under the carrying of the gas-solid mixture, and in the process, the gasifying agent is gradually consumed and enters the reduction zone 1-C mainly for gasification reaction after passing through the transition zone 1-B. The secondary gasifying agent enters the gasification furnace 1 from the secondary gasifying agent inlet of the transition zone, contacts with high-concentration carbon particles, generates oxidation-based reaction and releases heat, and burns part of generated combustible gas to form a local high-temperature area, so that the gasification reaction near the area is promoted. Meanwhile, heat at the local high temperature is carried to the upper part of the hearth under the action of heat radiation and fluidization, so that the temperature of the middle upper part of the hearth is increased. Since the gasification reaction is endothermic, the increase in temperature provides heat for the gasification reaction in the region above it, promoting the progress of the gasification reaction, thereby increasing the gasification efficiency and carbon conversion rate of the system.
The throat f arranged on the gasification furnace 1 reduces the back mixing of small particle materials to the lower part of the hearth, improves the solid particle concentration of a transition region and a reduction region, promotes the gasification reaction of a high-temperature region at the middle upper part of the hearth, improves the gasification efficiency and the carbon conversion rate, and reduces the carbon content of fly ash; on the other hand, the circulation of large-particle solid materials in an oxidation zone is enhanced, the retention time is prolonged, and the carbon content of bottom slag is reduced.
The generated coal gas carries the carbon-containing materials which are not completely reacted to enter a gas-solid separator 2 from a gasification product outlet e, most particles are collected and return to a hearth through a downcomer 3, a material returning device 4 and a material returning inclined pipe 5 in sequence, and a small part of the particles escape from the gas-solid separator 2 to enter a subsequent cooling and purifying system.
Wherein, the primary gasification agent is oxygen-enriched air with oxygen-enriched concentration of 25 percent, and water vapor is introduced to adjust the temperature and the fluidization speed in the bottom oxidation zone 1-A; the secondary gasification agent is oxygen-enriched air with oxygen-enriched concentration of 70%, and water vapor is introduced to adjust the fluidization speed and temperature.
Example four
The following takes pulverized coal as an example to specifically describe the oxygen-enriched gasification method of the circulating fluidized bed in one embodiment, and the method comprises the following steps:
(1) the pulverized coal is fed into the hearth from a coal feeding port, circulating solid particles containing a large amount of incompletely reacted carbon enter the hearth from a material returning port, a primary gasifying agent enters the hearth from a primary gasifying agent inlet at the bottom of the hearth, and the pulverized coal, the returning material and the primary gasifying agent undergo a reaction mainly comprising a combustion reaction and release heat;
(2) the fluidization speed at the bottom of the hearth is low (1.5-2.5 m/s), so that large-particle materials are not carried into the upper part of the hearth, but continuously react with the first-stage gasification agent in a bubbling fluidization state in an oxidation zone at the bottom of the hearth; the proportion and the composition of the first-stage gasifying agent are adjusted, and the temperature of the oxidation zone is controlled to be not higher than 950 ℃.
(3) The unreacted first stage gasifying agent and the generated gas carry the incompletely reacted small particle carbon containing material and heat to move from bottom to top in the hearth, the oxidant is gradually consumed in the process, the reaction in the hearth is gradually changed into the reaction mainly based on gasification, and the gasification reaction absorbs heat to consume the heat released by the combustion reaction.
(4) The second-stage gasifying agent enters the hearth from the second-stage gasifying agent inlet, contacts with high-concentration carbon particles, reacts and releases heat, meanwhile, part of generated combustible gas is combusted to release heat, and the released heat forms a local high-temperature area (the highest temperature can reach 1200 ℃) in the area near the second-stage gasifying agent inlet;
(5) the heat released by the reaction of the secondary gasifying agent and the combustible is carried to the upper part of the hearth under the action of thermal radiation and fluidization, so that the temperature of the middle upper part of the hearth is increased, heat is provided for the gasification reaction of the region, and the gasification reaction is promoted to be carried out;
(6) the generated coal gas carries the carbon-containing materials which are not completely reacted to enter a gas-solid separator from a gasification product outlet, most particles are collected and returned to the hearth through a material returning device, and a small part of the particles escape from the gas-solid separator to enter a subsequent cooling and purifying system.
(7) Most of the small-particle carbon-containing solid materials returned from the material returning port are carried to move to the upper part of the hearth and continue to circularly participate in the reaction, and a part of the small-particle carbon-containing materials are back-mixed and enter the lower part of the hearth.
Furthermore, the introduction of the secondary gasification agent is carried out at a position below the material returning port, the fluidization speed at the material returning port is improved, and more materials returned by the material returning port are carried into an area above the material returning port to participate in multiple circulation.
Preferably, a throat is arranged below the material returning port, and the arrangement of the throat enables small-particle materials returned by the material returning port to move towards the upper part of the hearth more under the structural constraint and high fluidization speed action of the throat, so that the back mixing of the returned materials towards the lower part of the hearth is reduced, and the concentration of the small-particle materials in a high-temperature circulation loop above the throat is improved.
It should be noted that, by adjusting the diameter of the hearth and the distribution ratio of the gasifying agent, the lower fluidization speed of the oxidation zone at the bottom of the hearth can be maintained, the residence time of large-particle solid materials in the oxidation zone can be prolonged, the full reaction of the large-particle solid materials can be ensured, and the carbon content of bottom slag can be reduced.
Although embodiments of the present invention have been shown and described, it would be appreciated by those skilled in the art that changes may be made in these embodiments without departing from the principles and spirit of the invention. The scope of applicability of the present invention is defined by the appended claims and their equivalents.
List of reference numerals:
1 gasification furnace
2 gas-solid separator
3 down pipe
4 material returning device
5 return inclined tube
1-A oxidation zone
1-B transition region
1-C reduction zone
a first stage gasifying agent inlet
b1 first and second gasifying agent inlets
b2 second stage gasifying agent inlet
b3 third stage gasifying agent inlet
b4 fourth stage gasifying agent inlet
c feeding port
d material returning port
e outlet for gasification products
f, the throat.
Claims (11)
1. The utility model provides a circulating fluidized bed gasification equipment, includes gasifier, gas-solid separator and returning charge ware, gasifier and gas-solid separator intercommunication, gas-solid separator and returning charge ware intercommunication, returning charge ware and gasifier intercommunication, its characterized in that:
the gasification furnace is provided with a gasification agent inlet, a feeding port, a material returning port and a gasification product outlet, wherein the gasification agent inlet comprises a primary gasification agent inlet and a secondary gasification agent inlet, the primary gasification agent inlet is positioned at a first position, the secondary gasification agent inlet is positioned at a second position different from the first position,
wherein the gasification furnace comprises a throat with a diameter reduced relative to the main body of the gasification furnace,
wherein the throat is positioned below the material returning port,
wherein the gasification furnace is divided into an oxidation zone, a transition zone and a reduction zone from bottom to top, a throat is positioned at the lower part of the transition zone, the throat is in a '> <' type structure,
the primary gasification agent is air or oxygen-enriched air with oxygen-enriched concentration less than 40%, or a mixture of air or oxygen-enriched air with oxygen-enriched concentration less than 40% and water vapor, the secondary gasification agent is oxygen-enriched air with oxygen-enriched concentration greater than 50%, or a mixture of oxygen and water vapor, and the fluidization speed at the bottom of the gasification furnace is controlled to be 1.5 m/s-2.5 m/s.
2. The circulating fluidized bed gasification apparatus of claim 1, wherein: the secondary gasification agent inlet is positioned below the middle part of the gasification furnace.
3. The circulating fluidized bed gasification apparatus of claim 2, wherein: the height of the hearth of the gasification furnace is H, and the height of the material returning opening from the bottom of the hearth is H0And 0.1H is not more than H0≤0.3H。
4. The circulating fluidized bed gasification apparatus according to claim 3, wherein: the height of the secondary gasification agent inlet from the bottom of the hearth is h, and h is not more than h0。
5. The circulating fluidized bed gasification apparatus of claim 1, wherein: the gasification agent inlet comprises a plurality of secondary gasification agent inlets, and the plurality of secondary gasification agent inlets are distributed on the same layer or distributed on multiple layers along the height direction of the gasification furnace.
6. The circulating fluidized bed gasification apparatus of claim 5, wherein: projections of the secondary gasifying agent inlets of different layers on the section vertical to the height direction of the gasification furnace are staggered with each other.
7. The circulating fluidized bed gasification apparatus of claim 1, wherein: the gasification furnace comprises an oxidation zone, a transition zone and a reduction zone from bottom to top, the diameters of the transition zone and the reduction zone are D, and the diameter of the oxidation zone is D1And D is less than or equal to D1。
8. A circulating fluidized bed gasification method using the circulating fluidized bed gasification apparatus according to any one of claims 1 to 7, characterized in that: the circulating fluidized bed gasification method comprises the following steps:
(1) the fuel enters the gasification furnace from the feeding port, the circulating solid particles containing incompletely reacted carbon enter the gasification furnace from the return port, the primary gasification agent enters the gasification furnace from the primary gasification agent inlet, and the fuel, the return material and the primary gasification agent are subjected to a reaction mainly based on a combustion reaction and release heat;
(2) the secondary gasification agent enters the gasification furnace from the secondary gasification agent inlet, contacts with carbon particles, reacts and releases heat, and simultaneously combusts part of generated combustible gas to release heat;
(3) the gasification product carries the incompletely reacted carbon-containing materials to enter a gas-solid separator from a gasification product outlet;
(4) the circulating solid particles separated by the gas-solid separator are returned to the gasification furnace through a material returning device, the gasification substances separated by the gas-solid separator are collected,
the fluidization speed of the bottom of the gasification furnace is controlled to be 1.5 m/s-2.5 m/s, wherein the primary gasification agent is air or oxygen-enriched air with oxygen-enriched concentration less than 40 percent, or a mixture of air or oxygen-enriched air with oxygen-enriched concentration less than 40 percent and water vapor, and the secondary gasification agent is oxygen-enriched air with oxygen-enriched concentration greater than 50 percent, or a mixture of oxygen and water vapor.
9. The circulating fluidized bed gasification process of claim 8, wherein: the gasification furnace forms an oxidation zone, a transition zone and a reduction zone from bottom to top in the operation process, and the temperature of the oxidation zone is controlled to be not higher than 950 ℃.
10. The circulating fluidized bed gasification process of claim 8, wherein: the reaction temperature of the gasification furnace is between 850 ℃ and 1200 ℃.
11. The circulating fluidized bed gasification process of claim 8, wherein: the proportion of oxygen in the secondary gasification agent to the total oxygen of the gasification agent is 10-60%.
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