CN109054900B - Coal gasification method and system - Google Patents
Coal gasification method and system Download PDFInfo
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- CN109054900B CN109054900B CN201810940301.0A CN201810940301A CN109054900B CN 109054900 B CN109054900 B CN 109054900B CN 201810940301 A CN201810940301 A CN 201810940301A CN 109054900 B CN109054900 B CN 109054900B
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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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—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
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/006—Starting from ores containing non ferrous metallic oxides
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
Abstract
The invention provides a coal gasification method and a coal gasification system, relates to the technical field of coal chemical industry, realizes oxygen supply for a coal gasification process, obtains a product containing simple substance iron and a titanium-containing substance, and reduces the coal gasification cost. The coal gasification method comprises the steps of placing the ilmenite into an oxidation reactor, and introducing oxygen-containing gas to carry out oxidation reaction on the ilmenite to obtain oxygen-loaded ilmenite; placing the oxygen-loaded ilmenite and raw coal in a reduction reactor, wherein the oxygen-loaded ilmenite provides oxygen, the raw coal is subjected to a coal gasification reaction, and the oxygen-loaded ilmenite is subjected to a reduction reaction to generate elemental iron; carrying out gas flow to remove a part of products in the reduction reactor, and separating the products carried by the gas flow to obtain combustible gas, simple substance iron and titanium-containing substances; returning the residual product to the oxidation reactor for oxygen loading again for coal gasification reaction in the reduction reactor. The coal gasification method and the coal gasification system are applied to the field of coal gasification by adopting chemical chain gasification reaction.
Description
Technical Field
The invention relates to the technical field of coal chemical industry, in particular to a coal gasification method and a coal gasification system.
Background
The chemical chain gasification reaction is one of coal gasification methods, and the basic principle is that the traditional gasification process of direct contact reaction of fuel and air is decomposed into 2 gas-solid reactions by the action of an oxygen carrier: air reaction and fuel gasification reaction. In the reaction process, the fuel does not need to be in contact with the air, and the oxygen carrier transfers the oxygen in the air to the fuel.
In the coal chemical chain gasification reaction, coal is not directly contacted with air in a gasification furnace, water vapor is used as a gasification medium, and oxygen and heat are transferred through circulation of an oxygen carrier between an air reactor and a gasification reactor, so that the non-contact gasification reaction of the coal and the air is completed.
Since the oxygen carrier needs to be continuously circulated between the air reaction and the fuel gasification reaction, it is required that the higher the oxygen carrying capacity and the mechanical strength of the oxygen carrier, the better. Although the artificially prepared oxygen carrier meets the requirements on oxygen carrying capacity and mechanical strength, the preparation cost is high, so that the coal gasification cost is high; the natural oxygen carrier has low cost, but the mechanical strength is low, so that the consumption of the oxygen carrier is relatively high in the coal gasification process, and the coal gasification cost is increased indirectly.
Disclosure of Invention
In view of the above problems in the prior art, embodiments of the present invention provide a coal gasification method and system to reduce the cost of coal gasification.
In order to achieve the above purpose, the embodiment of the invention adopts the following technical scheme:
in a first aspect, an embodiment of the present invention provides a coal gasification method, including: putting the ilmenite into an oxidation reactor, and introducing oxygen-containing gas to perform oxidation reaction on the ilmenite so as to obtain oxygen-loaded ilmenite; placing the oxygen-loaded ilmenite and raw coal in a reduction reactor, and introducing steam, wherein the oxygen-loaded ilmenite provides oxygen, the raw coal is subjected to coal gasification reaction, and the oxygen-loaded ilmenite is subjected to reduction reaction to generate elemental iron; carrying out gas flow to remove a part of products in the reduction reactor, and separating the products carried out by the gas flow to obtain combustible gas, elemental iron and titanium-containing substances; returning the product which is not carried out by the gas flow to the oxidation reactor, and carrying out oxygen loading again to be used for the coal gasification reaction in the reduction reactor again.
In some embodiments, the ilmenite ore has a particle size of 0.5 to 3mm, and the raw coal has a particle size of 2 to 10 mm.
In some embodiments, the gas flow in the oxidation reactor has a gas velocity of 0.5 to 2m/s and a temperature of 1000 to 1100 ℃.
In some embodiments, the gas flow in the reduction reactor has a gas velocity of 1 to 5m/s and a temperature of 700 to 900 ℃.
In some embodiments, the particle size of the solid particles in a portion of the product in the reduction reactor carried over with the gas stream is less than or equal to 0.5 mm.
In some embodiments, the step of separating the products carried over by the gas stream to obtain the combustible gas, elemental iron, and titaniferous material comprises: carrying out gas-solid separation on the product carried by the airflow, extracting to obtain combustible gas, and discharging a product containing elemental iron and a titanium-containing substance; carrying out magnetic separation on the product containing the elemental iron and the titanium-containing substance, extracting to obtain the elemental iron, and discharging the product containing the titanium-containing substance; and (3) carrying out flotation and/or gravity separation on the product containing the titanium-containing substance, and extracting to obtain the titanium-containing substance.
In some embodiments, between the step of placing the ilmenite ore in an oxidation reactor and introducing an oxygen-containing gas and the step of placing the oxygen-loaded ilmenite ore and raw coal in a reduction reactor and introducing steam, further comprising: and carrying out gas-solid separation on the product in the oxidation reactor to obtain oxygen-poor gas and oxygen-loaded ilmenite, discharging the oxygen-poor gas, and introducing the oxygen-loaded ilmenite into the reduction reactor.
In some embodiments, the coal gasification method further comprises: discharging the residual product in the reduction reactor out of the reduction reactor; wherein the residual product is a product in the reduction reactor that is neither carried over by the gas stream nor returned to the oxidation reactor.
In a second aspect, the present invention provides a coal gasification system comprising: the oxidation reactor is used for carrying out oxidation reaction on the ilmenite and oxygen-containing gas to obtain the oxygen-loaded ilmenite; a reduction reactor for supplying oxygen to the oxygen-loaded ilmenite, coal gasification reaction of raw coal occurs, and the oxygen-loaded ilmenite undergoes reduction reaction to generate elemental iron; and the first separation equipment is used for separating a product brought out by the airflow in the reduction reactor to obtain combustible gas, elemental iron and a titanium-containing substance.
In some embodiments, the oxidation reactor is provided with a first feed inlet for feeding the ilmenite, a gas inlet for feeding an oxygen-containing gas, and a discharge outlet for discharging the product in the oxidation reactor.
The reduction reactor is provided with a first feed inlet for introducing the oxygen-loaded ilmenite, a second feed inlet for introducing the raw coal, an air inlet for introducing the water vapor and a first discharge outlet for discharging a product brought out by the airflow in the reduction reactor.
The coal gasification system further comprises: and the second separation equipment is connected between the discharge hole of the oxidation reactor and the first feed hole of the reduction reactor and is used for carrying out gas-solid separation on the product in the oxidation reactor to obtain oxygen-poor gas and oxygen-loaded ilmenite, discharging the oxygen-poor gas and introducing the oxygen-loaded ilmenite into the reduction reactor.
In some embodiments, the oxidation reactor is further provided with a second feed inlet for the reduced ilmenite ore that is passed into the reduction reactor.
The reduction reactor is also provided with a second discharge port for discharging reduced ilmenite.
And the second feed inlet of the oxidation reactor is communicated with the second discharge outlet of the reduction reactor.
In some embodiments, the first separation apparatus comprises: the cyclone separator is connected with the reduction reactor and is used for carrying out gas-solid separation on a product brought out by the airflow in the reduction reactor, extracting to obtain combustible gas and discharging a product containing elemental iron and titanium-containing substances; the magnetic separator is connected with the cyclone separator and is used for carrying out magnetic separation on the product containing the elemental iron and the titanium-containing substances, extracting the elemental iron and discharging the product containing the titanium-containing substances; and the flotation separator and/or gravity separator is connected with the magnetic separator and is used for performing flotation and/or gravity separation on the product containing the titanium-containing substance to extract the titanium-containing substance.
The coal gasification method and the coal gasification system provided by the invention can produce the following beneficial effects:
the method has the advantages that the cheap and easily-obtained ilmenite is used as the oxygen carrier to carry oxygen to the coal gasification reaction, oxygen required by the coal gasification reaction is provided, the characteristics that the ilmenite is easy to oxidize and reduce are utilized, oxygen is supplied to the coal gasification reaction, products containing simple substance iron and titanium-containing substances are obtained, the simple substance iron and the titanium-containing substances with high purity can be obtained through separation of the simple substance iron and the titanium-containing substances, so that economic benefits are brought, the defect of cost increase caused by large oxygen carrier consumption due to the use of a natural oxygen carrier is overcome, and the purpose of reducing the coal gasification reaction cost is realized.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a flow diagram of a coal gasification process provided in accordance with certain embodiments of the present invention;
FIG. 2 is a flow diagram of a coal gasification process according to further embodiments of the present invention;
FIG. 3 is a block diagram of a coal gasification system according to still other embodiments of the present invention.
Description of reference numerals:
1-an oxidation reactor; 11-a first feed inlet of an oxidation reactor;
12-the gas inlet of the oxidation reactor; 13-a second feed inlet to the oxidation reactor;
14-discharge of the oxidation reactor; 2-a reduction reactor;
21-a first feed inlet of the reduction reactor; 22-a second feed inlet of the reduction reactor;
23-gas inlet of the reduction reactor; 24-a first discharge port of the reduction reactor;
25-a second discharge port of the reduction reactor; 26-a third discharge outlet of the reduction reactor;
3-a second separation device; 31-feed inlet of second separation device;
32-the gas outlet of the second separation device; 33-discharge of the second separation device;
4-a first separation device; 5-a first-stage separation device;
51-feed inlet of the first stage separation device; 52-outlet of the first stage separation device;
53-discharge port of first-stage separation device; 6-a secondary separation device;
61-feed inlet of the secondary separation device; 62-a first discharge port of the secondary separation device;
63-a second discharge port of the secondary separation device; 7-a third-stage separation device;
71-feed inlet of the tertiary separation device; 72-a first discharge port of the third stage separation device;
73-a second discharge port of the tertiary separation device.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
An embodiment of the present invention provides a coal gasification method, as shown in fig. 1 to 3, including the steps of:
step S1: the titanic iron ore is placed in an oxidation reactor 1, oxygen-containing gas is introduced to carry out oxidation reaction on the titanic iron ore, and the titanic iron ore loaded with oxygen is obtained.
In the above step S1, the main chemical reaction process performed in the oxidation reactor 1 includes:
2Me+O2→2MeO；
wherein Me is a general abbreviation of metal elements, and Me mainly comprises iron (Fe) in the titanic iron ore.
In the step S1, the iron atoms on the surface of the ilmenite are oxidized into high-valence iron, and the ilmenite is in solid solution at high temperature (about 1000 ℃), the iron atoms inside the ilmenite migrate to the surface and are oxidized, and the ilmenite framework remains intact. The oxidation reaction causes the grains of the ilmenite to grow and the internal porosity of the ilmenite to become greater, which can increase the degree to which the ilmenite is mechanically pulverized during the circulation between the oxidation reactor and the reduction reactor.
In some embodiments, the ilmenite ore of step S1 above may have a titanium iron content of less than or equal to 30% by mass, with the balance being gangue. The gangue can be used as a good heat accumulator and carries heat to circulate between the oxidation reactor 1 and the reduction reactor 2, so that heat is provided for the coal gasification reaction, the unit energy consumption is reduced, and the utilization rate of the fuel heat value is improved.
In some embodiments, in the step S1, the oxygen-containing gas participating in the oxidation reaction may be air, which has the advantages of easy availability and low cost, and can save cost.
In the step S1, the particle size of the ilmenite ore may affect the quality of the oxidation reaction, and the large particle size of the ilmenite ore makes the ilmenite ore not easily contact with the oxygen-containing gas, which results in a long reaction time and insufficient reaction; too small a particle size of the ilmenite ore increases the processing cost of the ilmenite ore, indirectly increasing the cost of the coal gasification reaction. In some embodiments, the titaniferous ore that participates in the oxidation reaction may have a particle size in the range of 0.5 to 3mm, in which range more iron in the titaniferous ore may be oxidized and the titaniferous ore particles are easier to process.
In the step S1, the gas velocity of the gas flow in the oxidation reactor 1 also affects the quality of the oxidation reaction, because, on the one hand, reasonable disturbance of the gas velocity can improve the uniformity of the oxidized ilmenite and increase the mechanical pulverization degree of the ilmenite; on the other hand, the excess oxygen-containing gas helps to enable more ilmenite to be loaded with oxygen, increasing the carbon conversion in the subsequent coal gasification reaction. In some embodiments, the gas flow rate of the gas flow in the oxidation reactor 1 can be controlled to be 0.5-2 m/s, and in this gas flow rate range, the ilmenite can be uniformly oxidized, the mechanical pulverization degree is higher, and the carbon conversion rate in the subsequent coal gasification reaction is improved.
In the step S1, the temperature in the oxidation reactor 1 may also affect the quality of the oxidation reaction, and the proper temperature can ensure that iron atoms in the ilmenite are easier to migrate to the surface of the ilmenite, and can also ensure that the skeleton of the ilmenite is complete, the iron atoms migrated to the surface of the ilmenite are oxidized by the oxygen-containing gas, and the iron atoms in the ilmenite are continuously oxidized along with the reaction, thereby finally completing the process of loading oxygen in the ilmenite. The temperature in the oxidation reactor may be controlled by controlling the amount of heat-carrying products such as ilmenite and semicoke recycled into the oxidation reactor in the reduction reactor 2, and the temperature at which the environment in the oxidation reactor 1 is heated. In some embodiments, the temperature can be controlled to be 1000-1100 ℃, and the oxidation reaction is relatively sufficient in the temperature range.
In the step S1, the reaction time in the oxidation reactor 1 also affects the quality of the oxidation reaction, and the reaction time is too short, so that the oxidation reaction is insufficient, which affects the amount of oxygen carried by the ilmenite, and thus the efficiency of the whole coal gasification reaction; the reaction time is too long, and the ineffective reaction time in the oxidation reaction can cause resource waste. In some embodiments, the reaction time of the ilmenite in the oxidation reactor is controlled to be 5-20 minutes, and in this time range, the reaction of the ilmenite and the oxygen-containing gas can be relatively sufficient, and the waste of resources caused by ineffective reaction time is avoided.
As shown in fig. 2 and 3, in some embodiments, after the step S1, the following steps may be further included: and (3) carrying out gas-solid separation on the product in the oxidation reactor 1 to obtain oxygen-poor gas and oxygen-loaded ilmenite, discharging the oxygen-poor gas, and introducing the oxygen-loaded ilmenite into the reduction reactor 2.
In the above steps, the gas-solid separation of the product in the oxidation reactor 1 can be performed by adopting a cyclone separator, and the cyclone separator has the advantages of simple structure, low cost, convenient maintenance and the like.
Step S2: the oxygen-loaded ilmenite and the raw coal are placed in a reduction reactor 2, steam is introduced, the oxygen-loaded ilmenite provides oxygen, the raw coal undergoes a coal gasification reaction, and the oxygen-loaded ilmenite undergoes a reduction reaction to form elemental iron.
In the above step S2, the main chemical reaction process performed in the reduction reactor 2 includes:
C+H2O→CO+H2；
MeO+CO→Me+CO2；
MeO+H2→Me+H2O；
CO+3H2→CH4+H2O；
in step S2, the pyrolysis product of the raw coal includes CO and H2And the reducing substance, the oxygen-loaded ilmenite provides oxygen and heat to react with the reducing substance, and the iron-containing oxide in the oxygen-loaded ilmenite is reduced to elemental iron by the reducing substance. In the process of reducing the oxygen-loaded ilmenite, due to the diffusion effect, iron oxide on the surface of the ilmenite particles is always reduced first, while iron oxide inside the ilmenite particles migrates towards the particle surface, and the migration is accompanied by reduction, so that the pores inside the ilmenite particles are continuously increased, and the ilmenite particles become loose, so that the ilmenite particles are more easily pulverized mechanically.
In step S2, the temperature in the reduction reactor 2 may affect the quality of the coal gasification reaction, and the coal gasification reaction may not be sufficient or even occur due to too low temperature in the reduction reactor 2; the temperature in the reduction reactor 2 is too high to facilitate the coal gasification reaction. In some embodiments, the temperature in the reduction reactor 2 may be controlled to 700 to 900 ℃, and in this temperature range, the coal gasification reaction may be sufficient. It is noted that at least a portion of the heat used to maintain the temperature within the reduction reactor 2 may be supplied by the heat carried by the product discharged from the oxidation reactor 1, including the oxygen-laden ilmenite ore.
In the above step S2, the gas flow rate of the gas flow in the reduction reactor 2 also affects the quality of the coal gasification reaction and the reduction reaction, because the gas flow in the reduction reactor 2 plays a role of bringing the product in the reduction reactor 2 to the first separation device 4, and on the other hand, the gas flow in the reduction reactor 2 helps to uniformly mix the substances in the coal gasification reaction, thereby improving the carbon conversion rate in the coal gasification reaction. In some embodiments, the gas flow in the reduction reactor 2 may be controlled to have a gas flow rate of 1-5 m/s, which may enable the materials in the coal gasification reaction to be mixed uniformly, and may enable products containing elemental iron and titanium-containing materials to be carried out relatively easily.
In the step S2, the particle size of the raw coal in the reduction reactor 2 affects the quality of the coal gasification reaction, under the disturbance of the gas flow, the coal particles and the oxygen-loaded ilmenite particles are uniformly mixed as much as possible, and if the particle size of the raw coal is too large, the raw coal is not in sufficient contact with the reaction atmosphere, which results in a long reaction time; if the particle size of the raw coal is too small, the processing cost of the raw coal is increased, and the coal gasification cost is increased indirectly. In some embodiments, the particle size of the raw coal participating in the coal gasification reaction in the reduction reactor 2 may be 2 to 10mm, and in this particle size range, the coal gasification reaction is relatively sufficient and the raw coal particles are easy to process.
Step S3: and (3) taking a part of products in the reduction reactor out by using the airflow, and separating the products taken out by the airflow to obtain combustible gas, simple substance iron and titanium-containing substances.
In step S3, the gas stream formed of the steam and the gas such as the combustible gas generated by the coal gasification reaction in the reduction reactor 2 carries the product having a particle size smaller than a predetermined value and enters the first separation device 4. In some embodiments, a portion of the products in reduction reactor 2 carried over by the gas stream comprises: elemental iron powder with the grain size of less than or equal to 0.5mm, titanium-containing material powder, oxygen carrier ore powder and the like, and products with the grain size of less than or equal to 0.5mm can be easily carried away by airflow.
With reference to fig. 2 and fig. 3, as a possible implementation manner, the step S3 specifically includes the following three steps:
step S31: and (3) carrying out gas-solid separation on the product carried by the airflow, extracting to obtain combustible gas, and discharging the product containing the elemental iron and the titanium-containing substance.
In the step S31, the gas-solid separation of the product in the reduction reactor 2 carried out by the gas flow can be performed by using a cyclone separator, which has the advantages of simple structure, low cost, convenient maintenance, etc.
In some embodiments, after the gas-solid separation and extraction are performed to obtain the crude combustible gas, the crude combustible gas may be further purified to obtain the combustible gas.
It should be noted that, in some embodiments, after step S31, between the extraction of the elemental iron from the product containing the elemental iron and the titanium-containing material, the product containing the elemental iron and the titanium-containing material is subjected to an oxygen-insulated cooling operation, so as to avoid that the elemental iron in the product is oxidized in an oxygen-containing and high-temperature environment, which affects the extraction efficiency of the elemental iron.
Step S32: carrying out magnetic separation on the product containing the simple substance iron and the titanium-containing substance, extracting to obtain the simple substance iron, and discharging the product containing the titanium-containing substance.
In step S32, the product containing elemental iron and the titanium-containing material is passed through a magnetic field, and the elemental iron is gathered together due to its high magnetic permeability to the magnetic field, thereby achieving extraction of the elemental iron.
In some embodiments, the product containing elemental iron and titanium-containing material may be magnetically separated multiple times to maximize extraction of the elemental iron.
Step S33: and (3) carrying out flotation and/or gravity separation on the product containing the titanium-containing substance, and extracting to obtain the titanium-containing substance.
In step S33, in the flotation process, a surfactant capable of generating a large amount of bubbles is used, and the bubbles can separate the titaniferous material from impurities, so as to extract the titaniferous material. In the gravity separation process, the extraction of the titaniferous material can be realized by utilizing the difference of the movement speed and the movement direction of different materials in the titaniferous material-containing product in a medium (water or other liquid with higher relative density).
In some embodiments, the titaniferous material can be extracted by flotation alone, gravity alone, or a combination of flotation and gravity. If the flotation and gravity separation are combined, the gravity separation can be carried out after the flotation, or the gravity separation can be carried out after the gravity separation. In addition, when flotation and/or gravity separation is carried out, multiple times of flotation and/or gravity separation can be carried out so as to extract titaniferous materials to the maximum extent.
Step S4: the product not carried over by the gas stream is returned to the oxidation reactor 1 and the oxygen load is renewed for reuse in the coal gasification reaction in the reduction reactor 2.
In the reduction reactor 2, the raw coal pyrolysis reaction generates semicoke. In the step S4, the products not taken out by the gas flow include reduced ilmenite and semicoke, in some embodiments, the mass of the semicoke is 20% to 30% of the mass of the raw coal, and both the reduced ilmenite and the semicoke carry a large amount of heat, so as to provide heat for the oxidation reaction in the oxidation reactor 1, and achieve the effect of improving the energy utilization rate to the maximum extent. It should be noted that the ilmenite ore is circulated between the oxidation reactor 1 and the reduction reactor 2 several times, the particle size of the ilmenite ore is continuously reduced, the degree of mechanical pulverization is gradually increased, when the particle size of the ilmenite ore is lower than a certain value, in some embodiments, when the particle size of the ilmenite ore is less than or equal to 0.5mm, most of the iron is already separated from the ilmenite ore skeleton, and the elemental iron is separated from the surface of the ilmenite ore particle and is further carried to the first separation device 4 by the gas flow. Thereby, the amount of the ilmenite ore circulated between the oxidation reactor 1 and the reduction reactor 2 is rapidly reduced, and in order to maintain the mass ratio of the ilmenite ore and the pulverized coal loaded with oxygen in the reduction reactor 2 within a certain range, in step S1, an operation of replenishing the ilmenite ore to the oxidation reactor 1 is further included.
Referring again to fig. 2 and 3, in some embodiments, the product in reduction reactor 2 is partially carried by the gas stream to first separation device 4 and partially returned to oxidation reactor 1, while residual product that is neither carried by the gas stream nor discharged to oxidation reactor 1 may be discharged from reduction reactor 2. The residual products in the reduction reactor 2 which are not carried away by the gas stream and are not discharged to the oxidation reactor 1 comprise ash, which is the mineral residue left after the coal gasification reaction of raw coal and the oxygen-loaded ilmenite, and the particles are large and can be deposited at the bottom of the reduction reactor 2. The ash residue does not participate in the chemical reaction and has no function of carrying heat, and the ash residue deposited at the bottom of the reduction reactor 2 for a long time can absorb the internal temperature of the reduction reactor 2 to cause heat waste and occupy the space in the reduction reactor 2, so the ash residue can be discharged from the reduction reactor 2 periodically or aperiodically to avoid the influence on the coal gasification reaction efficiency.
According to the coal gasification method provided by the embodiment of the invention, the cheap and easily-obtained ilmenite is used as the oxygen carrier to carry oxygen to the coal gasification reaction, so that oxygen required by the coal gasification reaction is provided, oxygen is supplied to the coal gasification reaction by utilizing the characteristic that the ilmenite is easy to oxidize and reduce, elemental iron is obtained, and the elemental iron with higher purity can be obtained by separating a product containing the elemental iron, so that economic benefits are brought, the defect of cost increase caused by high consumption of the oxygen carrier due to the use of a natural oxygen carrier is overcome, and the purpose of reducing the cost of the coal gasification reaction is realized.
In addition to the above-described detailed description of the coal gasification method according to the embodiment of the present invention, as shown in fig. 3, a coal gasification system according to an embodiment of the present invention includes: an oxidation reactor 1, a reduction reactor 2, and a first separation device 4. Wherein the oxidation reactor 1 is used for carrying out oxidation reaction on the ilmenite with oxygen-containing gas to obtain the oxygen-loaded ilmenite. The reduction reactor 2 is used to supply oxygen to the oxygen-loaded ilmenite, coal gasification reaction of the raw coal occurs, and reduction reaction of the oxygen-loaded ilmenite occurs to generate elemental iron. And the first separation equipment 4 is used for separating the product in the reduction reactor 2 to obtain combustible gas, elemental iron and titanium-containing substances. It should be noted that the "titanium-containing material" mainly includes titanium-containing oxide.
In some embodiments, as shown in fig. 3, in the above coal gasification system, the oxidation reactor 1 is provided with a first inlet port 11, an inlet port 12, and an outlet port 14. Wherein the first feed inlet 11 of the oxidation reactor is used for feeding the ilmenite, the gas inlet 12 of the oxidation reactor is used for feeding the oxygen-containing gas, and the discharge outlet 14 of the oxidation reactor is used for discharging the products in the oxidation reactor 1.
The reduction reactor 2 is provided with a first inlet port 21, a second inlet port 22, an inlet port 23, and a first outlet port 24. Wherein, the first feed inlet 21 of the reduction reactor is used for introducing the ferrotitanium ore loaded with oxygen, the second feed inlet 22 of the reduction reactor is used for introducing raw coal, the air inlet 23 of the reduction reactor is used for introducing water vapor, and the first discharge outlet 24 of the reduction reactor is connected with the first separation equipment 4 and is used for discharging the products which can be taken out by the gas flow in the reduction reactor to the first separation equipment 4.
As a possible design, as shown in fig. 3, the coal gasification system further comprises a second separation device 3 connected between the discharge port 14 of the oxidation reactor 1 and the first feed port 21 of the reduction reactor 2. The second separation equipment 3 is used for carrying out gas-solid separation on the product in the oxidation reactor 1 to obtain oxygen-poor gas and oxygen-loaded ilmenite, discharging the oxygen-poor gas and introducing the oxygen-loaded ilmenite into the reduction reactor 2. The "oxygen-deficient gas" means that in the oxidation reactor 1, oxygen in the oxygen-containing gas is supported in the ilmenite ore, and the oxygen content in the oxygen-containing gas is reduced to become an oxygen-deficient gas.
In some embodiments, the second separating apparatus 3 comprises a cyclonic separator. The cyclone separator separates the oxygen-bearing titanyl iron ore with larger inertial centrifugal force from the airflow by means of the rotary motion of the oxygen-poor gas airflow, so as to realize the separation of the oxygen-poor gas and the oxygen-bearing titanic iron ore.
In some embodiments, the second separation device 3 is provided with an inlet 31, an outlet 32 and an outlet 33. Wherein the inlet 31 of the second separation device is used for introducing the product in the oxidation reactor 2, the outlet 32 of the second separation device is used for discharging oxygen-poor gas, and the outlet 33 of the second separation device is used for discharging the oxygen-loaded ilmenite.
As a possible design, continuing to refer to fig. 3, the reduction reactor 2 is also provided with a second discharge 25, the second discharge 25 of the reduction reactor being used for discharging the product containing the reduced ilmenite. The oxidation reactor 1 is also provided with a second inlet 13, the second inlet 13 of the oxidation reactor being for the introduction of a product containing reduced ilmenite in the reduction reactor 2. The second discharge port 25 of the reduction reactor is communicated with the second feed port 13 of the oxidation reactor, the reduced ilmenite in the reduction reactor 2 is returned to the oxidation reactor 1 through the second discharge port 25 of the reduction reactor and the second feed port 13 of the oxidation reactor which are communicated, oxygen loading is continued, after the oxygen loading is performed, the oxygen-loaded ilmenite is returned to the reduction reactor 2 through the discharge port 33 of the first separation device and the first feed port 21 of the reduction reactor, oxygen is supplied for the coal gasification reaction in the reduction reactor 2, and thus, the ilmenite is continuously circulated between the oxidation reactor 1 and the reduction reactor 2, and is mechanically pulverized due to continuous oxidation and reduction of iron inside while supplying oxygen for the coal gasification reaction in the reduction reactor 2, and subsequent extraction of elemental iron and titaniferous materials is facilitated.
In addition, in the process that the ilmenite continuously circulates between the oxidation reactor 1 and the reduction reactor 2, the ilmenite carries heat to continuously circulate between the oxidation reactor 1 and the reduction reactor 2, so that the heat is recycled, the heat directly supplied from the outside is reduced, the cost is saved to a certain extent, and the economic benefit of the whole coal gasification reaction is improved.
Furthermore, in some embodiments, pyrolysis of the raw coal in reduction reactor 2 produces char, which is also capable of carrying heat with the ilmenite constantly circulating between oxidation reactor 1 and reduction reactor 2, thereby increasing the amount of heat that can be recycled.
As a possible design, the reduction reactor 2 is further provided with a third discharge port 26, and the third discharge port 26 of the reduction reactor is used for discharging residual products (including ash) which are not taken away by the gas flow in the coal gasification reaction and are not discharged to the oxidation reactor 1, so as to avoid heat waste caused by the fact that the residual products (including ash) are deposited at the bottom of the reduction reactor 2 for a long time to absorb the internal temperature of the reduction reactor 2, and avoid occupying the space in the reduction reactor 2 to influence the coal gasification reaction efficiency.
In some embodiments, the third discharge port 26 of the reduction reactor may be provided at the bottom of the reduction reactor 2 to facilitate efficient discharge of residual products (including ash) deposited at the bottom of the reduction reactor 2.
With continued reference to fig. 3, in some embodiments, the first separation apparatus 4 includes a primary separation device 5 for extracting combustible gas from the product of the reduction reactor 2 to remove primary residual material. And the secondary separation device 6 is used for extracting the simple substance iron in the primary residual substances and discharging secondary residual substances. And the third-stage separation device 7 is used for extracting titanium-containing materials in the second-stage residual materials.
In some embodiments, the primary separation device 5 comprises a cyclone separator, the secondary separation device 6 comprises a magnetic separator, and the tertiary separation device 7 comprises a flotation separator and/or a gravity separator. The cyclone separator generates a rotational motion by means of the airflow in the reduction reactor 2, so that the product containing the elemental iron and the titanium-containing substance with larger inertial centrifugal force is separated from the airflow, and the separation (gas-solid separation) of the combustible gas from the product containing the elemental iron and the titanium-containing substance is realized. The magnetic separator utilizes the characteristic of high conductivity of elementary substance iron to gather the elementary substance iron, thereby realizing the extraction of the elementary substance iron. The flotation separator extracts the titaniferous material by utilizing bubbles generated by the surfactant. The gravity separator utilizes the difference of the movement speed and direction of different substances in the secondary residual substances in a medium (water or other liquid with higher relative density) to realize the extraction of the titaniferous substances.
As a possible design, the primary separation device 5 is provided with a feed opening 51, a gas outlet 52 and a discharge opening 53. The inlet 51 of the primary separation device is communicated with the first outlet 24 of the reduction reactor. The inlet 51 of the first-stage separation device is used for introducing products brought out by the airflow in the reduction reactor, the outlet 52 of the first-stage separation device is used for discharging the extracted combustible gas, and the outlet 53 of the first-stage separation device is used for discharging first-stage residual substances which are products containing elemental iron and titanium-containing substances.
As a possible design, the secondary separation device 6 is provided with a feed opening 61, a first discharge opening 62 and a second discharge opening 63. The inlet 61 of the secondary separation device is communicated with the outlet 53 of the primary separation device. The inlet 61 of the secondary separation device is used for introducing the primary residual substances. The first discharge port 62 of the secondary separation device is used for discharging the extracted elemental iron, and the second discharge port 63 of the secondary separation device is used for discharging secondary residual substances, wherein the secondary residual substances are products containing titanium-containing substances.
As a possible design, the tertiary separation device 7 is provided with a feed opening 71, a first discharge opening 72 and a second discharge opening 73. The feed inlet 71 of the third-stage separation device is communicated with the second discharge outlet 63 of the second-stage separation device. The inlet 71 of the third stage separation device is used for introducing the second stage residual substances. The first outlet 72 of the tertiary separation device is used to discharge the extracted titaniferous material and the second outlet 73 of the tertiary separation device is used to discharge ash. The "ash" refers to a series of physical and chemical changes in coal gasification reaction at high temperature, and finally organic components are volatilized and dissipated, while inorganic components (mainly inorganic salts and oxides) remain, and the residue is called ash.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.
Claims (9)
1. A coal gasification process, characterized in that it comprises:
putting the ilmenite into an oxidation reactor, and introducing oxygen-containing gas to perform oxidation reaction on the ilmenite so as to obtain oxygen-loaded ilmenite;
placing the oxygen-loaded ilmenite and raw coal in a reduction reactor, and introducing steam, wherein the oxygen-loaded ilmenite provides oxygen, the raw coal is subjected to coal gasification reaction, and the oxygen-loaded ilmenite is subjected to reduction reaction to generate elemental iron;
carrying out gas flow to remove a part of products in the reduction reactor, and separating the products carried out by the gas flow to obtain combustible gas, elemental iron and titanium-containing substances;
returning the products which are not carried out by the gas flow to the oxidation reactor, and carrying out oxygen loading again to be used for the coal gasification reaction in the reduction reactor again;
the step of separating the products brought by the airflow to obtain combustible gas, elemental iron and titanium-containing substances comprises the following steps: carrying out gas-solid separation on the product carried by the airflow, extracting to obtain combustible gas, and discharging a product containing elemental iron and a titanium-containing substance; carrying out magnetic separation on the product containing the elemental iron and the titanium-containing substance, extracting to obtain the elemental iron, and discharging the product containing the titanium-containing substance; and (3) carrying out flotation and/or gravity separation on the product containing the titanium-containing substance, and extracting to obtain the titanium-containing substance.
2. The coal gasification method according to claim 1, wherein the particle size of the ilmenite ore is 0.5 to 3mm, and the particle size of the raw coal is 2 to 10 mm.
3. The coal gasification method according to claim 1, wherein the gas flow in the oxidation reactor has a gas velocity of 0.5 to 2m/s and a temperature of 1000 to 1100 ℃.
4. The coal gasification method according to claim 1, wherein the gas flow in the reduction reactor has a gas velocity of 1 to 5m/s and a temperature of 700 to 900 ℃.
5. The coal gasification process of claim 1, wherein a fraction of the product in the reduction reactor carried over with the gas stream has a particle size of less than or equal to 0.5 mm.
6. The coal gasification method according to claim 1, wherein between the step of introducing oxygen-containing gas into the oxidizing reactor to which the ilmenite ore with the oxygen-loaded ilmenite ore and the raw coal are introduced into the reducing reactor, steam is introduced, the method further comprises: and carrying out gas-solid separation on the product in the oxidation reactor to obtain oxygen-poor gas and oxygen-loaded ilmenite, discharging the oxygen-poor gas, and introducing the oxygen-loaded ilmenite into the reduction reactor.
7. The coal gasification process of claim 1, further comprising: discharging the residual product in the reduction reactor out of the reduction reactor; wherein the residual product is a product in the reduction reactor that is neither carried over by the gas stream nor returned to the oxidation reactor.
8. A coal gasification system, characterized in that the coal gasification system comprises:
the oxidation reactor is used for carrying out oxidation reaction on the ilmenite and oxygen-containing gas to obtain the oxygen-loaded ilmenite; the oxidation reactor is provided with a first feed inlet for introducing the titaniferous iron ore, a gas inlet for introducing oxygen-containing gas and a discharge outlet for discharging products in the oxidation reactor;
a reduction reactor for supplying oxygen to the oxygen-loaded ilmenite, coal gasification reaction of raw coal occurs, and the oxygen-loaded ilmenite undergoes reduction reaction to generate elemental iron; the reduction reactor is provided with a first feed port for introducing the oxygen-loaded ilmenite, a second feed port for introducing the raw coal, an air inlet for introducing water vapor and a first discharge port for discharging a product brought out by air flow in the reduction reactor;
the first separation equipment is used for separating a product brought out by the airflow in the reduction reactor to obtain combustible gas, elemental iron and a titanium-containing substance; the first separation equipment is connected with a first discharge hole of the reduction reactor;
the first separation apparatus comprises: the cyclone separator is connected with the reduction reactor and is used for carrying out gas-solid separation on the product in the reduction reactor, extracting to obtain combustible gas and discharging the product containing the elemental iron and the titanium-containing material; the magnetic separator is connected with the cyclone separator and is used for carrying out magnetic separation on the product containing the elemental iron and the titanium-containing substances, extracting the elemental iron and discharging the product containing the titanium-containing substances; the flotation separator and/or gravity separator is connected with the magnetic separator and is used for performing flotation and/or gravity separation on the product containing the titanium-containing substance to extract the titanium-containing substance;
the coal gasification system further comprises: and the second separation equipment is connected between the discharge hole of the oxidation reactor and the first feed hole of the reduction reactor and is used for carrying out gas-solid separation on the product in the oxidation reactor to obtain oxygen-poor gas and oxygen-loaded ilmenite, discharging the oxygen-poor gas and introducing the oxygen-loaded ilmenite into the reduction reactor.
9. The coal gasification system according to claim 8, wherein the oxidation reactor is further provided with a second feed inlet for the reduced ilmenite ore into the reduction reactor;
the reduction reactor is also provided with a second discharge hole for discharging reduced ilmenite;
and the second feed inlet of the oxidation reactor is communicated with the second discharge outlet of the reduction reactor.
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| CN111996060B (en) * | 2020-09-15 | 2022-06-24 | 中国石油化工股份有限公司 | Titanium-iron ore oxygen carrier modified by perovskite structure oxide and preparation method thereof |
| CN113832280A (en) * | 2021-09-01 | 2021-12-24 | 新奥科技发展有限公司 | Method and apparatus for producing reduced ilmenite |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101875483A (en) * | 2009-04-29 | 2010-11-03 | Ifp公司 | Integrated process for production of energy and/or synthesis gas by production of oxygen in situ, combustion and gasification in a chemical cycle |
| CN101896581A (en) * | 2007-12-12 | 2010-11-24 | 奥图泰有限公司 | Process and plant for producing char and fuel gas |
| CN203333695U (en) * | 2013-05-23 | 2013-12-11 | 北京神雾环境能源科技集团股份有限公司 | Cold-feeding conveying-bed smelting system for preparing reducing gas through medium-level and low-level coal gasification |
| WO2017111614A1 (en) * | 2015-12-22 | 2017-06-29 | Institutt For Energiteknikk | Sustainable oxygen carriers for chemical looping combustion with oxygen uncoupling and methods for their manufacture |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7083658B2 (en) * | 2003-05-29 | 2006-08-01 | Alstom Technology Ltd | Hot solids gasifier with CO2 removal and hydrogen production |
| US8202349B2 (en) * | 2009-06-30 | 2012-06-19 | General Electric Company | Method and apparatus for removal of carbon dioxide from pre-combustion syngas |
| CN101891147B (en) * | 2010-08-11 | 2013-05-01 | 华北电力大学 | Solid fuel fluidized bed near-zero emission hydrogen generating device |
| CN103060003A (en) * | 2012-12-27 | 2013-04-24 | 东南大学 | Method and device for preparing H2 and separating CO2 based on calcium-based sorbent |
| CN104848207B (en) * | 2015-04-07 | 2017-09-01 | 东南大学 | The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation |
| CN106244241B (en) * | 2016-07-19 | 2018-12-14 | 东南大学 | A kind of coal gasification preparing synthetic gas and chemical chain oxygen-hydrogen manufacturing combined cycle power plant and method |
| CN107142125A (en) * | 2017-06-07 | 2017-09-08 | 中国科学院广州能源研究所 | A kind of sludge chemical chain gasification orientation produces synthetic gas method and realizes the device of this method |
| CN207193218U (en) * | 2017-08-01 | 2018-04-06 | 东北大学 | A kind of biomass char vaporizing system for synthesis gas system |
| CN107523361A (en) * | 2017-09-26 | 2017-12-29 | 中国科学院广州能源研究所 | High nitrogen antibiotic bacterium dregs prepare the process and system of low nitrogen biological fuel gas |
-
2018
- 2018-08-17 CN CN201810940301.0A patent/CN109054900B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101896581A (en) * | 2007-12-12 | 2010-11-24 | 奥图泰有限公司 | Process and plant for producing char and fuel gas |
| CN101875483A (en) * | 2009-04-29 | 2010-11-03 | Ifp公司 | Integrated process for production of energy and/or synthesis gas by production of oxygen in situ, combustion and gasification in a chemical cycle |
| CN203333695U (en) * | 2013-05-23 | 2013-12-11 | 北京神雾环境能源科技集团股份有限公司 | Cold-feeding conveying-bed smelting system for preparing reducing gas through medium-level and low-level coal gasification |
| WO2017111614A1 (en) * | 2015-12-22 | 2017-06-29 | Institutt For Energiteknikk | Sustainable oxygen carriers for chemical looping combustion with oxygen uncoupling and methods for their manufacture |
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